JP2019042628A - Gas-liquid mixer - Google Patents

Abstract

To provide a gas-liquid mixer capable of mixing gas and liquid highly efficiently.SOLUTION: A gas-liquid mixer 20 includes a cylindrical body 22 in which an inlet part 28 of a fluid containing gas and liquid is formed on one end in the axial direction, and an outlet part 30 of the fluid is formed on the other end in the axial direction, a plurality of partition parts 24, each having a plurality of openings 24A, provided in the cylindrical body 22 at intervals in the axial direction of the cylindrical body 22, for partitioning the inside of the cylindrical body 22 in the axial direction, and flow rate lowering means (as a sample, a flow rate degradation structure 26) for lowering a flow rate of the liquid flowing in the cylindrical body 22 furthermore than a flow rate of the liquid flowing in the inlet part 28.SELECTED DRAWING: Figure 1

Description

  The present invention relates to a gas-liquid mixing device.

  Conventionally, in the case of dissolving a gas with low solubility in a liquid such as water, a method of bubbling by flowing the gas through a porous body (made of resin, metal, ceramic etc.) installed in the liquid, Method of mixing gas and liquid (gas and liquid) using jig of ejector structure, method of atomizing high pressure gas through fine nozzle and spraying into liquid, passing gas liquid through several spiral slits Methods such as stirring and mixing have been used.

  For example, the aeration (aeration) method is a method of sending a gas (mainly oxygen) into water, and in recent years, aeration using microbubbles has increased. However, in addition to the need for high-pressure gas, it takes several tens of minutes to saturate the concentration of dissolved gas (for example, oxygen) in water, and there is a problem that the gas dissolution efficiency is low.

  The bubble-free oxygen dissolution method is a method in which high pressure water is sprayed and fed into a tank filled with high pressure oxygen gas, and oxygen is dissolved in water by contacting atomized water with pressurized oxygen. How to However, it requires an oxygen tank that can withstand high pressure, a high pressure pump that feeds water, etc., which makes the apparatus expensive and requires power.

  On the other hand, there is a static mixer which does not use power as a static gas-liquid mixing method. This device is a system in which gas and liquid are passed through a mixing section with a complicated shape to break up and refine air bubbles, and they are mixed by swirling and turbulent flow, but they are mixed using liquid and gas. The efficiency of the In addition, it is necessary to reduce the inner diameter of the gas-liquid mixing device in order to create a turbulent flow state, and as a result, the pressure loss is also large. For example, Patent Document 1 discloses a method of stacking a plurality of meshes and flowing gas and liquid horizontally or vertically to the mesh surface to promote dissolution. In this patent document 1, gas and liquid are allowed to flow horizontally from the end of the mesh having unevenness to the mesh surface to divide air bubbles, causing micro vortices to occur and mix the gas and liquid (mixture of gas and liquid). ing. However, when the gas and liquid flow horizontally to the closely stacked mesh, the flow becomes laminar and agitation is not performed, and the pressure loss in the mixer becomes large, so the air under low pressure loss It is difficult to do liquid mixing. Furthermore, since the gas and the liquid are not stirred, a partial flow is likely to occur, which may result in insufficient mixing.

Unexamined-Japanese-Patent No. 8-173782

  The present invention has been made in view of the above-mentioned facts, and an object of the present invention is to provide a gas-liquid mixing device capable of mixing a gas and a liquid with high efficiency.

  In the gas-liquid mixing device according to the first aspect of the present invention, an inlet for fluid containing gas and liquid is formed at one end in the axial direction, and an outlet for the fluid is formed at the other end in the axial direction. A cylinder and a plurality of openings are provided in the cylinder at intervals in the axial direction of the cylinder, and a plurality of partition parts for partitioning the cylinder in the axial direction, and the flow through the inlet And a flow rate reduction means for reducing the flow rate of the liquid flowing in the cylinder than the flow rate of the liquid.

In the gas-liquid mixing device of the first aspect, the fluid containing gas and liquid flows into the cylinder through the inlet. At this time, the flow velocity reduction means reduces the flow velocity of the liquid in the cylinder than the inlet portion. Furthermore, since the cylinder is axially divided by the partition part, for example, the flow velocity of the liquid in the cylinder is lower than that of the configuration in which the partition part is not disposed in the cylinder. For this reason, the gas in the fluid exhibits a behavior similar to or similar to the floating behavior in the stationary water to form a gas pool in the cylinder. On the other hand, the liquid flows in a gas reservoir formed in the cylinder, and is dispersed and finely divided when passing through a plurality of openings in a partition provided in the middle. Thus, the contact area (gas-liquid contact area) of the liquid and the gas is increased by the liquid being dispersed and finely divided. Then, the gas is dissolved in the liquid in the space formed between the adjacent partition parts (in other words, the mixing of the gas and the liquid is promoted).
Here, in the gas-liquid mixing device, for example, the gas and the liquid are allowed to flow through a mesh or the like so that the bubbles are dispersed, in order to disperse the liquid in the gas reservoir formed in the cylinder and make the liquid into fine droplets and dissolve the gas in the liquid. Gas and liquid can be mixed with high efficiency as compared with the prior art in which gas and liquid are mixed by fragmentation and refinement.

  The gas-liquid mixing device according to a second aspect of the present invention is the gas-liquid mixing device according to the first aspect, wherein the flow velocity reduction means has an inner diameter of the cylindrical body larger than an inner diameter of the inlet.

  In the gas-liquid mixing device according to the second aspect, since the inner diameter of the cylindrical body is larger than the inner diameter of the inlet, for example, the inner diameter of the cylindrical body is smaller than that of the inlet. The channel cross-sectional area is increased. Thereby, the pressure loss when the liquid flows in the cylinder can be reduced.

  The gas-liquid mixing device according to a third aspect of the present invention is the gas-liquid mixing device according to the first aspect or the second aspect, wherein the flow velocity reduction means is disposed between the inlet portion and the partition portion It has a baffle that blocks the flow.

  In the gas-liquid mixing device according to the third aspect, since the baffle plate is disposed between the inlet portion and the partition portion, the flow of the fluid flowing from the inlet portion is blocked by the baffle plate, and the flow velocity of the liquid in the cylinder is the inlet. Lower than part. Here, in the gas-liquid mixing device, by disposing the baffle plate between the inlet portion and the partition portion, the flow velocity of the liquid flowing in the cylinder can be easily adjusted.

  A gas-liquid mixing device according to a fourth aspect of the present invention is the gas-liquid mixing device according to any one of the first to third aspects, wherein a space is maintained between the axially adjacent partitions. Holding members are disposed.

  In the gas-liquid mixing device of the fourth aspect, by arranging the holding member between the partitions adjacent to each other in the axial direction of the cylinder, the space between the adjacent partitions can be easily held.

  A gas-liquid mixing device according to a fifth aspect of the present invention is the gas-liquid mixing device according to any one of the first to fourth aspects, wherein the dividing portion is constituted by a dividing member in which a plurality of openings are formed. Among the plurality of partition portions, the partition portion near the inlet portion is configured by stacking the plurality of partition members.

  In the gas-liquid mixing device of the fifth aspect, among the plurality of partition portions, the partition portions near the inlet portion are configured by overlapping the plurality of partition members. For this reason, the dynamic pressure of the fluid flowing into the cylinder decreases at the beginning of the inflow, and the flow velocity distribution of the liquid in the cylinder becomes uniform. Thereby, a gas reservoir is easily formed in the cylinder.

  A gas-liquid mixing device according to a sixth aspect of the present invention is the gas-liquid mixing device according to the fifth aspect, wherein the positions of the openings of the axially stacked partition members are offset in the axial direction.

  In the gas-liquid mixing device of the sixth aspect, the position of the opening of one partition member and the position of the openings of the other partition members stacked on the one partition member are offset in the axial direction, for example, The liquid can be dispersed and finely divided as compared with the configuration in which the positions of the openings do not shift in the axial direction (the same in the axial direction).

  The gas-liquid mixing device according to a seventh aspect of the present invention is the gas-liquid mixing device according to the fifth aspect or the sixth aspect, wherein the partition member is formed of plain weave or twill weave mesh, expanded metal, or a plurality of through holes. A plate-like member.

  In the gas-liquid mixing device according to the seventh aspect, since a member capable of setting a large number of openings is used as the partition member, the liquid can be further dispersed and finely divided when the liquid passes through the plurality of openings of the partition member.

  The gas-liquid mixing device according to an eighth aspect of the present invention is the gas-liquid mixing device according to any one of the first to seventh aspects, wherein a plurality of the inlet and the outlet are formed in the cylinder. ing.

  In the gas-liquid mixing device according to the eighth aspect, since a plurality of inlets and outlets are formed in the cylinder, for example, compared with a configuration in which one inlet and outlet are formed in the cylinder, the cylinder It is possible to suppress the drift of fluid in

  The gas-liquid mixing device according to a ninth aspect of the present invention is the gas-liquid mixing device according to any one of the first to eighth aspects, wherein the cross-sectional average flow velocity of the liquid flowing in the cylinder is less than 0.3 m / s. It is.

  In the gas-liquid mixing device of the ninth aspect, since the cross-sectional average flow velocity of the liquid flowing in the cylinder is a low-speed flow area of less than 0.3 m / s, the gas behaves similarly or similar to the floating behavior in the stationary water in the cylinder. It is easy to show behavior and a gas reservoir is easily formed in the cylinder. For this reason, in the above-described gas-liquid mixing apparatus, for example, a gas reservoir is easily formed in the cylinder compared with a configuration in which the cross-sectional average flow velocity of the liquid is 0.3 m / s or more, and the gas and the liquid are mixed efficiently. be able to.

  ADVANTAGE OF THE INVENTION According to this invention, the gas-liquid mixing apparatus which can mix gas and a liquid with high efficiency can be provided.

1 is a cross-sectional view of a gas-liquid mixing device according to an embodiment of the present invention. It is an image figure of the gas-liquid mixing mode in the gas-liquid mixing apparatus in FIG. 5 is a flow diagram of a test apparatus for evaluating the performance of the gas-liquid mixing device of Example 1. FIG. It is a graph which shows the relationship between the water flow rate of the gas-liquid mixing apparatus of Example 1 and the comparative example 1, and dissolved oxygen concentration. It is a graph which shows the relationship between the water flow rate of the gas-liquid mixing apparatus of Example 1 and the comparative example 1, and pressure loss. It is a graph which shows the relationship between the water flow rate of the gas-liquid mixing apparatus of Example 1 and the comparative example 1, and oxygen solubility. It is a graph which shows the relationship between the Reynolds number of a gas-liquid mixing apparatus of Example 1 and the comparative example 1, and oxygen solubility. It is a graph which shows the relationship between the water flow volume of the gas-liquid mixing apparatus of Comparative Example 1 and Comparative Example 2, and dissolved oxygen concentration. FIG. 2 is a flow diagram of a recycling type ozone water production device to which the gas-liquid mixing device of Example 1 is applied. It is a graph which shows a time-dependent change of the density | concentration of the ozone water produced | generated with the recycle water electrolyzer of FIG. (A) batch system, (b) continuous extraction system. FIG. 2 is a flow diagram of a recycling type hydrogen water producing device to which the gas-liquid mixing device of Example 1 is applied. It is a graph which shows a time-dependent change of the density | concentration of the hydrogen water produced | generated with the recycling type hydrogen water production apparatus of FIG.

  Hereinafter, a gas-liquid mixing apparatus according to an embodiment of the present invention will be described.

<Gas-Liquid Mixing Device>
FIG. 1 shows a cross-sectional view of the gas-liquid mixing device 20 of the present embodiment. The gas-liquid mixing device 20 is a device that dissolves a gas in a liquid and mixes the gas and the liquid.

  The gas-liquid mixing device 20 includes a cylindrical body 22, a partition 24 provided in the cylindrical body 22, and a flow velocity reduction structure 26.

(Tube 22)
The cylindrical body 22 is cylindrical as shown in FIG. 1, and an inlet 28 is formed at one end in the axial direction (upper end in FIG. 1), and the other end in the axial direction (FIG. 1) An outlet 30 is formed at the lower end). Describing the cylinder 22 in detail, the cylinder 22 includes an upper cylinder 22A integrated with the inlet 28 and a lower cylinder 22B integrated with the outlet 30, and the lower cylinder 22B. The upper end portion of the upper case 22 is fitted into the upper cylindrical body 22A from below.

  The upper cylindrical body 22A is a cylindrical member having a ceiling, and an inlet 28 is formed in the ceiling. The inlet 28 is constituted by a pipe extending along the axial direction of the upper cylindrical body 22A (the same as the axial direction of the cylindrical body 22).

  The lower cylindrical body 22B is a cylindrical member having a bottom, and the outlet 30 is formed at the bottom. The outlet 30 is constituted by a pipe extending along the axial direction of the lower cylindrical body 22B (the same as the axial direction of the cylindrical body 22).

  Further, the inner diameter D1 of the cylindrical body 22 is larger than the inner diameter D2 of the inlet 28 and the inner diameter D3 of the outlet 30.

  As a material for forming the cylindrical body 22, a resin, a metal or the like may be used. In addition, it is preferable to select the material suitable for the kind of fluid as a material which forms the cylinder 22. As shown in FIG. For example, when dissolving a corrosive gas such as ozone to a high concentration in a liquid, as a material of the cylindrical body 22, a resin of Teflon (registered trademark) such as PFA or a corrosion resistant material such as titanium may be used. preferable. When used for a low corrosive fluid, general purpose plastics such as polyethylene, polypropylene, polyvinyl chloride and stainless steel may be used. Further, when it is desired to use a material having high thermal conductivity, aluminum or copper may be used.

  Further, the shape of the cylindrical body 22 is not limited to the cylindrical shape. For example, the shape of the cylindrical body 22 may be a polygonal cylindrical shape (cylindrical shape with a sectional polygonal shape) or an elliptical cylindrical shape.

  In addition, the cylindrical body 22 of this embodiment is an example of the cylindrical body in this invention.

(Partitioner 24)
As shown in FIG. 1, the partition portion 24 has a plurality of openings 24A, and a plurality of openings 24A are provided in the cylindrical body 22 at intervals in the axial direction of the cylindrical body 22, and the inside of the cylindrical body 22 is Divided in the axial direction. The partition portion 24 is constituted by one partition member 32 having a plurality of openings 24A. The outer shape of the partition member 32 is the same as the inner shape of the cylindrical body 22 (in the present embodiment, the outer shape of the partition member 32 is circular), and the outer peripheral portion is in close contact with the inner peripheral surface of the cylindrical body 22 . Further, the partition member 32 extends in a direction orthogonal to the axial direction of the cylinder 22.

  As the partition member 32, a plain weave or twill weave mesh, an expanded metal, or a plate-like member having a plurality of through holes may be used. The partition member 32 is not particularly limited to the above configuration as long as the liquid can be dispersed and finely divided.

Moreover, as a material which forms the partition member 32, although what, such as a fiber, a plastics, and a metal, may be used, it is preferable to select the material which does not corrode easily with the fluid to be used. For example, in the case of dissolving ultra-high concentration ozone in a liquid, it is preferable to use titanium and Teflon (registered trademark) or the like having high corrosion resistance as the material of the partition member 32.
On the other hand, when hydrogen, oxygen or nitrogen, etc., which is less corrosive, is dissolved in the liquid, the material of the partition member 32 may be general-purpose resin, nylon, engineering plastic, stainless steel, carbon steel, copper or aluminum having high thermal conductivity. It is preferable to use a material.

  In addition, the partition part 24 of this embodiment is an example of the partition part in this invention.

(Flow velocity reduction structure 26)
The flow velocity reduction structure 26 lowers the flow velocity (cross-sectional average flow velocity U2) of the liquid flowing in the cylinder 22 more than the flow velocity of the liquid flowing through the inlet 28 (cross-sectional average flow velocity U1), as shown in FIGS. Structure. The flow velocity reduction structure 26 will be described in more detail. The flow velocity reduction structure 26 is a structure in which the inner diameter D1 of the cylindrical body 22 is larger than the inner diameter D2 of the inlet 28. In the flow velocity reduction structure 26 of the present embodiment, the inner diameter D1 of the cylindrical body 22 is larger than the inner diameter D3 of the outlet 30.

  In addition, the cross-sectional average flow velocity U2 of the liquid flowing from the inlet portion 28 in the upper portion in the cylindrical body 22 toward the outlet portion 30 in the lower portion is less than 0.3 m / s. Specifically, the inner diameter D1 of the cylindrical body 22 is set such that the cross-sectional average flow velocity U2 of the liquid flowing through the cylindrical body 22 is less than 0.3 m / s.

  Further, the cross-sectional average flow velocity U1 of the liquid flowing through the inlet 28 is set to 0.3 m / s or more and 1 m / s or less. Specifically, the inner diameter D1 of the inlet 28 is set such that the cross-sectional average flow velocity U1 of the liquid flowing through the inlet 28 is less than 0.3 m / s.

  The flow velocity reduction structure 26 of the present embodiment is an example of the flow velocity reduction means in the present invention.

(Holding member 34)
The gas-liquid mixing device 20 also includes a holding member 34. This holding member 34 is arrange | positioned between the partition parts 24 (partition member 32) adjacent to the axial direction of the cylindrical body 22, as FIG. 1 shows. The spacing between the adjacent partitions 24 is maintained by the holding member 34. In other words, the space portion 36 is formed between the adjacent partition portions 24 by the holding member 34.

  The holding member 34 is not particularly limited as long as it can hold the space between the adjacent partition portions 24. For example, an O-ring or packing may be used. Further, as a material for forming the holding member 34, a material similar to that of the partition member 32 (for example, Teflon (registered trademark) or titanium) may be used.

  Next, the operation and effect of the present embodiment will be described.

First, before describing the operation and effect of the present embodiment, a gas-liquid mixing device of a reference example in which the partition portion 24 is not disposed in the cylindrical body 22 will be described. In the gas-liquid mixing device of this reference example, the cylinder 22 is formed of transparent acrylic resin, and the partition portion 24 is not disposed in the cylinder 22. A fluid (mixture) containing gas (here, oxygen gas) and liquid (here, water) from the inlet 28 (here, 3/8 inch piping) in the cylinder 22 of the gas-liquid mixing apparatus of this reference example The flow condition of the fluid when it was poured was observed. Note that the flow rate of oxygen gas (hereinafter referred to as “oxygen gas flow rate” as appropriate) is 120 mL / min, and the flow rate of water (hereinafter referred to as “water flow rate” as appropriate) is 1 L / min to 8 L / min. did.
As a result of observation, it was revealed that oxygen gas fills the inside of the cylindrical body 22 to form a gas reservoir (gas reservoir) when the water flow rate is 1 L / min to 2 L / min. On the other hand, the water flowed down along the inner peripheral surface of the cylindrical body 22. Thus, even when the partition portion 24 and the holding member 34 are not disposed, although a gas reservoir can be formed in the cylindrical body 22, most of the liquid flows down the inner peripheral surface of the cylindrical body 22, so the contact area between the gas and the liquid Became smaller, and it was found that mixing of gas and liquid did not proceed. In addition, when the water flow rate is 4 L / min or more, the dynamic pressure of the fluid supplied from the thin inlet 28 into the cylinder 22 becomes high, so the flow velocity of the liquid flowing in the cylinder 22 is not sufficiently reduced. It turned out that a gas reservoir can not be formed in the cylinder 22.
Therefore, it has become clear that, by arranging the partition part 24 in the cylindrical body 22, the liquid in the cylindrical body 22 can be subdivided and finely divided to increase the gas-liquid contact area. Further, by arranging the partition part 24 in the cylindrical body 22, the dynamic pressure of the fluid flowing into the cylindrical body 22 from the inlet part 28 is suppressed, and the flow velocity in the cylindrical body 22 becomes low and substantially uniform. It turned out that a gas reservoir becomes easy to be formed.

  In the gas-liquid mixing device 20 of the present embodiment, as shown in FIG. 2, a fluid containing gas and liquid flows (flows down) into the cylindrical body 22 through the inlet 28. At this time, since the fluid flows down perpendicularly to the surface of the partition 24 (partition member 32) of the cylindrical body 22, for example, the fluid flows down along the surface of the partition 24 (partition member 32) as compared with the conventional configuration. Gas and liquid can be mixed. Furthermore, since the outer peripheral portion of the partition member 32 is in close contact with the inner peripheral surface of the cylindrical body 22, it is possible to suppress the flow of fluid from falling between the outer peripheral portion of the partition member 32 and the inner peripheral surface of the cylindrical body 22. Therefore, for example, the gas and the liquid can be mixed more than in the case where the gas and the liquid flow down from between the outer peripheral portion of the partition member 32 and the inner peripheral surface of the cylindrical body 22.

  Then, the flow velocity of the liquid (the cross-sectional average flow velocity) of the fluid flowing into the cylinder 22 from the inlet 28 is reduced in the cylinder 22 than the inlet 28 by the flow velocity reduction structure 26. Specifically, since the inner diameter D1 of the cylindrical body 22 is larger than the inner diameter D2 of the inlet portion 28, the cross sectional average flow velocity U2 of the liquid in the cylindrical body 22 is higher than the cross sectional average flow velocity U1 at the inlet portion 28 descend. Further, since the inside of the cylindrical body 22 is axially divided by the partition portion 24, the flow velocity of the fluid becomes low and substantially uniform in the cylindrical body 22. At this time, the gas in the fluid forms a gas pool Z in the cylindrical body 22 with a behavior similar or similar to the floating behavior in the stationary water. On the other hand, the liquid flows in the gas reservoir Z formed in the cylindrical body 22, and is dispersed and finely divided when passing through the plurality of openings 24A in the partition portion 24 provided on the way. Thus, the contact area (gas-liquid contact area) of the liquid and the gas is increased by the liquid being dispersed and finely divided. Then, the gas is dissolved in the liquid in the space 36 formed between the adjacent partitions 24 (in other words, the mixing of the gas and the liquid is promoted).

  Here, in the gas-liquid mixing device 20, for example, the gas and the liquid are flowed through a mesh or the like to disperse the gas in the liquid by dispersing and finely dispersing the liquid in the gas reservoir Z formed in the cylindrical body 22. The gas and the liquid can be mixed with high efficiency as compared with the prior art in which the air bubbles are subdivided and miniaturized to mix the gas and the liquid.

  Further, in the gas-liquid mixing device 20, since the inner diameter D1 of the cylindrical body 22 is larger than the inner diameter D2 of the inlet 28, for example, the inside of the cylindrical body 22 is smaller than the inner diameter D1 or less. The channel cross-sectional area of the For this reason, the pressure loss when the liquid flows in the inside of the cylindrical body 22 can be reduced.

  Furthermore, in the gas-liquid mixing apparatus 20, by arranging the holding member 34 between the partitions 24 adjacent in the axial direction of the cylindrical body 22, the space between the adjacent partitions 24 can be easily held.

  Further, in the gas-liquid mixing apparatus 20, since a member capable of setting a large number of openings 24A is used as the partition member 32, when the liquid passes through the plurality of openings 24A of the partition member 32, the liquid is dispersed more finely Can be

  Furthermore, in the gas-liquid mixing device 20, since the cross-sectional average flow velocity U2 of the liquid flowing in the cylinder 22 is a low-speed flow area of less than 0.3 m / s, the gas flowing into the cylinder 22 is in the standing water. It is likely to exhibit behavior similar or similar to the floating behavior, and a gas reservoir Z is likely to be formed in the cylindrical body 22. For this reason, in the gas-liquid mixing device 20, for example, compared with the configuration in which the cross-sectional average flow velocity U2 of the liquid is 0.3 m / s or more, the gas reservoir Z is easily formed in the cylindrical body 22, and the gas and the gas efficiently. The liquids can be mixed.

  In the above embodiment, the holding member 34 is disposed between the adjacent partitions 24 (partition members 32), but the present invention is not limited to this configuration. For example, without using the holding member 34, the outer peripheral portions of the adjacent partition members 32 may be fixed (fixed) to the inner peripheral surface of the cylindrical body 22 to maintain the distance between the adjacent partition members 32. .

  Moreover, in the above-mentioned embodiment, although the flow-rate fall structure 26 is used as an example of the flow-rate fall means in this invention, this invention is not limited to this structure. For example, instead of the flow velocity reduction structure 26, a baffle plate (not shown) that obstructs the flow of fluid may be disposed between the inlet 28 and the partition 24 (the partition 24 closest to the inlet 28). By arranging the baffle plate between the inlet 28 and the partition 24 in this manner, the flow of the fluid flowing in from the inlet 28 is blocked by the baffle, and the flow velocity (the cross-sectional average flow velocity) decreases. That is, the cross-sectional average flow velocity U2 of the liquid in the cylindrical body 22 is lower than the cross-sectional average flow velocity U1 of the liquid at the inlet 28. When the baffle plate is disposed between the inlet 28 and the partition 24, the cross-sectional average flow velocity U2 of the liquid flowing in the cylinder 22 can be easily adjusted. The flow velocity reduction structure 26 and the baffle plate may be used in combination.

Furthermore, in the above-mentioned embodiment, although partitioning part 24 is constituted by one partitioning member 32, the present invention is not limited to this composition. For example, among the plurality of partition portions 24, the partition portions 24 near the inlet 28 may be configured by stacking the plurality of partition members 32. As described above, in the case where the plurality of partition members 32 are stacked to form the partition part 24 closer to the inlet 28 among the plurality of partition parts 24, the dynamic pressure of the fluid flowing into the cylinder 22 decreases at the initial inflow. The flow velocity distribution of the liquid in 22 is made uniform. Thereby, the gas reservoir Z is easily formed in the cylindrical body 22. Further, for example, all of the plurality of partition portions 24 may be configured by the plurality of partition members 32. Furthermore, for example, the number of overlapping portions of the partition portions 24 closer to the inlet 28 among the plurality of partition portions 24 may be larger than that of the other partition portions 24.
Furthermore, when one partition portion 24 is configured by a plurality of partition members 32, it is preferable to shift the positions of the openings of the partition members 32 stacked on one another in the axial direction to overlap. That is, by shifting the position of the opening of one partitioning member 32 and the position of the opening of the other partitioning member 32 stacked on the one partitioning member 32 in the axial direction of the cylindrical body 22, for example, Compared with the configuration in which the position is not shifted in the axial direction of the cylindrical body 22 (the same in the axial direction), the liquid can be dispersed and finely divided.

  Furthermore, in the above-mentioned embodiment, although the entrance part 28 and the exit part 30 are formed in the cylindrical body 22 one each, the present invention is not limited to this composition. For example, a plurality of inlets 28 and outlets 30 may be formed in the cylindrical body 22. When a plurality of inlet portions 28 and outlet portions 30 are formed in the cylindrical body 22 in this manner, for example, in the cylindrical body 22 as compared with a configuration in which one inlet portion 28 and one outlet portion 30 are formed in the cylindrical body 22. It is possible to suppress the drift of the fluid. The number of inlets 28 and the number of outlets 30 formed in the cylindrical body 22 may be changed, or the inner diameter D2 of the inlet 28 and the inner diameter D3 of the outlet 30 may be changed.

  Hereinafter, the present invention will be described in more detail by way of examples. The present invention is not limited to the following examples.

Example 1
In the gas-liquid mixing apparatus 20 (see FIG. 1) of Example 1, a PFA flat bottom jar (Samplertec Co., Ltd., 0103L) having an outer diameter of 49 mm, an inner diameter of 44 mm, a height of 120 mm, and a volume of 180 mL was used as the cylinder 22. In addition, in order to attach the 3/8 inch piping constituting the inlet 28 and the outlet 30 respectively to the bottom and the ceiling of the flat bottom jar, a Teflon (registered trademark) joint was welded. Remove the cap of this cylindrical body 22 and insert one PFA coated O-ring with an inner diameter of 37.7 mm and a wire diameter of 3.5 mm as the holding member 34 in the cylindrical body 22 (Freon Industry Co., Ltd., nominal size P-38) And a partition part 24 formed by overlapping two pieces of plain weave # 80 titanium mesh (a wire diameter of 0.1 mm and an opening of 47% if it is manufactured by φ44 mm as the partition member 32) alternately. 27 stages were stacked. That is, the numbers of O-rings and titanium meshes are 27 and 54, respectively.
After the titanium mesh and the O-ring are filled in the cylindrical body 22 and the cap is closed, the gas-liquid mixing device 20 is completed, so the manufacture of the gas-liquid mixing device 20 becomes very easy.

  The reason why expensive materials such as PFA (a type of Teflon (registered trademark)) and titanium (Ti) are used for the gas-liquid mixing device 20 of Example 1 is that it has a strong oxidizing power of 150 mg / L or more. This is to make it possible to generate concentration ozone water. In order to flow such a fluid, it is necessary to use a material excellent in ozone resistance, and it is difficult to select a material other than Teflon (registered trademark), acrylic, Ti, and glass.

  Next, the gas and the liquid mixed in the gas-liquid mixing device 20 of the first embodiment will be described. As the gas to be mixed, for example, oxygen, nitrogen, air, hydrogen, ozone and the like may be used as long as the gas is hardly soluble in liquid (large in Henry's constant). As the liquid, a liquid which does not easily dissolve gas, such as water, alcohol, an acidic solution, an alkaline solution, oil and the like may be used. When particles that may clog the mesh are present in the liquid, it is preferable to remove the particles in advance with a filter or the like.

  The size of the gas-liquid mixing device 20 according to the first embodiment is preferably determined in consideration of the flow rate of the fluid to be flowed. In the case of flowing a large flow of gas and liquid, the inner diameter D1 of the cylindrical body 22, the outer diameter of the mesh and the inner diameter of the O-ring are increased to increase the cross-sectional area of the flow path. At this time, the gas reservoir Z can be easily formed in the cylindrical body 22 by designing the flow path such that the cross-sectional average flow velocity U2 of the liquid is a low-speed flow area of less than 0.3 m / s.

  For example, the water flow rate when flowing water to the gas-liquid mixing device 20 of Example 1, the cross-sectional average flow velocity U1 of the liquid (water) in the inlet 28 and the cross-sectional average flow velocity U2 of the liquid (water) in the cylindrical body 22 The relationship with is summarized in Table 1.

  From Table 1, it can be seen that the following two main points are satisfied under any conditions of the cross-sectional average flow velocity of the liquid flowing to the gas-liquid mixing device 20 of Example 1 of 1 L / min to 12 L / min.

  1. The cross-sectional average flow velocity U2 of the liquid in the inlet portion 28 is 0.3 m / s or more under all conditions, and the gas flows in the state of bubbles in the inlet portion 28 (a gas reservoir is formed in the inlet portion 28 Not formed).

  2. The cross-sectional average flow velocity U1 of the liquid in the cylinder 22 is less than 0.3 m / s under all conditions, and the gas exhibits the floating behavior in the same manner as the bubbles in the stationary water. Thus, a gas reservoir is formed in the cylindrical body 22.

  It is preferable to set the inner diameter D1 of the cylindrical body 22 of the gas-liquid mixing device 20 and the inner diameter D2 of the inlet 28 in consideration of the above two points. In the gas-liquid mixing apparatus 20, a partial flow tends to occur when the flow rate is low. Therefore, a flow straightening part for straightening the fluid is provided in at least one of the vicinity of the inlet 28 and the outlet 30; A plurality of the respective 30 may be provided to suppress the drift. For example, when the water flow rate in Table 1 is in the range of 1 L / min to 4 L / min, the Reynolds number Re (-) in the cylindrical body 22 is 571-2284 and the flow of water is laminar, so it is likely to cause a partial flow. . In the case where the gas-liquid mixing device 20 is used under such conditions, the drifting can be suppressed by installing the straightening unit and the plurality of inlets 28 and outlets 30 as described above. On the other hand, when the water flow rate in Table 1 is in the range of 4 L / min to 12 L / min, the cross-sectional average flow velocity U1 of the liquid in the inlet 28 becomes high at 1.5 m / s to 4.5 m / s. It becomes difficult for air bubbles conveyed by influence to stay in the cylinder 22. Therefore, use means such as increasing the number of meshes and the like that configure the partition 24 in a portion near the inlet 28 or providing a baffle in the center of the mesh and the like that configure the uppermost partition 24. Thus, the cross-sectional average flow velocity of the liquid at the inlet 28 and the outlet 30 can be averaged and suppressed to less than 0.3 m / s. When the gas-liquid mixing device 20 is always used at a high flow rate, the cross-sectional average flow velocity U1 of the liquid at the inlet 28 is 0.3 <U1 by a method such as making the number of the inlets 28 plural. The dynamic pressure may be suppressed by setting it to be 1.0 m / s.

<Test Example 1>
The results of dissolving oxygen in tap water using the gas-liquid mixing device of Example 1 will be described. The flow of the test apparatus used for the test is shown in FIG. In this test, water was flushed from a tap water tap, and oxygen gas (gas) was mixed with tap water (liquid) through an oxygen flow meter (MFC: mass flow controller). A mixed fluid of tap water and oxygen gas was flowed downward from the inlet 28 at the top of the gas-liquid mixer 20 of Example 1, and was withdrawn from the outlet 30. The tap water supply line to the inlet 28 was constituted by 3/8 inch piping, and the oxygen gas supply line was constituted by 1/4 inch piping. The flow rate of tap water to flow to the gas-liquid mixing device 20 (hereinafter referred to as “water flow rate” as appropriate) is changed between 0.6 L / min and 12 L / min, and the flow rate of oxygen gas is fixed at 120 mL / min did. In the experiment, the pressure loss in the gas-liquid mixing device 20 and the dissolved oxygen concentration and undissolved oxygen amount in the outlet 30 were measured. The water flow rate was measured with a 1 L measuring cylinder, and the dissolved oxygen concentration was measured with an optical dissolved oxygen analyzer (Metler Toledo, Seven2Go pro). Also, in order to confirm the material balance of the input oxygen, the amount of undissolved oxygen was measured by the water substitution method. The water temperature was 15 ° C.

  For comparison with the gas-liquid mixing apparatus 20 of Example 1, a commercially available static mixer (Noritake Co., Ltd., Model 3 / 8- (1) -N40-174-0, number of elements 24. Hereinafter, “Comparative Example 1” as appropriate The performance is evaluated according to the flow of FIG. There are also mixers with 12 elements in the commercially available static mixer, but since the oxygen dissolution performance is lower by 30% or more compared to the mixer with 24 elements, the mixer with 24 elements with high oxygen dissolution performance (comparative example 1) (gas-liquid mixing device).

  The experimental results are shown in FIG. The horizontal axis in FIG. 4 is the water flow rate, and the vertical axis is the dissolved oxygen concentration at the outlet of the gas-liquid mixing device. Although the tap water of the raw material contains dissolved oxygen of about 9 mg / L, the vertical axis in FIG. 5 is a value including the dissolved oxygen in the tap water of the raw material originally contained. From this FIG. 5, the dissolved oxygen concentration of Example 1 and Comparative Example 1 was almost equal only when the water flow rate was 4 L / min. However, Example 1 showed a higher dissolved oxygen concentration than Comparative Example 1 at other water flow rates. In particular, in the low water region, Example 1 was able to produce oxygen water having a concentration about 50% higher than that of Comparative Example 1. For example, when tap water of 0.6 L / min was flowed to Example 1, high concentration oxygen water of 35 mg / L was obtained. Considering that the saturated solubility of oxygen in tap water at 15 ° C. is 49 mg / L, by using Example 1, by flowing oxygen gas at a flow rate of 1⁄5 of the water flow rate, the saturation concentration is approximately It became clear that 70% of oxygen could be dissolved. On the other hand, the maximum dissolved oxygen concentration of Comparative Example 1 was 25 mg / L, which was lower than that of Example 1. Moreover, even if it compares by the dissolved oxygen concentration in water flow volume = 1.2 L / min, while the example is 30.0 mg / L, the comparative example 1 is 20.9 mg / L, and the example 1 The dissolved oxygen concentration was 10 mg / L higher than that of Comparative Example 1.

  The relationship between the water flow rate and the pressure loss of Example 1 and Comparative Example 1 is shown in FIG. In Example 1, the pressure loss was larger than that of Comparative Example 1 at a water flow rate of less than 3 L / min, but the pressure loss was smaller than that of Comparative Example 1 at a water flow rate of 3 L / min or more, and a pressure of 0.1 MPa If the loss was allowed, a high flow rate of 8 L / min could be flowed. On the other hand, in Comparative Example 1, the pressure loss at high flow rate was large, and even when a pressure of 0.15 MPa was applied, only water of about 4 L / min could flow.

  Next, it was calculated from the material balance how many% of the oxygen gas supplied was dissolved in water (hereinafter, defined as oxygen solubility (%)). The results are shown in FIG. In this figure, the horizontal axis represents water flow rate, and the vertical axis represents oxygen solubility. It is understood that oxygen can be dissolved efficiently in any water flow region in comparison with comparative example 1 in the first embodiment. In particular, when 12 L / min of water and 120 mL / min of oxygen gas were allowed to flow, it was found that 57% of the oxygen introduced could be dissolved in water. This value is an oxygen solubility which can not be reached by other small mixers, and it can be seen that the oxygen gas of the raw material could be dissolved efficiently. Also, at high water flow rates of 6 L / min or more in FIG. 4, the reason why the dissolved oxygen concentration at the outlet of the trunk cylinder mixer does not decrease even if the water flow rate is increased is proportional to the water flow rate as seen in FIG. It turned out that it is because oxygen solubility goes up.

  The relationship between the Reynolds number of the tap water flowing inside of Example 1 and Comparative Example 1 and the oxygen solubility is shown in FIG. Example 1 exhibited much higher oxygen solubility than Comparative Example 1 even under the condition of low water flow rate and low Reynolds number. Further, at a water flow rate of 6 L / min or more, the Reynolds number of the embodiment is a turbulent flow of 3300 or more, and the oxygen solubility is increased by the gas-liquid stirring effect in the space portion 36 between the meshes (partition members 32). There is. If the water flow rate can be increased to 12 L / min or more by disregarding the pressure loss, it is possible to further increase the oxygen solubility.

  From the above results, in the gas-liquid mixing device 20 of Example 1, the gas is stored in the cylindrical body 22, and the liquid constituting the partition 24 is dispersed and finely divided to increase the contact area of the gas and the liquid. By promoting the mixing and stirring of the gas and the liquid in the space portion 36, it is possible to enhance the dissolution efficiency of the gas to the liquid, and furthermore, it is apparent that the pressure drop is small, which is superior to ever. became.

Test Example 2
The performance of a horizontal gas-liquid mixing device (hereinafter, described as "Comparative Example 2") imitating the gas-liquid mixing device described in Patent Document 1 (Japanese Patent Application Laid-Open No. 8-173782) was evaluated. In this test, a space of 40 mm in width (W), 100 mm in depth (D), 3 mm in height (H) is formed inside the cylindrical body of Comparative Example 2, and 15 pieces of # 100 titanium mesh of W40 mm and D100 are formed therein. installed. Further, the number of pipes in the inlet and outlet of the fluid of Comparative Example 2 is two each, and the inlet and outlet are provided with rectifying portions (spaces) of W 40 mm, D 100 mm, and H 10 mm, respectively. We suppressed the drift of fluid in the body. This comparative example 2 was installed in the apparatus of FIG. 3, the water flow rate was changed to 1 L / min to 4 L / min, the oxygen flow rate was fixed to 120 mL / min, and the dissolved oxygen concentration was measured. The dissolved oxygen concentration was measured using Comparative Example 1 for comparison. The results are shown in FIG.

  The dissolved oxygen concentration of Comparative Example 2 was lower than Comparative Example 1 under all water flow rates, and the superiority of Comparative Example 1 was remarkable. The pressure loss in Comparative Example 2 was large, and the pressure loss at a water flow rate of 4 L / min was 0.12 MPa, which was substantially the same as Comparative Example 1, and was larger than Example 1. Therefore, Comparative Example 2 has lower performance than Comparative Example 1 and Example 1. From this, it has been found that a mixer having a structure in which spaces are provided between adjacent meshes, rather than stacking the meshes closely, is better.

<Test Example 3>
The gas-liquid mixing apparatus 20 of Example 1 was incorporated into the recycling type ozone water production apparatus of FIG. 9, and was installed downstream of a water electrolysis cell that generates ozone gas having a concentration of about 10 vol. About this electrolysis method, the method as described in Japanese Patent Application No. 2016-220967 (filing date November 11, 2016) is used. The electrode area of the water electrolysis cell was 18 cm ² and a current of 27 A was passed through it to electrolyze water. The anode water tank was filled with pure water, and the amount recycled was 1.6 L / min. In addition, 0.5 M brine was recycled to the cathode at a flow rate of 0.7 L / min. The amount of water in the anode water tank was 3.0 liters. In this test, the “batch type” in which ozone water is not extracted, and the “continuous extraction type” in which ozone water is continuously extracted at 0.1 L / min and the pure water of that portion is supplied to the anode water tank High concentration ozone water was produced by the method. The results are shown in FIGS. 10 (a) and 10 (b).

  As shown in FIG. 10 (a) and FIG. 10 (b), it was possible to obtain an ultra-high concentration ozone water having a batch type of 159 mg / L and a continuous withdrawal type of 0.1 L / min of 112 mg / L. The concentration of ozone water in the case of equilibrium concentration with ozone gas having a concentration of 10 vol.% Is about 70 mg / L as calculated from Henry's law. Therefore, it has been found that when ozone water is produced batchwise using Example 1, it is possible to produce "supersaturated ozone water" having a concentration twice or more the saturation concentration.

<Test Example 4>
The gas-liquid mixing device 20 of Example 1 was incorporated into the recycling type hydrogen water producing device of FIG. 11, and was installed downstream of the water electrolysis cell to carry out recycle water electrolysis. The method described in Japanese Patent Application No. 2016-220967 is also used for this electrolysis method. The electrode area of the water electrolysis cell was 50 cm ² , and a current of 60 A was applied thereto to conduct water electrolysis. Pure water was supplied to both the anode and the cathode, and the amount of recycled water was 1.0 L / min for the anode water and 3.0 L / min for the cathode water. The amount of water in the recycling tank was 3.0 L, and high concentration hydrogen water was produced in a batch system without extracting water. The concentration of hydrogen water was measured by a dissolved hydrogen concentration meter (Koei Denshi Kenkyusho, KM2100DH, upper limit of measurement = 2.0 mg / L). The saturated hydrogen concentration at 20 ° C. and 1 atm is 1.62 mg / L. The results are shown in FIG.

  As shown in FIG. 12, saturated hydrogen water became about 18 minutes after the start of operation, and 3 L of high concentration hydrogen water having a supersaturated hydrogen concentration of 2.0 mg / L or more could be generated over 20 minutes. It is the first in the world to produce supersaturated hydrogen water using an atmospheric pressure tank. This also shows that the gas-liquid mixing device 20 of Example 1 has high performance.

  As mentioned above, although one embodiment of the present invention was described, the present invention is not limited to the above, and can be variously modified and carried out in addition to the above in the range which does not deviate from the main point. Of course. For example, the fluid may be made to flow from the lower inlet 28 to the upper outlet 30 by turning the gas-liquid mixing device 20 upside down.

  In addition, since the gas-liquid mixing apparatus in the present invention has high dissolution performance in the gas-liquid mixing operation, oxygen-enriched water or high concentration functional water (ozone water, hydrogen water, accelerated oxidized water mixed with ozone and hydrogen peroxide) It can be applied to various industrial fields, such as production of and etc. and use in a degassing system by gas purge using nitrogen, argon or the like.

Reference Signs List 20 gas-liquid mixing device 22 cylinder 24 partition 24A opening 26 flow velocity reduction structure (flow velocity reduction means)
28 inlet portion 30 outlet portion 32 partition member 34 holding member 36 space portion D1 inner diameter (inner diameter of cylinder)
D2 inner diameter (inner diameter of inlet)

Claims (9)

A cylinder having an inlet for fluid containing gas and liquid formed at one end in the axial direction and an outlet for the fluid at the other end in the axial direction;
A plurality of openings formed in the cylindrical body at intervals in the axial direction of the cylindrical body and having a plurality of openings, and partitioning the cylindrical body in the axial direction;
A flow velocity reducing means for reducing the flow velocity of the liquid flowing in the cylinder than the flow velocity of the liquid flowing in the inlet portion;
Gas-liquid mixing device equipped with   The gas-liquid mixing device according to claim 1, wherein the flow velocity reduction means is configured such that an inner diameter of the cylindrical body is larger than an inner diameter of the inlet.   The gas-liquid mixing device according to claim 1 or 2, wherein the flow velocity reduction means has a baffle plate disposed between the inlet portion and the partition portion to block the flow of the fluid.   The gas-liquid mixing device according to any one of claims 1 to 3, wherein a holding member for holding a space is disposed between the axially adjacent partition parts. The partition part is constituted by a partition member in which a plurality of openings are formed,
The gas-liquid mixing device according to any one of claims 1 to 4, wherein the plurality of partition members near the inlet portion among the plurality of partition portions are configured by stacking a plurality of the partition members.   The gas-liquid mixing device according to claim 5, wherein the axially stacked partition members are offset in the axial direction from each other in the positions of the openings.   The gas-liquid mixing device according to claim 5 or 6, wherein the partition member is a plain weave or twill weave mesh, an expanded metal, or a plate-like member in which a plurality of through holes are formed.   The gas-liquid mixing device according to any one of claims 1 to 7, wherein a plurality of the inlet portion and the outlet portion are respectively formed in the cylinder. The gas-liquid mixing device according to any one of claims 1 to 8, wherein a cross-sectional average flow velocity of the liquid flowing in the cylinder is less than 0.3 m / s.