JP7370534B2 - liquid processing equipment - Google Patents

Description

The present invention relates to a liquid treatment device for performing cavitation treatment on liquid in which gas is dissolved.

Various nozzles have been proposed in which a constriction section is provided in the water flow path using a venturi or orifice, and dissolved air is precipitated as fine bubbles by the depressurizing effect when water passes through at a high flow rate (Patent Documents 1 to 6). In particular, the systems disclosed in Patent Documents 1 and 2 are those in which a threaded member is arranged in the middle of a flow path, and the water flow is further increased in speed by the thread valley or the gap formed between the opposing threaded members. It is said that it can improve cavitation efficiency and generate microbubbles at a higher density.

Further, in the nozzles disclosed in Patent Documents 1 and 2, a remarkable turbulent agitation region is formed around the threaded member due to the collision between the threaded member and the liquid flow and the reduced pressure boiling of dissolved gas accompanying cavitation. By supplying the gas to a multiphase flow of liquid and gas, it is possible to efficiently dissolve the gas in the liquid. The gas newly dissolved in the liquid due to this dissolution can become bubbles again due to cavitation when it comes into contact with the screw member. For example, even when using water to be treated that lacks the amount of dissolved air, the amount of dissolved air can be supplemented by passing through the nozzle while supplying air in the form of a multiphase flow, making it possible to perform sufficient cavitation treatment.

WO2016-178436 publication WO2016-195116 publication JP 2018-144018 Publication

In Patent Documents 1 to 3, as a means for forming a multiphase flow to be supplied to a nozzle, gas is directly introduced into a constriction part (cavitation treatment part) in which a screw member is arranged through a gas introduction hole formed in the nozzle body. Alternatively, a method of near-liquid mixing using a tee joint or venturi ejector provided upstream of the nozzle is adopted. However, this method has the drawback that the size of the bubbles (gas phase) that come into contact with the screw member becomes too large, and the efficiency of gas dissolution into the liquid is poor. In this case, when using a liquid to be treated that is deficient in the amount of dissolved gas, even if the gas is supplemented from the outside in the form of a multiphase flow, if the dissolution of the gas is difficult to proceed, sufficient cavitation cannot be expected to occur.

An object of the present invention is to be able to perform gas dissolution treatment using a liquid treatment nozzle having a structure in which cavitation treatment is performed using a threaded member much more efficiently than before, and to solve the problem of dissolving a liquid to be treated which is deficient in dissolved gas amount. An object of the present invention is to provide a liquid treatment device that can generate sufficient cavitation even when using a liquid treatment device.

In order to solve the above problems, the liquid processing device of the present invention includes:
A single liquid flow path having a liquid inlet at one end and a liquid outlet at the other end is formed, and a part of the liquid flow path is formed between a nozzle body defined as a cavitation treatment section and a cavitation treatment section. The nozzle body is equipped with a plurality of threaded members that are attached to the nozzle body so that the tip ends of the legs protrude inside the flow path, and the liquid in which gas is dissolved flows from the liquid inlet to the liquid outlet. A liquid processing nozzle that performs cavitation treatment on the liquid based on reduced pressure precipitation of dissolved gas by bringing the liquid into contact with the thread valley formed on the outer circumferential surface of the leg while increasing the speed;
A hollow outer cylinder member having an inlet at one end and an outlet at the other end, and a spiral flow path provided inside the outer cylinder member connecting the inlet and the outlet. a flow path forming member whose helical axis is formed along the central axis of the outer cylindrical member, and provided on the liquid inlet side of the liquid processing nozzle so that the spiral flow path communicates with the liquid flow path of the liquid processing nozzle. a gas-liquid mixer,
A multiphase flow supply section that supplies a multiphase flow of gas and liquid to the inlet of the gas-liquid mixer,
The air bubbles in the multiphase flow are pulverized by flowing through the spiral flow path of the gas-liquid mixer and then supplied to the liquid processing nozzle, and the pulverized gas is drawn into the turbulent area generated in the cavitation treatment section and dissolved. It is characterized by being made to do.

In the liquid processing nozzle used in the present invention, when the liquid collides with the threaded member and detours downstream, it is throttled in the thread trough, increasing the speed and causing cavitation, so dissolved gas components of the liquid The liquid becomes supersaturated due to negative pressure, and bubbles are precipitated while the liquid is violently agitated, creating a turbulent region. At this time, by mixing the gas phase (gas) with the liquid supplied to the turbulent region to form a multiphase flow, the above stirring progresses gas-liquid mixing and agitation, and the gas phase components (gas components) are dissolved in the liquid. progresses. However, when the multiphase flow collides with a threaded member, if the entire inner space of the thread valley is covered with large bubbles, the contact efficiency between the liquid containing dissolved gas and the thread valley decreases, and the cavitation efficiency is significantly reduced. (i.e., the thread valley loses its function as an effective thread valley as a cavitation point). As a result, the formation of a turbulent region that generates the driving force for mixing and stirring gas phase components becomes less pronounced, leading to a decrease in gas dissolution efficiency. Furthermore, the effect of improving liquid permeability or cleaning performance, which is unique to cavitation treatment, may be easily impaired.

However, in the liquid processing apparatus of the present invention, a gas-liquid mixer having a spiral flow path is provided upstream of the liquid processing nozzle. As a result, the multiphase flow is passed through the spiral flow path of the gas-liquid mixer, and the centrifugal force of the forcedly generated spiral flow promotes stirring and mixing of the gas and liquid phases, so the gas phase is made up of fine bubbles. It is supplied to the threaded member of the liquid treatment nozzle in a pulverized state. As a result, the contact efficiency between the gas-containing liquid and the thread valley can be increased, and the gas dissolution efficiency can be increased.

The gas-liquid mixer is desirably configured to finely pulverize bubbles to a bubble diameter of 1.5 h or less, with the thread pitch of the screw member being h (mm). If the diameter of the bubbles obtained by pulverization in the gas-liquid mixer exceeds 1.5 hours, the effect of improving gas dissolution efficiency may not be significant. The bubble diameter is more preferably 1.0 h or less. Further, there is no limit to the lower limit of the bubble diameter, but in the case of mixing and stirring using a gas-liquid mixer having a spiral flow path, about 0.2 hours may be the limit for pulverization.

The flow path forming member of the gas-liquid mixer can be configured as a twisted plate member obtained by twisting a band-shaped metal plate so that the central axis in the width direction of the metal plate is the helical axis. By using such a twisted plate member, the spiral flow path of the gas-liquid mixer can be easily and inexpensively formed. Further, by using the twisted plate member, the spiral flow path is formed by a first spiral flow path formed by a space between the first main surface of the twisted plate member and the cylindrical inner peripheral surface of the outer cylinder member, It can be configured to include a second spiral flow path formed by a space between the second main surface of the torsion plate member and the cylindrical inner circumferential surface of the outer cylinder member. Thereby, two systems of spiral flows having different rotational phases can be formed on both sides of the torsion plate member, and the gas phase crushing efficiency can be further improved with a simple structure.

It is preferable that the total length of the outer cylinder member is determined so that the spiral flow path includes a spiral section of one period or more. If the spiral section included in the spiral flow path is less than one period, the gas phase pulverization efficiency of the gas-liquid mixer may decrease, and the gas dissolution efficiency in the downstream liquid processing nozzle may become insufficient. More preferably, the total length of the outer cylindrical member is determined such that the helical flow path includes a helical section of 1.5 cycles or more, more preferably 2 cycles or more.

Further, the value of λ/Dx is set to 1.5 or more and 4 or less, where the inner diameter of the cylindrical inner peripheral surface of the outer cylinder member is Dx (mm), and the helical period length of the torsion plate member is λ (mm). It's good to be there. If the value of λ/Dx exceeds 4, the total length of the outer cylindrical member becomes too large, causing a problem when securing the number of cycles of the spiral flow path necessary to ensure the gas phase pulverization efficiency of the gas-liquid mixer. There are cases. In addition, if the value of λ/Dx is less than 1.5, the flow resistance of the spiral flow path formed by the twisted plate member becomes too large, the gas phase crushing efficiency of the gas-liquid mixer decreases, and the downstream side Gas dissolution efficiency in the processing nozzle may be insufficient.

The threaded member used in the liquid treatment nozzle may have a thread pitch and thread depth of 0.20 mm or more and 0.40 mm or less, and a nominal thread diameter M of 1.0 mm or more and 2.0 mm or less. In this case, a plurality of virtual screw placement planes perpendicular to the central axis of the liquid flow path can be set in the cavitation treatment section along the central axis, and the above-mentioned screw members are attached to each screw placement surface. Two or more legs can be distributed such that the longitudinal direction of the legs is along the screw placement surface. On this premise, the liquid treatment nozzle can be further configured as follows.
・A total of 8 or more screw members are arranged in such a way that two or more screw members are distributed to each screw arrangement surface (hereinafter, a group of screw members arranged on one screw arrangement surface is referred to as a "plane screw group"). ).
・In each screw arrangement surface, the in-plane flow area ratio defined as the ratio of the liquid flow area to the total cross-sectional area of the liquid flow path is ensured to be 40% or more, and the area of the liquid flow area of the liquid flow path is 3.8 mm. ² or more is secured.
・The total number of trough points located within 70% of the radius of the liquid flow path from the cross-sectional center of the liquid flow path when projected onto a plane perpendicular to the central axis is calculated as When defined as the 70% valley point areal density divided by the cross-sectional area of the road, the value of the 70% valley point areal density is ensured to be 2.0 pieces/mm ² or more.
- The distance between adjacent screw placement surfaces in the central axis direction is ensured to be greater than or equal to the nominal screw diameter.

A liquid processing nozzle equipped with these features can dramatically improve the 70% trough point density while ensuring a sufficient liquid flow rate at the normal tap water pressure, and in particular, it has significantly expanded the cross-sectional area of the flow path. Even in a large flow rate nozzle, a sufficient 70% valley point density can be ensured with a simple structure. By circulating the gas-liquid mixer unique to the present invention as a pre-treatment, the bubble diameter of the multiphase flow supplied to the liquid processing nozzle can be reduced, and even when using a multiphase flow with a high gas phase content, it is possible to reduce the bubble diameter by 70%. Even though the points are highly dense, they can effectively function as cavitation points, and gas dissolution efficiency can be greatly increased even in a high-flow nozzle.

The liquid processing nozzle having the above configuration will be described in more detail below.
The reason why it is preferable to set the numerical ranges of the thread pitch and thread depth of the threaded member as described above is as follows. First, when the thread valley depth is less than 0.2 mm, the cavitation effect (bubble precipitation effect due to reduced pressure of dissolved gas) in the thread valley becomes less noticeable, and when the thread valley depth is 0.40 mm or more, the improvement in the cavitation effect reaches a plateau. Become. Furthermore, if the thread pitch increases to 0.40 mm or more, the number of thread troughs per unit length of the screw leg portion decreases, making it impossible to improve the areal density at the 70% trough point. Therefore, the thread pitch and thread depth are preferably set to 0.20 mm or more and 0.40 mm or less. In addition, from the viewpoints of ensuring the strength of the threaded member, preventing the cross section of the flow path from being excessively occupied by the threaded member, and ensuring sufficient liquid flow rate even at normal liquid delivery pressures such as water pressure, The nominal thread diameter of the member is preferably set to 1.0 mm or more and 2.0 mm or less. The value range of this nominal thread diameter almost matches the range of the nominal thread diameter of the JIS coarse pitch screw, which covers the above thread pitch and thread root depth. It is preferable that eight or more screw members are disposed in the liquid flow path in total. By dividing these 8 or more screw members into multiple (2 or more) surface screw sets and distributing them over multiple screw placement surfaces instead of arranging them densely on one screw placement surface, 70% It is possible to increase the valley point density.

If the in-plane flow area ratio becomes too small on each screw arrangement surface, the contact area between the water flow and the screw member becomes excessive, and the flow rate decreases significantly due to pressure loss. As a result, the area where a sufficient flow rate can be obtained when liquid flows under normal water pressure becomes smaller than the 70% radius from the center of the cross section, and it may not be possible to secure a sufficient number of valley points that effectively function as cavitation points. . Further, even if the in-plane flow area ratio is large to some extent, if the absolute value of the area of the liquid flow region becomes too small due to a reduction in the cross-sectional inner diameter of the flow path, the flow rate may similarly decrease significantly. As a result of careful consideration in view of this situation, we found that if the in-plane flow area ratio is secured at 40% or more on each screw placement surface, and the area of the liquid flow area is secured at 3.8 mm2 ^or more, the above It has been found that such problems are eliminated and the pressure drop when the liquid flow passes through the individual screw placement surfaces is significantly reduced. By ensuring that the distance between adjacent screw arrangement surfaces (plane thread sets) is greater than or equal to the nominal thread diameter of the screw member used, multiple plane thread sets that satisfy the above conditions can be installed in the direction of the center axis of the flow path. Even if they are arranged in series, the increase in pressure loss can be kept extremely small compared to when the face thread assembly is arranged alone, and more thread members are arranged in one liquid flow path than before. Despite this, the required flow velocity within the cross section can be ensured sufficiently. As a result, when the value of the area density at the 70% valley point was set to 1.6 particles/mm2 ^or higher, which was previously impossible to achieve, a sufficient flow velocity was secured at the thread valley forming the 70% valley point, and cavitation was prevented. A liquid processing nozzle with extremely high efficiency can be realized.

If the in-plane flow area ratio is less than 40% on each screw placement surface, or if the area of the liquid circulation area is less than 3.8 ^mm2 , the pressure loss of each surface screw set placed on the screw placement surface will be This increases and makes it impossible to secure a sufficient flow velocity at the thread valley, which is the 70% valley point. Furthermore, if the interval between two adjacent screw arrangement surfaces (plane thread set) becomes smaller than the nominal thread diameter of the threaded member used, the combined pressure loss of those two plane thread sets becomes large, and similarly, the 70% trough point This leads to the inability to secure a sufficient flow velocity at the thread valley that forms the

In the liquid processing nozzle described above, it is preferable that the area of the liquid flow area of the liquid flow path is more preferably 5.0 mm ² or more on each screw arrangement surface. The present inventor created liquid processing nozzles in which the area of the liquid circulation area was varied in various ways while ensuring an in-plane circulation area ratio of 40% or more, and as a result of conducting a water flow test at normal water pressure, the inventor found that the liquid circulation area In areas where the area is 5.0 mm2 ^or more, the flow rate tends to increase almost linearly as the area increases, whereas in areas where the area is less than 5.0 ^mm2 , the flow rate shows a linear relationship. It was found that the curve deviates downward from the curve and rapidly decreases depending on the logarithm of the area of the liquid flow region. This means that under normal water pressure flow conditions, when the area of the liquid flow area is less than 5.0 ^mm2 , the increase in pressure drop increases each time the number of surface screw sets inserted in the nozzle increases. This means that the flow rate increases rapidly, making it impossible to obtain a flow rate commensurate with the cross-sectional area. Therefore, in order to increase the number of surface threads and further increase the value of the 70% valley point areal density, it is extremely important to ensure the area of the liquid circulation region to be 5.0 mm ² or more. In this case, it is possible to ensure that the value of the 70% valley point area density is 2.0 pieces/mm ² (approximately twice the maximum value (1.1 pieces/mm ² ) disclosed in Patent Document 2) or more. Become.

It is desirable that the screw members be arranged on the screw arrangement surface in such a positional relationship that the longitudinal direction of the legs coincides with the diameter of the circular axial cross section of the liquid flow path. By matching the longitudinal direction of the leg with the diameter of the circular axial cross section of the liquid flow path, the tip of the threaded member approaches the center of the cross section of the liquid flow path where the flow velocity increases, so it is possible to increase the number of trough points by 70%. Works in your favor. In this case, by setting two or more screw placement surfaces containing three or more screw members in the central axis direction, the value of the 70% valley point area density of the entire nozzle can be significantly improved, and the cavitation generation efficiency can be significantly increased. be able to. In addition, three or more screw members on the screw arrangement surface can be arranged so that the end surfaces of the legs of each screw surround the center of the cross section to form a center gap. The flow (center flow) is less likely to be obstructed by the formation of the liquid flow gap, and cavitation generation efficiency can be further improved.

It is desirable that the leg portions of the screw member be placed between mutually adjacent screw placement surfaces in a positional relationship in which they overlap each other while making the longitudinal directions coincide when projected onto a plane. According to this configuration, it is possible to create a liquid treatment nozzle that has a particularly low pressure loss even though contact with a large number of threaded members is allowed, and a liquid treatment nozzle that has a low pressure loss while dramatically increasing the number of 70% valley points. It can be realized. In the liquid processing nozzle of this configuration, even if the distance between adjacent screw arrangement surfaces (plane thread set) approaches a limit value equal to the nominal thread diameter of the threaded member, an increase in pressure loss is unlikely to occur, and as a result, the flow path center axis The arrangement interval of the screw members in the direction can be made more dense, and there is an advantage that a liquid treatment nozzle with excellent cavitation generation efficiency can be configured compactly. This effect is particularly remarkable when the distance between adjacent screw arrangement surfaces (plane thread set) is kept at twice the nominal screw diameter or less. Additionally, when using a screw member with a head with a larger diameter than the leg, the interval between the screw placement surfaces (plane screw set) must be set larger than the outer diameter of the head. .

For example, a configuration is adopted in which the same number of three or more screw members are arranged on each of the adjacent screw arrangement surfaces at equal angular intervals around the center of the cross section so that the legs follow the cross-sectional radial direction of the liquid flow path. In this case, it is preferable to set the arrangement angle phase of the screw member around the center of the cross section to be the same between adjacent screw arrangement surfaces. In this way, adjacent screw members in the same screw arrangement plane are connected in the axial direction like a wall, and the flow path cross section is partitioned by the wall-like screw row, and within the partitioned area. Since no other screw member is interposed in the screw, the liquid collision resistance is greatly reduced even though a large number of screws are arranged. Further, on the inner surface of the wall-like screw row, a large number of thread valleys of the individual screw members are densely arranged, and the cavitation efficiency can be dramatically increased.

On the other hand, the leg portions of the screw member between adjacent screw placement surfaces can also be placed in a positional relationship such that their longitudinal directions intersect with each other when projected onto a plane. In this configuration, when the liquid flow passes through the multiple surface screw sets, the loss due to the collision between the individual screw members and the liquid flow is slightly larger, but the effect of stirring the liquid by the turbulence generated by the collision is more pronounced. becomes. For example, a liquid processing nozzle with the above configuration may also be used for gases (one or more selected from air, oxygen, carbon dioxide, nitrogen, hydrogen, ozone, etc.) and liquids (water, edible oil, gasoline, light oil, etc.). By supplying a mixed flow of gas (fossil fuel, alcohol, etc.), the efficiency of dissolving gas in liquid can be increased due to the above-mentioned stirring effect. Furthermore, it can be effectively employed for the purpose of forming an emulsion by stirring and mixing liquids with low mutual solubility (for example, an organic liquid and an aqueous liquid with low hydrophilicity).

In the above configuration, it is preferable that the interval between the screw arrangement surfaces in the central axis direction be set to 2.0 times or more the nominal screw diameter of the screw member. Thereby, it is possible to reduce pressure loss when flowing liquid through the plurality of face screw sets. The interval between the screw arrangement surfaces is more preferably set to 4.0 times or more. For example, if the same number of screw members (three or more) are arranged on each of the adjacent screw arrangement surfaces at equal angular intervals around the center of the cross section so that the legs follow the cross-sectional radial direction of the liquid flow path, the above-mentioned In order to employ this configuration, the arrangement angular phase of the screw members around the center of the cross section is determined in such a manner that adjacent screw arrangement surfaces are shifted from each other.

The details of the operation and effects of the present invention have already been described in the "Means for Solving the Problems" section, so they will not be repeated here.

FIG. 1 is a conceptual diagram showing an example of a liquid treatment device of the present invention together with a usage pattern. 1A is a cross-sectional view and a side view showing an example of a gas-liquid mixer used in the liquid processing device of FIG. 1A. FIG. FIG. 1B is a cross-sectional view showing an example of a liquid treatment nozzle used in the liquid treatment apparatus of FIG. 1A. FIG. 1C is an axial cross-sectional view showing the screw member layout on each screw arrangement surface of the liquid treatment nozzle of FIG. 1C. FIG. 3 is an axial sectional view showing an enlarged main part of FIG. 2; FIG. 1C is a cross-sectional view of a main part of the liquid treatment nozzle in FIG. 1C, in which four sets of plane threads having the layout in FIG. 2 are arranged in the central axis direction. FIG. 7 is a cross-sectional view of the main parts of eight liquid treatment nozzles arranged in the same manner. FIG. 1C is a cross-sectional view of a main part of the liquid treatment nozzle of FIG. 1C, showing a structure in which one surface screw set is rotated by 45 degrees. FIG. 7 is a cross-sectional view of a main part of the liquid processing nozzle shown in FIG. 1C, in which one surface screw set has the layout shown in FIG. 6; FIG. 8 is a cross-sectional view of a main part of the liquid processing nozzle in which the surface screw set is divided into mutually orthogonal screw member pairs, and the respective positions are shifted in the central axis direction in the structure of FIG. 7 . FIG. 8 is a cross-sectional view of a main part of a liquid treatment nozzle in which two pairs of surface screw sets similar to the liquid treatment nozzle of FIG. 7 are arranged in the central axis direction. FIG. 2 is a cross-sectional view showing a venturi ejector connected to the gas-liquid mixer of the liquid processing apparatus shown in FIG. 1; FIG. 2 is an axial cross-sectional view of a main part of a liquid processing nozzle in which a surface screw set is composed of three screw members. FIG. 2 is an axial sectional view of a main part of a liquid processing nozzle in which a surface screw set is composed of eight screw members. FIG. 2 is an axial sectional view of a main part of a liquid processing nozzle in which a surface screw set is configured by four screw members without forming a center gap. FIG. 14 is a cross-sectional view of a main part of a liquid processing nozzle in which two sets of plane threads shown in FIG. 13 are arranged in the central axis direction. 2 is a graph showing the relationship between the area of the liquid flow area and the flow rate when water is caused to flow under a constant dynamic water pressure in a liquid treatment nozzle in which four screw members are arranged in a cross shape. A graph showing a comparison of the cross-sectional flow velocity distribution of a liquid processing nozzle in which four threaded members are arranged in a cross shape between a nozzle with a cross-sectional inner diameter of 4.2 mm or more and a nozzle with a cross-sectional inner diameter of 3.5 mm. 2 is a graph showing the relationship between water flow dynamic pressure and flow rate of various liquid processing nozzles in which a plurality of liquid processing nozzles are arranged by alternately rotating the surface screw set by 45 degrees, together with the results for the liquid processing nozzle of a comparative example. The relationship between water flow dynamic pressure and flow rate of various liquid processing nozzles in which a plurality of face screw sets are arranged in a mutually overlapping phase relationship, together with the results for liquid processing nozzles in which two sets of face thread sets are arranged with the face thread sets rotated by 45 degrees from each other. Graph showing. The figure which shows the structure of the apparatus which evaluates the slime dirt removal ability of treated water. FIG. 3 is an axial sectional view of a main part of a liquid treatment nozzle of a comparative example. The figure explaining the dimensional relationship of each part of the liquid processing nozzle used in the experimental example. Schematic diagram of the test equipment used for the water flow test.

Embodiments of the present invention will be described below with reference to the accompanying drawings.
FIG. 1A is a conceptual diagram showing an example of a liquid treatment device according to an embodiment of the present invention together with a usage pattern. The liquid processing device 300 has a liquid processing nozzle 1, a gas-liquid mixer 150, and a multiphase flow supply section 165 arranged in series communication in this order from the downstream side in the liquid distribution direction (arrow), and includes a liquid storage section 250 ( It is provided on a circulation pipe 180 that circulates liquid stored in a tank, storage tank, pond, etc.). The liquid to be treated is, for example, water (or an aqueous solution in which desired solute components are dissolved as necessary), but liquids other than water (for example, organic solvents such as alcohol, fossil fuels such as gasoline or diesel oil, (edible oil, etc.) may also be used.

A pump 175 is provided on the circulation pipe 180 , and when the pump 175 operates, the liquid in the liquid storage section 250 flows into the circulation pipe 180 and is supplied to the multiphase flow supply section 165 of the liquid processing device 300 . Gas is mixed into the liquid W from the gas supply source 170 via the gas supply pipe 171 in the multiphase flow supply section 165, and the gas introduced by the gas-liquid mixer 150 is finely pulverized and sent to the liquid processing nozzle 1. At least a portion of the gas is dissolved and returned to the liquid reservoir 250. The type of gas is air in this embodiment (the gas supply source 170 is an air compressor), but other gases such as oxygen, nitrogen, carbon dioxide, hydrogen gas, and ozone may also be used. A mixed gas of two or more selected types may be used.

FIG. 1B shows an example of a gas-liquid mixer 150 used in the liquid processing apparatus shown in FIG. 1A. The gas-liquid mixer 150 includes an outer cylinder member 151 and a flow path forming member 155. The outer cylinder member 151 is formed into a hollow cylindrical shape with an inlet 159 formed at one end and an outlet 160 formed at the other end. The material is, for example, metal or plastic such as polyvinyl chloride, and in this embodiment stainless steel is used. At both ends of the outer cylindrical member 151, a joint portion for connecting to another piping element, and in this embodiment, a male thread portion 152 is formed.

On the other hand, the flow path forming member 155 is provided inside the outer cylinder member 151, and the spiral flow paths 157 and 158 connecting the inlet 159 and the outlet 160 are formed so that the helical axis HC of the helical flow paths 157 and 158 It is formed along the central axis of the outer cylinder member 151. In this embodiment, the flow path forming member 155 is a twisted plate member (hereinafter also referred to as the twisted plate member 155) obtained by twisting a band-shaped metal plate so that the central axis O in the width direction is the helical axis HC. It can be configured as In this embodiment, the material of the flow path forming member 155 is stainless steel.

Inside the outer cylindrical member 151, the torsion plate member 155 has a first helical flow path 157 between the first main surface of the torsion plate member 155 and the inner circumferential surface of the outer cylindrical member 151, and a second helical flow path 157 between the first main surface of the torsion plate member 155 and the inner peripheral surface of the outer cylindrical member 151. A second spiral flow path 158 is formed between the main surface and the inner peripheral surface of the outer cylinder member 151. The total length of the outer cylindrical member 151 is determined so that the helical flow path includes a helical section 156 of one period or more, and in this embodiment, two periods. Further, the value of λ/Dx is set to 1.5 or more and 4 or less, where the inner diameter of the cylindrical inner peripheral surface of the outer cylinder member 151 is Dx (mm), and the helical period length of the torsion plate member 155 is λ (mm). has been done. Dx is, for example, 5 mm or more and 30 mm or less (for example, 15 mm), and the value of λ is, for example, 20 mm or more and 300 mm or less (for example, 50 mm). Further, the thickness of the plate material constituting the torsion plate member 155 is selected within a range not exceeding 1/4 of Dx, for example, in a range of 0.3 mm or more and 4 mm or less (for example, 1 mm).

FIG. 1C is a cross-sectional view showing an example of the liquid treatment nozzle 1. This liquid processing nozzle 1 includes a nozzle body 2 in which a liquid flow path 3 is formed. The nozzle body 2 is formed into a cylindrical shape, and one liquid flow path 3 having a circular cross section is formed through the nozzle body 2 in the direction of the central axis O thereof. The liquid flow path 3 has a liquid inlet 4 at one end (on the right side of the drawing) and a liquid outlet 5 at the other end, and at an intermediate position in the flow direction there is a liquid inlet 4 with a diameter smaller than that of the liquid inlet 4 and the liquid outlet 5. A constriction portion 9 is formed to form a partial section of the liquid flow path 3. In the liquid flow path 3, the side closer to the liquid inlet 4 than the constriction part 9 is an inflow chamber 6, and the side closer to the liquid outlet 5 is an outflow chamber 7. A screw member 10 is attached to the constriction part 9 so that the tip side of the leg protrudes inside the flow path, thereby forming a cavitation treatment part CV.

The material of the nozzle body 2 is, for example, a resin such as ABS, nylon, polycarbonate, polyacetal, or PTFE, but may also be a metal such as stainless steel or brass, or a ceramic such as alumina, and is appropriately selected depending on the application. Further, the material of the screw member 10 is, for example, stainless steel, but depending on the application, a heat-resistant alloy such as titanium, Hastelloy, or Inconel (all trademarks) with higher corrosion resistance may be used, or a material with higher wear resistance may be used. If this poses a problem, it is also possible to use ceramic materials such as quartz or alumina. In particular, quartz is suitable for application to fields where metal contamination is averse (for example, the semiconductor field), and in this case, the resin nozzle body 2 is preferably made of, for example, PTFE.

The threaded member 10 used has a thread pitch and thread root depth of 0.20 mm or more and 0.40 mm or less, and a nominal thread diameter M of 1.0 mm or more and 2.0 mm or less. In this embodiment, the screw member 10 is a No. 0 class 1 pan head machine screw defined by JIS. In the cavitation treatment section CV, a plurality of virtual screw arrangement surfaces perpendicular to the central axis O of the liquid flow path 3 are set along the central axis O, two surfaces LP1 and LP2 in FIG. 1C. The screw member 10 described above is arranged so that the longitudinal direction of the leg portions is along the respective screw arrangement surfaces LP1 and LP2. In the embodiment of FIG. 1C, the total number of screw members 10 is eight (as described later, the number may exceed eight), and there are two or more screw members 10 for each screw placement surface LP1, LP2, and four in FIG. 1C. are distributed one by one.

In FIG. 1C, the screw members 10 are arranged on each screw arrangement surface LP1, LP2 according to the layout shown in FIG. 2. Specifically, the four screw members 10 on each of the screw placement surfaces LP1 and LP2 are arranged in a cross shape orthogonal to each other, and each has a female threaded portion 19f on the inner surface of the screw hole 19 formed in the nozzle body 2. The legs are screwed so that the tips of the legs protrude into the constricted portion 9 from the outer peripheral surface of the wall. The screw hole 19 and the screw member 10 can be set and fixed using an adhesive or the like. FIG. 3 shows a further enlarged view of the inside of the constricted portion 9, and a main circulation region 21 is formed between the screw member 10 and the inner circumferential surface of the constricted portion 9. Further, in each constriction section 9, a liquid circulation gap 15 is formed at the center position of the cross formed by the four collision sections 10. The end surfaces of the four collision parts 10 forming the liquid circulation gap 15 (FIG. 3) are formed flat, and the liquid circulation gap 15 is formed in a square shape in the projection described above.

In FIG. 3, the area of the liquid flow area (hereinafter also referred to as the total flow cross-sectional area) a on each of the screw arrangement surfaces LP1 and LP2 is defined as the total area inside the outer periphery of the projected area of the liquid flow path (herein, the area in FIG. 1C The area of the circular shaft cross section of the throttle part 9: where the inner diameter is d, πd ² /4)) is S1, and the projected area area of the collision part 10 (four screw members) is S2,
a=S1-S2 (unit: mm ² )
Define as . In this embodiment, the total area of the main flow area 21 and the liquid flow gap 15 corresponds to the total flow cross-sectional area a. As shown in FIG. 1C, the opening diameters of the liquid inlet 4 and the liquid outlet 5 are larger than the inner diameter of the constriction part 9. That is, the opening cross-sectional area of the liquid inlet 4 and the liquid outlet 5 is set larger than the total flow cross-sectional area a. Further, the inner circumferential surfaces of the inflow chamber 6 and the outflow chamber 7 that are connected to the constricted portion 9 are tapered portions 13 and 14, respectively. The tapered portion 14 on the liquid outlet 5 side and the tapered portion 13 on the liquid inlet 4 side have the same aperture ratio, but the section length of the tapered portion 14 is set larger. In each screw arrangement surface LP1, LP2, a total flow cross-sectional area a of 3.8 mm2 ^or more is ensured, and the ratio of the liquid flow area to the total cross-sectional area S1 of the liquid flow path (i.e., a/S1×100(% )) The in-plane distribution area ratio defined as 40% or more is ensured.

In FIG. 3, the depth h of the valley portion 21 appearing on the projected outline of the screw member (collision portion) 10 is ensured to be 0.2 mm or more. In addition, when a circle drawn with a radius corresponding to 70% of the distance to the inner peripheral edge of the liquid flow path is defined as the reference circle C ₇₀ with the projected point of the central axis O as the center, the bottom position of the trough 21 is Among the valley points represented, the number of valley points located inside the reference circle C ₇₀ (indicated by ○), that is, the number of valley points located inside the reference circle C 70, that is, the number of valley points located from the cross-sectional center of the liquid channel 3 to the center of the liquid channel 3 when projected onto a plane orthogonal to the central axis O. The number of valley points located in an area within 70% of the radius of 3 is defined as the number of 70% valley points _N70 . Then, the value obtained by dividing the sum of the values of the 70% valley point number _N70 for all the screw arrangement surfaces by the cross-sectional area S1 of the liquid flow path 3 (throttled portion 9) is defined as the 70% valley point area density. In the liquid treatment nozzle 1 of FIG. 1C, the value of the 70% valley point area density is ensured to be 1.6 nozzles/mm ² or more.

In FIG. 1C, the legs of the screw member 10 are arranged between mutually adjacent screw placement surfaces LP1 and LP2 in a positional relationship in which they overlap each other while making their longitudinal directions coincide when projected onto a plane orthogonal to the central axis O. There is. Specifically, a plane screw assembly consisting of four screw members 10 arranged in a cross shape overlaps each other between the screw arrangement surfaces LP1 and LP2 (i.e., a central axis O of the cross-shaped plane screw assembly). They are arranged in a positional relationship in which the surrounding arrangement angle phases match each other (hereinafter, such an arrangement will be referred to as "in-phase arrangement"). Further, the distance dp between the adjacent screw arrangement surfaces LP1 and LP2 is set to, for example, 1.05dh or more and 2M or less, where dh is the outer diameter of the screw head 10h in FIG. 2, and M is the nominal thread diameter of the screw leg 10f. has been done.

In the liquid processing nozzle 1 of FIG. 1C, for example, the liquid outlet 5 side is opened and water, for example, is passed through the liquid inlet 4 so that the dynamic pressure is about the normal water pressure (for example, 0.077 MPa). We will explain the effect when It is assumed that air is dissolved in this water (for example, the oxygen concentration at 20° C. (normal temperature) is about 8 ppm). The water flow is first constricted by the tapered part 13 and the constricted part 9, and then flows into a liquid circulation area formed between the screw member 10 and the inner peripheral surface of the constricted part 9, which is formed by the main circulation area 21 and the liquid circulation gap 15 in FIG. It passes through the threaded member 10 while colliding with it.

When passing through the outer circumferential surface of the threaded member 10, a high speed region is formed at the thread root and a low speed region is formed at the thread crest. Then, the high-speed region of the thread root becomes a negative pressure region according to Bernoulli's theorem, and cavitation occurs. Since the thread trough is formed with multiple turns around the outer periphery of the threaded member, and eight or more threaded members 10 are distributed over the plurality of screw placement surfaces LP1 and LP2, cavitation occurs in the trough in the constricted portion 9. This will occur multiple times at the same time. Then, when the water flow collides with the threaded member 10, dissolved air is violently precipitated under reduced pressure at the thread root, causing violent friction between the water flow and the surface of the threaded member 10 and the inner surface of the liquid flow path 3. Stir while stirring.

The liquid treatment nozzle 1 in FIG. 1C has an in-plane flow area ratio of 40% or more on each screw arrangement surface LP1, LP2, a total flow cross-sectional area of 3.8 mm ² or more, and an adjacent screw The interval dp between the arrangement surfaces LP1 and LP2 (plane screw set) is ensured to be larger than the nominal thread diameter of the screw member 10 used. As a result, even if a plurality of surface screw sets are arranged in series in the direction of the flow path center axis O, the increase in pressure loss of the nozzle can be kept extremely small. As a result, even though more screw members are arranged in one liquid flow path 3 than in the past, a sufficient flow velocity can be ensured within the cross section. For example, in Patent Document 2, the value of the 70% trough area density, which was thought to be about 1.1 pieces/ ^mm2 , has been increased to 1.6 pieces/ ^mm2 or more while ensuring a sufficient flow velocity. You can set it to a large value.

The present inventor has disclosed in Patent Document 2 that water subjected to cavitation treatment using the liquid treatment nozzle disclosed in the document has improved permeability into skin, hair, etc., and that the permeability improvement effect is due to liquid treatment. It was suggested that the larger the 70% trough point density of the nozzle, the more pronounced this becomes. Furthermore, the constituent components of skin and hair are proteins, which are macromolecules, and the improvement of water permeability at the molecular level into structures made of polymer networks is due to the presence of microbubbles in the water. There are aspects that cannot be explained by effects alone, such as the physical properties of water, especially the involvement of microbubbles in the collective (statistical) behavior of water, which is a polar molecule, and the penetrating power of water. He also mentioned that the number may be increasing. However, how the characteristics of the liquid after treatment are improved when cavitation treatment is performed using a nozzle in which the value of the 70% valley point area density has expanded to the above-mentioned large value is disclosed in Patent Document 2. is silent. On the other hand, Patent Document 3 discloses a system nozzle in which a nozzle casing accommodates eight core members in which only one threaded member is incorporated in a flow path with a circular cross section, but eight threaded members are stacked in a nozzle casing. Because of the configuration in which the cavitation treatment section is arranged one by one in a dispersed manner, the length of the flow path constituting the cavitation treatment section becomes too large, resulting in a problem that pressure loss is likely to occur.

Water subjected to cavitation treatment using the nozzles disclosed in Patent Documents 1 to 3 is water containing a large amount of microbubbles in the nano-range with an average diameter of about 100 nm to 300 nm, for example, when measured using a laser diffraction particle size meter. You can confirm that it is. However, as is clear from the experimental results described below, most of the microbubbles with the above average diameter that can be confirmed by a laser diffraction particle size analyzer disappear if they are stored in a tank etc. after cavitation treatment and left for a few minutes, and the sensitivity is normal. It becomes undetectable with a laser diffraction particle size analyzer. However, even in treated water after storage in which microbubbles are no longer detected, if a liquid treatment nozzle with a further increased 70% valley point area density as described above is used, it is possible to improve permeability due to cavitation treatment. The effect is achieved in the same way.

As shown in FIG. 10, in the liquid processing apparatus 300, the gas-liquid mixer 150 is installed on the liquid inlet side of the liquid processing nozzle 1 so that the spiral channels 157 and 158 communicate with the liquid channel 3 of the liquid processing nozzle 1. It is located. Specifically, the male threaded portion 152 on the outlet side of the outer cylinder member 151 is screwed into the female threaded portion 16 of the nozzle body 2 . A separate piping element (not shown) such as a relay pipe may be interposed between the gas-liquid mixer 150 and the liquid processing nozzle 1, but secondary air bubbles BS may be present while flowing through the separate piping element. There is also a concern that the gas-liquid mixer 150 and the liquid processing nozzle 1 are connected directly as shown in FIG. 10, as there is a concern that they may coalesce and become coarse.

Further, the multiphase flow supply unit 165 supplies a multiphase flow of gas and liquid to the inlet 159 of the gas-liquid mixer 150 . In this embodiment, the multiphase flow supply section 165 is configured as a venturi ejector, and gas is supplied from a gas supply pipe 171 (FIG. 1A) through a gas introduction joint 167 to a gas supply hole 166 communicating with the constriction section. A flow is formed. In this embodiment, the multiphase flow supply section 165 is also directly connected to the inlet 159 side of the gas-liquid mixer 150. The multiphase flow is distributed into a first spiral flow path 157 and a second spiral flow path 158, and crushes the gas phase into secondary bubbles BS while forming a first spiral flow TR1 and a second spiral flow TR2, respectively.

The primary bubbles BP in the multiphase flow are mixed with the liquid and finely pulverized by centrifugal force by flowing through the spiral channels 157 and 158 of the gas-liquid mixer 150, and are mixed with the liquid and finely pulverized by the threaded member 10 of the liquid processing nozzle 1 in FIG. 1C. The secondary cells BS are pulverized into secondary cells BS having a cell diameter of 1.5h or less (preferably 1h or less), with the screw pitch of h (mm). The liquid containing the secondary bubbles BS is supplied to the liquid treatment nozzle 1, and is dissolved by being caught in the turbulent region generated in the cavitation treatment section CV.

By supplying the gas phase in the multiphase flow to the screw member of the liquid treatment nozzle 1 in a state in which it is crushed into finer secondary bubbles BS, the contact efficiency between the gas-containing liquid and the screw root increases. As a result, the formation of a turbulent region that generates a driving force for mixing and stirring the gas phase components becomes significant, and the gas dissolution efficiency can be improved. Further, in the cavitation treatment section CV, a portion of the dissolved gas is immediately reprecipitated by cavitation, so that the cavitation efficiency within the thread root portion is significantly improved. Therefore, the effect of improving the permeability or detergency of the obtained liquid is also less likely to be impaired.

Hereinafter, various modifications of the liquid treatment nozzle that can be employed in the present invention will be described.
FIG. 4 shows a configuration in which the cavitation treatment section CV of the liquid treatment nozzle 1 of FIG. 1C has four sets of surface threads arranged in the direction of the central axis O in the layout shown in FIG. Specifically, the four screw arrangement surfaces LP1 to LP4 are arranged in the direction of the central axis O with the same surface spacing dp as in FIG. 1C, so that the cross-shaped surface screw sets in FIG. in phase). In this case, the 16 screw members 10 will be distributed to the four screw placement surfaces LP1 to LP4. Further, FIG. 5 shows an example of a cavitation treatment section CV in which the surface screw set of FIG. 2 is arranged in the same phase with respect to eight screw arrangement surfaces LP1 to LP8. In this case, 32 screw members 10 will be distributed to eight screw placement surfaces LP1 to LP8. The 70% valley point area density of each cavitation treatment section CV can be increased twice in the configuration of FIG. 4 and four times in the configuration of FIG. 5 compared to the configuration in FIG. 2.

Next, FIG. 6 shows a state in which a face screw set similar to the liquid treatment nozzle 1 of FIG. 1C is rotated by 45 degrees. Of the two screw placement surfaces LP1 and LP2 of the liquid treatment nozzle 1 in FIG. FIG. 7 shows an example of the cavitation treatment section CV when the cavitation treatment section CV is rotated by 45 degrees around the axis O to be in the state shown in FIG. The cavitation treatment section CV with this configuration can achieve the same 70% valley point area density as the configuration in FIG. The pressure drop will be slightly larger. However, by appropriately enlarging the surface spacing dp, this pressure loss is reduced, and cavitation processing capacity approximately equivalent to that of the cavitation processing section CV having the configuration shown in FIG. 2 is exhibited. Furthermore, since the turbulent agitation effect of the liquid is greater than that of the configuration shown in FIG. 1C, this configuration is more advantageous for the purpose of dissolving gas in liquid by supplying a multiphase flow.

FIG. 8 shows an example of the cavitation treatment section CV in which the surface screw set is divided into mutually orthogonal screw member pairs, and the respective positions are shifted in the direction of the central axis O in the configuration of FIG. 7. Specifically, the four screw members 10 arranged on the screw arrangement surfaces LP1 and LP2 in FIG. 1C are replaced by two screws separated by the nominal thread diameter M of the thread members 10 in the configuration of FIG. Two wires perpendicular to each other are distributed and arranged on the arrangement planes LP1, LP1' and LP2, LP2'. That is, an example is shown in which eight screw members 10 are distributed to four screw placement surfaces LP1, LP1', LP2, and LP2'. Further, the distance between the screw placement surface LP1' and the screw placement surface LP2 is set to be larger than the nominal thread diameter M (for example, about 1.5M to 2.0M). The 70% valley point area density in this configuration is equivalent to the configuration in FIG.

In addition, FIG. 9 shows cavitation treatment in which two sets of surface screws having the layout of FIG. 2 and two sets of surface screws having the layout of FIG. 6 are arranged alternately on the four screw placement surfaces LP1 to LP4. An example of part CV is shown below. In this example, 16 screw members 10 are distributed and arranged, four each on four screw placement surfaces LP1 to LP4. The 70% valley point areal density in this configuration is twice that of the configuration in FIG.

In the various embodiments described above, four screw members are arranged in a cross shape on the screw arrangement surface, but the number and arrangement form of the screw members on the screw arrangement surface are not limited to these. FIG. 11 shows an example in which a surface screw set is composed of three screw members 10. The tip surfaces of the three screw members 10 form a triangular center gap 15.

In addition, in the configuration of Fig. 1C, when the inner diameter of the liquid flow path 3 (throttled portion 9) is expanded, the total flow cross-sectional area is ensured to be 3.8 mm2 ^or more, and the in-plane flow area ratio is ensured to be 40% or more. If the conditions described above are satisfied, the number of screw members arranged on one screw arrangement surface, that is, the number of screw members constituting the surface screw set, should be more than four, for example, 6 or 8. It can also be used as a book. FIG. 12 shows an example in which the surface screw set is composed of eight screw members.

Further, when the threaded member is arranged along the inner diameter (diameter) of the liquid flow path 3 (throttled portion 9), it is also possible to omit the center gap by using a threaded member that crosses the inner diameter. FIG. 13 shows an example in which a surface screw set is constructed by four screw members without forming a center gap. Moreover, FIG. 14 shows an example in which two sets of the surface screw sets shown in FIG. 13 are arranged with their positions shifted in the central axis direction and their angular phases shifted by 45 degrees. In particular, in a large flow rate nozzle where the inner diameter of the constriction part 9 exceeds 10 mm, a sufficient flow velocity near the center of the cross section can be ensured even if the center gap is omitted, and the number of thread valleys near the center of the cross section where high flow speed can be achieved is increased. There is no problem above.

Further, the gas-liquid mixer 150 in FIG. 1B is not limited to the form in which a twisted plate member is used as the flow path forming member 155. For example, the flow path forming member may be formed as a solid cast member having a shape that combines the space occupied by the torsion plate member and the space occupied by the second spiral flow path 158, and this may be inserted into the corresponding member 151. . In this case, the second spiral flow path 158 in FIG. 1B is occupied by the flow path forming member, resulting in a gas-liquid mixer in which only the first spiral flow path 157 is formed.

Below, the results of various experiments conducted to confirm the effectiveness of the liquid treatment nozzle will be explained.
Various liquid processing nozzles for testing (hereinafter referred to as "test nozzles") having the shapes shown in FIG. 1C were created. FIG. 21 illustrates the dimensional relationship of each part in FIG. 1C. The material of the nozzle body 2 is ABS resin, the inner diameter of the liquid inlet 4 and the liquid outlet 5 is 20 mm, and the lengths of the inlet chamber 6 and the outlet chamber 7 in the flow direction are 15 mm and 45 mm, respectively. In addition, in the cavitation treatment section, the length of the constricted part 9 is 12 mm (up to 4 face screw sets) to 17 mm (8 face thread sets), and the inner diameter D of the constricted part 9 is various values from φ3.8 to φ11.5 mm. It was set to

The screw member used was a No. 0 class 1 pan head machine screw with a metric coarse pitch specified in JIS: B0205 (1997), and the material was stainless steel (SUS304). In addition, the nominal screw diameter of the legs is M1.0 (screw pitch: 0.25 mm, screw head outer diameter: 1.8 mm), M1.4 (screw pitch: 0.30 mm, screw head outer diameter: 2.0 mm). , M1.6 (thread pitch: 0.35 mm, screw head outer diameter: 2.4 mm), M2.0 (screw pitch: 0.40 mm, screw head outer diameter: 3.0 mm). The number of screw arrangement surfaces (surface screw sets) in the cavitation treatment section is from 1 to 8, and is set at various surface spacings. In addition, as shown in FIG. 20, a liquid treatment nozzle was also created in which two throttle holes 9 were formed in the partition wall 8 formed in the cavitation treatment section, and four screw members 10 were arranged in a cross shape for each throttle hole 9. .

The number and layout of screw members (plane screw sets) on each screw arrangement surface are three shown in FIG. 11, four shown in FIGS. 2 and 6, and eight shown in FIG. The positional relationship (angular phase) of the plane screw sets is either the same phase as shown in Figures 1C, 4, and 5, or 45° as shown in Figures 7 to 9 (if there are three or more screw placement planes, alternately shifted by 45°) (configuration). Further, the total flow cross-sectional area a of each screw placement surface was set to 3.4 to 56.8 mm ² and the in-plane flow area ratio was set to various values from 37.5% to 73.7%. Note that the test nozzles numbered 13 and 15 in Table 3 were configured to include one screw arrangement surface with only two threaded members arranged in the diametrical direction (in the table, "1/2" and display).

In addition, the number of 70% valley points inside the reference circle on each screw placement surface was counted on the projected image showing the layout of the screw members in the throttle section, and the total value on the screw placement surface was calculated as the total cross-sectional area of the throttle hole. A 70% valley point areal density value was calculated for each test nozzle by dividing the 70% valley point areal density value. For each nozzle created, the inside diameter of the constricted part, the number of screws in the assembly, the arrangement of surface screws, the spacing between surface screws, the in-plane flow cross-sectional area, the in-plane flow area ratio, the total number of 70% valley points, and the 70% valley point areal density. Each value is summarized in Tables 1 to 4. In addition, in each of the test nozzles in Tables 1 and 3, a screw member with a nominal screw diameter of M1.4 was used.

Next, a gas-liquid mixer 150 shown in FIG. 1B was created as follows. The outer cylinder member 151 was a stainless steel pipe member having a total length of 200 mm and an inner diameter Dx of 20 mm. The torsion plate member 155 was created by twisting a stainless steel band member with a thickness of 1 mm, a width of 14.8 mm, and a length of 200 mm so that the torsion period λ would be various values from 20 to 100 mm (Table 5 : Numbers 501 to 504). Then, using tap water as the liquid in the device system shown in FIG. The open flow rate was measured using a flowmeter (not shown). Further, the volumetric flow rate of the air supplied from the air compressor 170 to the multiphase flow supply unit (Venturi ejector) 165 is controlled by a flow rate adjustment valve 172 provided on the gas supply pipe 171, based on the flow rate when the circulating water is opened. The multiphase flow obtained at the outlet side of the gas-liquid mixer 150 is guided in-line to the flow cell of a laser scattering particle size meter (Shimadzu Corporation: SALD2200), and the secondary air bubbles contained are adjusted to 15%. The average diameter was measured (average bubble diameter ds (μm) after passing through the mixer).

Next, the water in the liquid storage part 250 (resin water tank: volume 150 L) was replaced with test deoxygenated water in which the amount of dissolved oxygen was reduced to 1 ppm by stripping treatment by blowing nitrogen gas into tap water. . Next, test nozzles numbered 21, 22, and 24 in Table 4 were connected to the downstream side of the gas-liquid mixer 150 as shown in FIG. 1A, and when the pump 175 was operated without mixing air. The flow rate was measured. Then, the outflow side end of the circulation pipe 180 is replaced in another recovery tank (not shown), and the pump 175 is operated while readjusting the air flow rate to 15% of the flow rate of the circulation pipe 180. Water from the liquid storage section 250 was collected into a recovery tank while being mixed with air by passing through the liquid processing device 300 only once, and the amount of dissolved oxygen was measured using an optical dissolved oxygen meter. Furthermore, as a comparative example, similar measurements were conducted for a case in which the gas-liquid mixer 150 was omitted (number 506: "*" indicates a comparative example). The above results are shown in Table 5.

According to this, when any test nozzle is installed, the amount of dissolved oxygen increases from 1 ppm before the test starts due to air mixing in one pass, but this increase is the same as when the gas-liquid mixer 150 is not connected. It can be seen that the results are better when connected. Looking at the results in more detail, assuming that the thread pitch of the threaded member used in the liquid processing nozzle is h, the average bubble diameter ds after passing through the mixer obtained at the outlet of the gas-liquid mixer 150 is 1.5 h or less (that is, ds/h 1.5 or less), especially when it is 1.0 h or less, it can be seen that the dissolved oxygen concentration after one-pass air mixing increases more markedly. It can also be seen that the average bubble diameter ds tends to shrink significantly when λ/Dx is 4 or less. On the other hand, it can be seen from the results in Table 5 that in the gas-liquid mixer numbered 501, in which λ/Dx is 1.5 or less, the decrease in the flow rate when open is somewhat large and the pressure drop is increased.

Next, the following tests were conducted using the test nozzles shown in Tables 1 to 4.
(1) Water flow test A test device shown in FIG. 22 was constructed, each test nozzle was installed, and a water flow test was conducted. Specifically, tap water with a water temperature of 20° C. and a dissolved oxygen concentration of 5 ppm was poured into a storage tank with a capacity of 50 L. The piping system was created using a PVC pipe with an inner diameter of 20 mm. One end of the suction piping was connected to the suction side of the vane pump, and the other end was inserted into the storage tank. On the other hand, the pipe on the pump discharge side branches into a test pipe to which a test nozzle is attached and a relief pipe that does not pass through the test nozzle, and water passing through the relief pipe is returned to the storage tank. The liquid treatment device of the present invention including a test nozzle is attached to the tip of the test pipe, and a dynamic hydraulic pressure gauge and a flow meter are inserted upstream thereof. By driving the vane pump in this state, it is possible to read the hydraulic pressure and flow rate when water is passed through the test nozzle in an open manner. In addition, the treated water that has passed through the test nozzle is collected in a collection tank. A flow rate adjustment valve is provided on the relief pipe, and by adjusting the opening degree of the valve, the hydraulic pressure and flow rate applied to the nozzle can be set to arbitrary values in a stepless manner.

In the water flow test, the dynamic water pressure was fixed at 0.077 MPa for all test nozzles, and the flow rate when water flowed without introducing air was measured. In addition, for some particularly selected test nozzles, we measured the flow rate changes when the hydrodynamic pressure was varied in various ways. In addition, the screw arrangement surface is only one surface, and the number and layout of the screw members (plane screw set) are four as shown in FIG. A separate test was also conducted to investigate the relationship between the flow cross-sectional area and the flow rate when the hydrodynamic pressure was fixed at 0.077 MPa using test nozzles with variously changed areas a.

(3) Evaluation of air dissolution ability when combined with a gas-liquid mixer In order to construct the liquid processing device 300 shown in FIG. Similar to the test results shown in 5, using deoxygenated water for testing with the amount of dissolved oxygen reduced to 1 ppm, while introducing 15% air by volume based on the water flow rate without air mixing. The dissolved oxygen concentration of the water collected after passing through the liquid treatment device 300 only once was measured.

(4) Slimy stain cleaning power evaluation test Using Hikiwari natto as a model for slimy stains similar to biofilm, tap water ( The detergency was evaluated using test water (initial oxygen concentration: 5 ppm). The water nozzle 201, which constitutes the main part of the device 200, is a PVC pipe with an inner diameter of 20 mm, the tip of which is sealed with a cap, and a plurality of nozzle holes are drilled through the pipe wall at intervals of 5 mm in the pipe axis direction. be. By supporting this water nozzle horizontally and supplying test water to the base end, it is sprayed downward from each nozzle hole.

The test water used the equipment system shown in Figure 22, and the conditions for the water flow test in (1) were changed to introduce air by adjusting the flow rate so that the final dissolved oxygen concentration in the recovered water was adjusted to 6 ppm. At the same time, the treated water, which had undergone cavitation treatment while being introduced with air through the liquid treatment device, was collected as test water in a collection tank (however, the hydraulic pressure was set at 0.077 MPa). The storage tank was then replaced with a recovery tank from which the test water was collected, and the liquid treatment device was replaced with a water spray nozzle. As a result, referring to FIG. 22, the test water in the recovery tank is sucked up by the vane pump and sprayed from the water nozzle 201 as shown in FIG. 19. Directly below the water spray nozzle 201, a rectifying tile 207 is installed vertically. The water spray nozzle 201 is tilted forward around the axis so that the water stream hits the upper surface of the rectifying tile 207 diagonally in front of the rectifying tile 207, and the water stream WF injected from each nozzle hole spreads on the rectifying tile 207. It becomes a single body and flows down like a film of water.

The sample tile 206 coated with the dirt model NT is arranged directly below the rectifying tile 207, and the film-like cleaning water flow WF from the rectifying tile flows down evenly in the width direction. The sample tile 206 is tilted by about 3 degrees by the spacer 205 so that the lower end side protrudes forward. The width of the water jet section of the water spray nozzle 201 is about 30 cm. Further, the rectifying tile 207 and the sample tile 206 are made of ceramic with a white and smooth glaze layer formed on one side, and have a height TH of 9 cm and a width TW of 18 cm. The width of the dirt model NT on the sample tile 206 is set to 3 to 4 cm, the total flow rate of the treated water to be injected is 6 L/min, and the actual flow rate hitting the dirt model NT is adjusted to 0.6 to 0.7 L/min. ing. As a result, for the removal of the dirt model NT, the main effect is the infiltration of the natto particles into the slimy layer that adheres to the tile, rather than the impact kinetic energy of the water flow.

The dirt model NT is made of Hikiwari natto, which is colored red with a dye and applied to the sample tile 206. The size of the bean particles contained in Hikiwari Natto is 2 to 3 mm, and the total coating weight is standardized to 1 g (number of particles: 40 to 50) using a digital scale. The sample tile after applying the stain model NT was dried for 90 minutes in an air-conditioned room at 20° C. and 50% RH, and then subjected to the test. During the test, a video was taken of the falling and removal of natto particles from the sample tile 206 as the cleaning progressed, and a video was taken of the change in the ratio of the number of removed particles to the initial total number of particles on the sample tile 206 as the water flow progressed. I read it from. Specifically, the same test was repeated three times for each case of circulating test water and normal water, and the average value of the three water passage times at which the removal rate was 50% was read.

The cleaning power of the test water was evaluated by the water flow time described above, but in order to facilitate comparison between normal tap water that has not been subjected to cavitation treatment and test water using different test nozzles, the following measures were taken. method was used.
・The test water was collected in a collection tank, left undisturbed for 10 minutes, and then used for testing. The test water after being left for 10 minutes was checked with a laser diffraction particle size meter (Shimadzu Corporation: SALD2200) to see if microbubbles could be measured. Along with water, the measurement results were below the detection limit.
・Evaluation of cleanability was performed by performing cavitation treatment using sample tiles created under the same conditions, rather than by comparing the absolute value of water flow time across multiple test nozzles. The water flow time ratio (removal rate: 50%) between normal water (blank water) and test water was compared. The above test results are summarized in Tables 1 to 4.

The obtained results will be explained below.
Figure 15 shows test nozzles with only one screw placement surface and various total flow cross-sectional areas (liquid flow area) of the screw placement surface, with dynamic water pressure fixed at 0.077 MPa, which is in the normal water pressure region. It is a graph showing the result of examining the relationship between the flow cross-sectional area a and the flow rate ρ when set. As is clear from this graph, in the region where the flow cross-sectional area a on the screw arrangement surface is 5.0 ^mm2 or more, as the area a increases, the flow rate ρ becomes a linear function of a:
ρ=1.75a+2.93...(I)
It can be seen that it shows a tendency to increase linearly. On the other hand, in a region where the flow cross-sectional area a is 5.0 ^mm2 , the flow rate ρ deviates downward from the above linear relationship, and as the total flow cross-sectional area a decreases, a function that depends on the logarithm of the area a:
ρ=9.28×ln(a)-3.37...(II)
It can be seen that the flow rate ρ is rapidly decreasing. This means that under normal water pressure flow conditions, when the total flow cross-sectional area a is less than 5.0 ^mm2 , the pressure drop increases rapidly as the number of face thread sets in the nozzle increases. This means that it becomes impossible to obtain a flow rate commensurate with the flow cross-sectional area. The specific conditions for the total flow cross-sectional area a to be 5.0 mm ² are, for example, when the inner diameter of the constriction part 9 is set to 4.2 mm and four M1.4 screw members are arranged according to the layout shown in Figure 2. corresponds to

Figure 16 explains the reason why it is important to ensure the total flow cross-sectional area a to be 5.0 mm2 ^or more in order to increase the number of face thread sets and further increase the value of the 70% valley point area density. It is. The horizontal axis represents the flow velocity distribution in the radial direction of the cross section of the throttle hole that forms the circular screw arrangement surface. Since the threaded member is placed within the cross section, the shape of the flow velocity distribution is naturally considered to be affected by this, but if we consider the symmetry of the threaded member arrangement, it will be the same as when no threaded member is placed within the cross section. , it is generally reasonable to assume a parabolic flow velocity distribution with the maximum value at the center of the cross section (solid line in the figure). From this state, if the inner diameter of the constricted portion 9 is reduced to, for example, 3.5 mm, the total flow cross-sectional area a becomes 3.5 mm ² . Even in this region, if we consider that the flow rate ρ changes according to the linear function shown by equation (I) with respect to the area a, the flow rate estimated from the extrapolated value of equation (I) to a = 3.5 mm ² is approximately It becomes 9.0L/min. However, in reality, due to the increase in pressure drop, the flow rate in this region is governed by equation (II), which includes the logarithm of a, and is around 8.3 L/min, which is 10% lower than the extrapolated value of equation (I). I understand that.

In this case, if the influence of pressure drop is small in this region and equation (I) holds true, the flow velocity distribution in the radial direction of the cross section should be the same as in the case of a = 5.0 mm ² , but in reality The flow velocity distribution in the radial direction has a parabolic shape with the maximum value reduced by 10% from the case of a=5.0 mm ² , as shown by the broken line in FIG. 16 . At a position corresponding to 70% of the cross-sectional radius, the flow velocity becomes approximately 1/2 of the maximum value ρ _M. Therefore, if the maximum flow velocity is reduced by 10% from the extrapolated value from equation (I), the cross-sectional radius position where the flow rate is 1/2 of the maximum value ρ _M when a = 5.0 mm ² is calculated to be 70 Reduce from the % position to the 67% position. If one more set of plane screws having such characteristics is added in the direction of the flow path axis, the cross-sectional radius position that provides 1/2 of ρ _M is further reduced to a 63% position.

When the inner diameter of the throttle part 9 is 3.5 mm and the nominal thread diameter M of the screw member is 1.4, according to geometric calculation, the number of 70% thread valleys is 8, whereas the number of 70% thread valleys is 8. The number is reduced by half to four. In this way, even if two sets of surface screws with a = 3.5 mm ² are arranged in the axial direction and the number of screw members in the flow path cross section is doubled, only one set of surface screws will be installed due to the increase in pressure loss. It can be seen that it cannot contribute to an increase in the number of thread roots by 70% compared to the case where On the other hand, if the surface screw set is set to a > 3.5 mm ² , the increase in pressure loss when two sets are arranged in the axial direction is smaller than when a = 3.5 mm ² . The increase is thought to theoretically contribute to a 70% increase in the number of thread roots, ie, an increase in the 70% root area density. In this case, the lower limit of the total flow cross-sectional area a is preferably around 3.8 mm ² , but it is more preferably set to 5.0 mm ² or more so that the above formula (I) holds true. Then, as explained in detail below based on the experimental results, the four cross-shaped screw members constituting the surface screw set are arranged in the same phase between the adjacent screw arrangement surfaces (that is, the legs of the screw members When adopting a configuration in which the screws are arranged in a positional relationship in which they overlap each other while matching the longitudinal direction, there is almost no increase in pressure loss due to the addition of surface threads, and it is possible to dramatically increase the number of thread roots by 70%. can. Furthermore, even when surface screw sets are arranged with the angular phase shifted between mutually adjacent screw arrangement surfaces, by increasing the distance between the surface screw sets, it is possible to suppress the increase in pressure loss due to the addition of surface thread sets, and 70 % thread root number can be similarly increased.

Figure 17 shows a surface screw set consisting of four cross-shaped screw members (M1.4) with an inner diameter of 5.0 mm in the constricted part, and a screw arrangement surface interval of 1.4 mm to 8.4 mm (nominal screw diameter). Test nozzles (numbered 1 to 5, hereinafter referred to as 45° nozzle : In Table 1 above, only numbers 2 and 4 were used for cleaning evaluation). The hydraulic pressure is set to various values from 0.046 MPa to 0.089 MPa, and each measured flow rate value is plotted against the set dynamic hydraulic pressure value. In addition, as comparison nozzles, one with only one set of surface screws (number 101), one with only one set of surface screws and the number of screw members increased to eight (number 102), The results obtained using the two-hole type shown in FIG. 20 (number 103) are also shown.

According to the above results, when the screw arrangement surface spacing dp is 1.4 mm (1.0M), which is equal to the nominal screw diameter, the increase in pressure loss is reduced when compared with nozzle number 101, which has only one set of surface screws. Although it is large, the flow rate is larger than the nozzle No. 102 in which eight screw members are arranged in the same plane, and the effect of reducing pressure loss by distributing the plane screw sets in the axial direction is clearly recognized. In addition, the flow rate of the nozzle No. 2 in which the screw arrangement surface spacing dp was increased to 1.5M was significantly increased, and the pressure loss reduction effect was extremely significant. This tendency becomes more pronounced as the screw arrangement surface spacing dp further increases (number 3: dp = 3.0M), and when the screw arrangement surface spacing dp reaches 4.5M, the surface screw set is multiplexed in the axial direction. Even when compared with numbers 101 and 103, which do not have the same flow rate, the flow characteristics are almost the same. In other words, it can be seen that by adopting such an arrangement surface spacing, almost no increase in pressure loss occurs even if a surface screw set is added with a shifted angular phase shift.

Fig. 18 shows a plane screw set consisting of four cross-shaped screw members (M1.4) with the inner diameter of the constriction part being 5.0 mm, and the screw arrangement surface spacing dp is 2.1 mm (=1.5M). This shows the results of a water flow test conducted using test nozzles (numbers 6 to 8) in which 2 to 8 sets of test nozzles (numbers 6 to 8) were set as shown in Figures 2, 4, and 5 and arranged in the same phase. be. The hydraulic pressure is set to various values from 0.046 MPa to 0.089 MPa, and each measured flow rate value is plotted against the set dynamic hydraulic pressure value. Also shown are the results for the 45° nozzle numbered 2 in FIG. 17, which has the same screw arrangement surface spacing. It can be seen that by arranging the plane screw sets in the same phase, the pressure loss hardly increases even if the number of plane screw sets is increased to eight sets. It can also be seen that the flow rate value is significantly increased compared to the 45° nozzle (number 2) with the same surface spacing.

The results of the slime/stain cleaning power evaluation test conducted for each nozzle will be explained below with reference to Tables 1 to 4. Table 1 shows the results for the 45° nozzles No. 2 and No. 4 and the in-phase nozzle No. 6 used in the water flow test, together with the results for the comparative nozzles No. 101 to 103. Moreover, the number 200 shows the result when normal tap water without cavitation treatment was used as blank water (normal water). As mentioned above, the evaluation is based on the water flow time ratio (removal rate: 50%) of the test water to the blank water when the removal rate is 50%, and when the value of this water flow time ratio is 1, the slime The detergency against dirt is equivalent to that of blank water, and when it is less than 1, it means that slimy dirt can be removed in a shorter time than blank water, and the smaller the absolute value, the better the detergency against slimy dirt. Show that there is.

First, the water treated by the nozzle No. 101 with only one set of surface threads has a water flow time ratio of less than 1, and has clearly better cleaning power than blank water. In addition, the results for nozzle No. 102, which had only one set of face screws but increased the number of screw members to eight, and Nozzle No. 103, which had two aperture holes, were also better than the blank water. It is shown that.

Here, the nozzle No. 102 has a 70% valley point area density of about 1.8 times that of the nozzle No. 101, and exhibits a particularly good cleaning effect. In addition, the in-plane flow area ratio was also secured at 5.1 ^mm2 , and it is considered that the flow velocity necessary for cavitation is sufficiently secured, but the value of the in-plane flow area ratio is as small as 26%, and the flow rate is also 6.1 mm2. It is small at 8L/min. In addition, the stain cleaning power evaluation test is also conducted using treated water diluted two times (or three times) with blank water. The ratio shows a good value of 0.5 or less. The table also shows the calculated value of the 70% valley point flow density obtained by dividing the 70% valley point number by the water flow rate at a hydraulic pressure of 0.077 MPa; It can also be understood that the cleaning ability indicated by the time ratio becomes better.

Next, regarding the results of test nozzles No. 2, 4, and 6, the cleaning ability of the treated water is superior because the 70% valley point area density is larger than that of nozzles No. 101 and No. 103. Recognize. On the other hand, in a comparison of the 70% trough point flow density, it is slightly inferior to the nozzle No. 102, and although the cleaning ability is not as good as this, it is similar to the Nozzle nozzle No. 102. When compared, the results show overwhelmingly good flow rates due to the increased in-plane flow area ratio.

Table 2 shows the results for the No. 7 and No. 8 nozzles, which have an increased number of face threads in an in-phase arrangement, compared to the results for the No. 101 and No. 6 test nozzles. Nozzles No. 7 and No. 8 have a small increase in pressure loss due to an increase in the number of surface threads, so while maintaining a large flow rate, both the 70% valley point area density and the 70% valley point flow density increase significantly. There is. As a result, even when the dilution rate is increased two to three times, the cleaning ability indicated by the water flow time ratio is better.

Table 3 summarizes the results of test nozzles (numbers 9 to 15) in which M1.4 screw members were used, but the inner diameter of the throttle part, the number of screws in the surface screw set, and the number of the surface screw sets were variously changed. It is. Further, numbers 109, 111, 112, and 113 represent nozzles having only one set of surface threads having the same configuration as the test nozzles numbered 9, 11, 12, and 13. Nozzle No. 10 uses a surface screw assembly shown in FIG. 11, which is composed of three screw members, and Nozzle No. 15 uses a surface screw assembly, in which the inner diameter of the throttle part is set to a value exceeding 10 mm. It is composed of eight wires shown in FIG. 12. In addition, the nozzles numbered 13 and 15 use 4 to 8 surface screws, but the number of screws is halved for one layer (for 4 surface screws, two diametrically opposing nozzles are used). The eight face screw sets are thinned out to only four cross-shaped screws). The test nozzles of Examples Nos. 9 to 15 had a 70% valley point area density of 2.0 nozzles/mm even though the flow rate increased to 30 L/min or more due to the expansion of the inner diameter of the constriction part 9. ² or more, and exhibits better cleaning performance than the nozzles numbered 109, 111, 112, and 113, which were provided with only one set of surface threads.

Table 4 shows test nozzles (number 21 -24). All of them exhibit good cleaning performance, but the nozzles numbered 22 to 24, which use screw members with a large thread depth of M1.4 to M2.0, have a small thread depth of M1.0. It can be seen that the same cleaning performance can be achieved with a smaller 70% valley point area density compared to the nozzle No. 21 using the threaded member.

In this way, any of the nozzles in Tables 1 to 4 can be used in combination with the gas-liquid mixer 150 (the one with number 503 in Table 5) to configure the liquid treatment device of the present invention. Delivers excellent cleaning performance. Furthermore, it can be seen that good results were obtained in all evaluations of air dissolution ability (dissolved oxygen concentration) using deoxygenated test water.

1 Liquid processing nozzle 2 Nozzle body 3 Liquid flow path 5 Liquid outlet 4 Liquid inlet 9 Restriction hole 10 Screw member 150 Gas-liquid mixer 151 Outer cylinder member 155 Channel forming member 156 Spiral section 157 First spiral channel 158 Second spiral Flow path 159 Inlet 160 Outlet 300 Liquid treatment device LP1 to LP4 Screw arrangement surface CV Cavitation treatment section

Claims (13)

A single liquid flow path having a liquid inlet at one end and a liquid outlet at the other end is formed, and a part of the liquid flow path is connected to a nozzle body defined as a cavitation treatment section and to the cavitation treatment section. and a plurality of screw members assembled to the nozzle body so that the tip end side of the leg protrudes inside the flow path, the liquid in which gas is dissolved flows from the liquid inlet to the liquid outlet, and the cavitation treatment is performed. A liquid that performs cavitation treatment based on vacuum precipitation of the gas dissolved in the liquid by bringing the liquid into contact with the thread valley formed on the outer circumferential surface of the leg of the screw member at an increased speed. a processing nozzle;
A hollow outer cylindrical member having an inlet at one end and an outlet at the other end, and a spiral flow path provided inside the outer cylindrical member and connecting the inlet and the outlet. a flow path forming member formed such that the helical axis of the flow path is along the central axis of the outer cylinder member, and the liquid a gas-liquid mixer provided on the liquid inlet side of the processing nozzle;
A liquid processing device comprising: a multiphase flow supply unit that supplies a multiphase flow of the gas and the liquid to the inlet of the gas-liquid mixer,
The liquid processing device supplies the bubbles in the multiphase flow to the liquid processing nozzle while pulverizing them by flowing them through the spiral flow path of the gas-liquid mixer, and eliminates the turbulent area generated in the cavitation processing section. The finely pulverized gas is drawn into and dissolved in the pulverized gas ,
In the liquid treatment nozzle, the threaded member has a thread pitch and thread depth of 0.20 mm or more and 0.40 mm or less, and a nominal thread diameter M of 1.0 mm or more and 2.0 mm or less, and the cavitation treatment section In the method, a plurality of virtual screw placement surfaces perpendicular to the central axis of the liquid flow path are set along the central axis, and two or more screw members are distributed to each of the screw placement surfaces. The leg has a structure in which the longitudinal direction of the leg is arranged along the screw arrangement surface, and the screw members, a total of eight or more, are arranged in such a manner that two or more screw members are distributed to each of the screw arrangement surfaces. At the same time, the area of the liquid circulation area of the liquid flow path is secured at 3.8 mm ² or more on each of the screw arrangement surfaces, and the in-plane circulation is determined as the ratio of the liquid circulation area to the total cross-sectional area of the liquid flow path. A full thread with a valley point that has an area ratio of 40% or more and is located in an area within 70% of the radius of the liquid flow path from the cross-sectional center of the liquid flow path when projected onto a plane orthogonal to the central axis. When defined as the 70% valley point areal density obtained by dividing the total number between the arrangement surfaces by the cross-sectional area of the liquid flow path, ensure that the value of the 70% valley point areal density is 1.6 pieces/mm2 or more ^. further, the distance between the screw arrangement surfaces adjacent to each other in the central axis direction of the liquid flow path is ensured to be equal to or larger than the nominal screw diameter,
On each of the mutually adjacent screw arrangement surfaces, three or more of the same number of screw members are arranged at equal angular intervals around the center of the cross section so that the leg portions are along the radial direction of the cross section of the liquid flow path, and . A liquid processing device, wherein the arrangement angle phase of the screw member around the center of the cross section is determined to be the same between the adjacent screw arrangement surfaces. 2. The liquid processing apparatus according to claim 1, wherein the gas-liquid mixer finely pulverizes the bubbles to a bubble diameter of 1.5 h or less, with a screw pitch of the screw member being h (mm). The flow path forming member of the gas-liquid mixer is configured as a twisted plate member obtained by twisting a strip-shaped metal plate such that the central axis in the width direction of the metal plate is the helical axis, and the spiral flow path is , a first spiral flow path formed by a space between the first main surface of the torsion plate member and the cylindrical inner circumferential surface of the outer cylinder member; a second main surface of the torsion plate member and the outer cylinder; 3. The liquid treatment device according to claim 1, further comprising a second spiral flow path formed by a space between the member and the cylindrical inner circumferential surface of the member. 4. The liquid processing device according to claim 3, wherein the outer cylinder member has a total length determined such that the first spiral flow path and the second spiral flow path each include a spiral section of 1.5 periods or more. . A claim in which λ/Dx is set to 1.5 or more and 4 or less, where the inner diameter of the cylindrical inner peripheral surface of the outer cylinder member is Dx (mm), and the helical periodic length of the torsion plate member is λ (mm). The liquid treatment device according to claim 3 or 4. Claim: The area of the liquid flow region of the liquid flow path is ensured at 5.0 mm ² or more on each of the screw arrangement surfaces, and the value of the 70% valley point area density is ensured at 2.0 pieces/mm ² or more. The liquid treatment device according to any one of claims 1 to 5 . Any one of claims 1 to 6, wherein the screw member is arranged on the screw arrangement surface in a positional relationship such that the longitudinal direction of the leg matches the diameter of the circular axial cross section of the liquid flow path. The liquid treatment device according to item 1 . 2. The liquid processing device according to claim 1 , wherein two or more screw arrangement surfaces including three or more of the screw members are set in the direction of the central axis. 9. The liquid treatment according to claim 8 , wherein the three or more screw members on the screw arrangement surface are arranged such that a tip end surface of the leg portion of each screw surrounds the center of the cross section to form a center gap. Device. 2. The liquid processing device according to claim 1 , wherein the screw member has a head having a larger diameter than the leg, and an interval between the screw arrangement surfaces is set to be larger than an outer diameter of the head. The liquid treatment device according to claim 1 , wherein the interval between the screw arrangement surfaces in the central axis direction is set to be 2.0 times or more the nominal screw diameter of the screw member. 12. The liquid treatment device according to claim 11 , wherein an interval between the screw arrangement surfaces in the direction of the central axis is set to be 4.0 times or more the nominal screw diameter of the screw member.
A single liquid flow path having a liquid inlet at one end and a liquid outlet at the other end is formed, and a part of the liquid flow path is connected to a nozzle body defined as a cavitation treatment section and to the cavitation treatment section. and a plurality of screw members assembled to the nozzle body so that the tip end side of the leg protrudes inside the flow path, the liquid in which gas is dissolved flows from the liquid inlet to the liquid outlet, and the cavitation treatment is performed. A liquid that performs cavitation treatment based on vacuum precipitation of the gas dissolved in the liquid by bringing the liquid into contact with the thread valley formed on the outer circumferential surface of the leg of the screw member at an increased speed. a processing nozzle;
A hollow outer cylindrical member having an inlet at one end and an outlet at the other end, and a spiral flow path provided inside the outer cylindrical member and connecting the inlet and the outlet. a flow path forming member formed such that the helical axis of the flow path is along the central axis of the outer cylinder member, and the liquid a gas-liquid mixer provided on the liquid inlet side of the processing nozzle;
A liquid processing device comprising: a multiphase flow supply unit that supplies a multiphase flow of the gas and the liquid to the inlet of the gas-liquid mixer,
The liquid processing device supplies the bubbles in the multiphase flow to the liquid processing nozzle while pulverizing them by flowing them through the spiral flow path of the gas-liquid mixer, and eliminates the turbulent area generated in the cavitation processing section. The finely pulverized gas is drawn into and dissolved in the pulverized gas,
In the liquid treatment nozzle, the threaded member has a thread pitch and thread depth of 0.20 mm or more and 0.40 mm or less, and a nominal thread diameter M of 1.0 mm or more and 2.0 mm or less, and the cavitation treatment section In the method, a plurality of virtual screw placement surfaces perpendicular to the central axis of the liquid flow path are set along the central axis, and two or more screw members are distributed to each of the screw placement surfaces. The leg has a structure in which the longitudinal direction of the leg is arranged along the screw arrangement surface, and the screw members, a total of eight or more, are arranged in such a manner that two or more screw members are distributed to each of the screw arrangement surfaces. At the same time, the area of the liquid circulation area of the liquid flow path is secured at 3.8 mm ² or more on each of the screw arrangement surfaces, and the in-plane circulation is determined as the ratio of the liquid circulation area to the total cross-sectional area of the liquid flow path. A full thread with a valley point that has an area ratio of 40% or more and is located in an area within 70% of the radius of the liquid flow path from the cross-sectional center of the liquid flow path when projected onto a plane orthogonal to the central axis. When defined as the 70% valley point areal density obtained by dividing the total number between the arrangement surfaces by the cross-sectional area of the liquid flow path, ensure that the value of the 70% valley point areal density is 1.6 pieces/mm2 or more ^. is,
As the screw placement surface, at least a first screw placement surface, a second screw placement surface, a third screw placement surface, and a fourth screw placement surface are set in this order along the central axis of the liquid flow path. and on each screw arrangement surface, the same number of three or more screw members are arranged at equal angular intervals around the center of the cross section so that the leg portions are along the radial direction of the cross section of the liquid flow path,
In the first screw placement surface, the second screw placement surface, the third screw placement surface, and the fourth screw placement surface, the distance between the screw placement surfaces adjacent to each other in the central axis direction is equal to the nominal screw diameter. 1.5 times or more, and the arrangement angle phase of the screw member around the center of the cross section is determined in a manner shifted from each other between the adjacent screw arrangement surfaces,
Between the first screw placement surface and the third screw placement surface, the placement angle phases of the screw members are determined to match each other,
A liquid processing nozzle, wherein the arrangement angle phases of the screw members are determined to match each other between the second screw arrangement surface and the fourth screw arrangement surface.

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