JP2017047423A - Mixing treatment body, mixing treatment method, fluid mixer, fluid mixing treatment apparatus, and system for culturing fish and shellfish - Google Patents

Abstract

PROBLEM TO BE SOLVED: To achieve reduction in electric power consumption of a pressure pump while reducing pressure loss, and increase outflow (improve efficiency) of mixing treated fluids.SOLUTION: A mixing treatment body has a plurality of mixing treatment flow passages through which multiple different fluids that are mixing treatment objects circulate so as to be subjected to mixing treatment. Each mixing treatment flow passage includes: an inflow starting end part where the fluids flow in; a middle part disposed and communicating in a separated state outward in the periphery of the inflow starting end part; and an outflow finishing end part communicating with the middle part and arranged by mutually changing positions with the inflow starting end part. The mixing treatment body is configured so that the fluids circulate in a meandering manner.SELECTED DRAWING: Figure 1

Description

  The present invention includes a mixed processing body and a mixing processing method for mixing and processing a plurality of different fluids, a fluid mixer including the mixed processing body, a fluid mixing processing apparatus equipped with the fluid mixer, and a fluid mixing processing apparatus. Related to aquaculture system. As the plurality of different fluids here, for example, there are combinations of liquid and liquid, liquid and gas, powder and liquid, and the liquid includes water, bath water, seawater, fuel oil, etc. Examples of the gas include oxygen, carbon dioxide, nitrogen, and air. Seafood is aquatic animals such as fish and shellfish.

  Conventionally, there exists what was disclosed by patent document 1 as one form of the fluid mixer. That is, in Patent Document 1, a disk-shaped second diffusion element is disposed opposite to a disk-shaped first diffusion element in which a fluid inlet is formed at the center, and between the two diffusion elements. A diffusion / mixing unit that forms a diffusion / mixing channel that diffuses and mixes the fluid flowing in from the inlet on the center side in the radial direction toward the peripheral side, and a fluid outlet in the center The disc-shaped second collective element is arranged opposite to the disc-shaped first collective element, and the fluid flowing from the peripheral side between the two collective elements is radially directed toward the central portion side. Disclosed is a fluid mixer that includes an assembly / mixing unit that forms an assembly / mixing channel that flows and collects / mixes, and that connects a terminal end of a diffusion / mixing channel and a start end of the assembly / mixing channel. Yes.

  The opposing surfaces of the first and second diffusing elements and the opposing surfaces of the first and second assembly elements are formed with a hexagonal recess group of appropriate identical depth and size in the honeycomb structure, and the opposing recesses Arrange them at different positions so that they communicate with each other, and in the diffusion / mixing flow path and the collecting / mixing flow path, the fluid flows in the radial direction while repeating the merging and splitting (dispersing) while meandering. ing.

JP-A-9-52034

  However, the fluid mixer disclosed in Patent Document 1 includes a diffusion / mixing flow path that diffuses and mixes the fluid flowing in from the inflow port on the central portion side in the radial direction toward the peripheral portion, and the peripheral portion. Since the flow channel structure that gathers and mixes the fluid flowing in from the side in the radial direction toward the center is formed in the same way, it is more concentrated than the diffusion / mixing channel with high mixing and dispersion function.・ Although the number of dispersions in the mixing channel was much smaller, the pressure loss was the same as that in the diffusion / mixing channel. Therefore, it has been desired to reduce the power consumption of the pressurizing pump that pressurizes and supplies the fluid to the fluid mixer, and to increase the flow rate (efficiency) of the processed fluid.

  Therefore, the present invention provides a mixed processing body and a mixing processing method capable of reducing the pressure loss and improving the refinement efficiency of the dispersed phase, and in addition to that, the power consumption of the pressure pump It is an object of the present invention to provide a fluid mixer, a fluid mixing treatment device, and a seafood aquaculture system that can reduce the amount of flow and increase the outflow amount (efficiency) of the mixed treatment fluid. .

The mixed processing body according to the invention of claim 1 is:
It has a number of mixing process flow paths that are mixed and processed by the flow of a plurality of different fluids to be mixed,
Each mixing treatment channel is connected to the inflow start end portion into which the fluid flows, the midway portion that is in communication with and arranged around the inflow start end portion, and the midstream portion. And an outflow end portion where the fluid flows out at different positions, and the inflowing fluid flows in a meandering manner from the inflow start end portion through the midway portion to the outflow end portion.

The mixed treatment body according to the invention described in claim 2 is the mixed treatment body according to the invention according to claim 1,
Each mixing processing channel according to claim 1, wherein the direction in which the fluid flows into the inflow start end portion and the direction in which the fluid flows into the midway portion are the same direction, and the direction in which these fluids flow in, the inflow The direction in which the fluid flows from the start end to the middle is perpendicular to the flow direction, and the inflowing fluid flows in a meandering manner in a meandering manner from the inflow start end to the outflow end portion fluid. Has been.

The mixing method according to the invention of claim 3 is:
The mixed treatment body according to claim 1 or 2 is disposed in a fluid flow path through which a plurality of different fluids to be mixed flows.
As the fluid flows in from the inflow start end portion of each mixing processing channel included in the mixing processing body and the fluid flows in each mixing processing channel, the fluid is mixed and processed.
The fluid after the mixing process flows out from the outflow end portion of each mixing process flow path and joins in the fluid flow path.

A fluid mixer according to the invention of claim 4 is provided.
A mixing case is provided that forms a fluid flow path for disposing the mixed processing body according to claim 1.

A fluid mixer according to the invention of claim 5 is a fluid mixer according to the invention of claim 4,
In the mixing case, a plurality of mixed processing bodies are arranged in series along the fluid flow path and at intervals.

A fluid mixing treatment apparatus according to the invention of claim 6 is provided.
The liquid as the fluid and the liquid or gas as the fluid are introduced into the fluid mixer according to claim 4 or 5 so that the liquid and the liquid or the liquid and the gas are mixed in the fluid mixer. It is configured.

A fluid mixing treatment device according to a seventh aspect of the invention is a fluid mixing treatment device according to the sixth aspect of the invention,
It is configured such that water as a liquid and fuel oil as a liquid are mixed to produce an emulsion fuel oil.

A fluid mixing and processing apparatus according to an eighth aspect of the present invention is the fluid mixing and processing apparatus according to the sixth aspect of the present invention,
It is configured such that water as a liquid and nitrogen gas as a gas are mixed to generate nitrogen water in which nitrogen gas is dissolved in water.

A fluid mixing treatment apparatus according to the invention described in claim 9 is the fluid mixing treatment apparatus according to the invention according to claim 6,
Hot water or water as a liquid and carbon dioxide gas as a gas are mixed to form a carbonated spring in which carbon dioxide gas is dissolved in hot water or water.

A fluid mixing treatment apparatus according to the invention of claim 10 is a fluid mixing treatment apparatus according to the invention of claim 6,
It is configured such that water as a liquid and oxygen gas as a gas are mixed to produce oxygen water in which oxygen gas is dissolved in water.

The seafood culture system according to the invention of claim 11
A fluid mixing treatment device according to claim 10 and a culture tank for culturing seafood,
Oxygen water generated by the fluid mixing treatment device is supplied to the culture tank as culture water.

  According to the present invention, the following effects are produced. That is, according to the present invention, it is possible to provide a mixed processing body and a mixing processing method capable of reducing pressure loss and improving the refinement efficiency of the dispersed phase. In addition, in addition to reducing the power consumption of the pressure pump, the fluid mixer, the fluid mixing treatment device, and the fluid mixing treatment device capable of increasing the flow rate (efficiency) of the mixed treatment fluid, and A seafood aquaculture system can be provided.

The perspective explanatory view of the fluid mixer which comprises the mixing treatment object concerning this embodiment. II sectional view explanatory drawing of FIG. II-II sectional view explanatory drawing of FIG. The conceptual explanatory drawing of the high concentration carbonated spring production | generation apparatus which concerns on this embodiment. Control block diagram The conceptual explanatory drawing of the seafood culture system which concerns on this embodiment.

  Embodiments of the present invention will be described below with reference to the drawings. First, the configuration of the mixed processing body and the mixing processing method according to the present embodiment will be described, followed by the configuration of the fluid mixer including the mixed processing body, and then the fluid mixing equipped with the fluid mixer. The structure of the gas-liquid mixing processing apparatus which is one form of the processing apparatus will be described, and finally, the structure of the seafood aquaculture system provided with the gas-liquid mixing processing apparatus will be described.

[Description of configuration of mixed processing body]
Reference numeral 20 shown in FIGS. 1 to 3 denotes a mixed processing body according to the present embodiment. Here, the partially enlarged sectional view of FIG. 2 is a sectional view taken along the line III-III of the partially enlarged explanatory view of FIG. As shown in FIGS. 1 to 3, the mixed processing body 20 is formed by laminating three plate-like layers 30, 40, and 50 having an outer shape formed in the same shape having a rectangular plate shape.

  Each plate-like layer 30, 40, 50 is formed with a large number of through-holes 31, 41, 51 that penetrate in the thickness direction. The through holes 31, 41 or 41, 51 between the adjacent plate layers 30, 40 or 40, 50 are partly connected to the polymerization state so as to form the first and second communication holes 70, 80. The through holes 31 and 51 of the first and third plate-like layers 30 and 50 are also arranged at different positions.

  The second communication hole 80 formed by the through holes 41 and 51 between the second and third plate layers 40 and 50 is outside the area where the through hole 31 of the first plate layer 30 is projected. Are arranged in a separated state (outside the opening area of the through-hole 31). That is, when the through hole 31 is projected from the upstream side to the downstream side from the direction orthogonal to the front surface (upstream side surface) of the first plate-like layer 30, the projected area of the through hole 31 is outside the projected area. The second communication hole 80 is arranged. By doing so, the fluid F flowing in from the through hole 31 is diffused around the through hole 31 so that a uniform mixing process is performed.

  And the mixing process flow path R mentioned later is made to extend in a meandering manner and in a diffusing manner. By doing so, the nanometer level of the dispersed phase of fluid F (the level including the dispersed phase particle size of less than 1 μm, desirably the dispersed phase mode diameter is less than 1 μm, more desirably, the dispersed phase mode diameter is 100 nm. In the vicinity) is ensured.

  The through holes 31, 41, 51 of the respective plate layers 30, 40, 50 are first and second communication holes 70, 80 arranged in a separated state in the extending direction of the plate layers 30, 40, 50. And a mixing processing flow path R extending in a meandering manner and in a diffusing manner from the upstream side to the downstream side (from the first layer to the third layer). The extending direction of the plate-like layers 30, 40, 50 here is a direction orthogonal to the thickness direction of the plate-like layers 30, 40, 50, and is along the plane of the plate-like layers 30, 40, 50. Direction.

  More specifically, the three plate-like layers 30, 40, and 50 that form the mixed processing body 20 are rectangular plate shapes having the same outer shape and the same thickness. These plate-like layers 30, 40, 50 are bonded by bringing the rear surface portion 33 of the first plate-like layer 30 and the front face portion 42 of the second-layer plate-like layer 40 into surface contact with each other in a laminated state. The rear surface portion 43 of the eye plate layer 40 and the front surface portion 52 of the third plate layer 50 are brought into surface contact with each other in a laminated state and bonded together to integrally form the mixed processing body 20. Reference numeral 32 denotes a front surface portion of the first plate layer 30, and reference numeral 53 denotes a rear surface portion of the third plate layer 50. And the mixing process body 20 arrange | positions in the orthogonal state with respect to the flow direction of the several different fluid F which is a mixing process object, and makes the fluid F flow through through the mixing process flow path R, and a mixing process Like to do. In addition, the mixing process body 20 can also shape | mold the three-layered plate-like layers 30,40,50 integrally.

  A large number of through holes 31, 41, 51 provided in alignment with the respective plate layers 30, 40, 50 are formed in a regular hexagon of the same shape and the same size, and have six corners.

  Each through-hole 31 having six corners provided in the first plate-like layer 30 has three through-holes in the second plate-like layer 40 in every other three corners clockwise. The three first communication holes 70 are formed by partially communicating one corner portion of each of 41 with the polymerized state. On the other hand, each through-hole 41 having six corners provided in the second plate-like layer 40 is formed in every other three corners in the clockwise direction of the first plate-like layer 30. Three corners of each of the three through holes 31 are partially communicated with each other in a superposed state to form three first communication holes 70. In the present embodiment, the opening area of the three first communication holes 70 is formed to be about one-eighth the opening area of the through hole 31.

  Of the corners of the through-holes 41 provided in the second-layer plate-like layer 40, the corners of the remaining three through-holes 41 that are not in communication with the corners of the through-hole 31 are plate-like in the third layer. Three corners of each of the three through holes 51 of the layer 50 are partially communicated with each other in a polymerized state to form three second communication holes 80. On the other hand, the through holes 51 having six corners provided in the third plate-like layer 50 have three pieces of the second plate-like layer 40 in every other three corners in the clockwise direction. Each of the through holes 41 has one corner portion that is partially communicated with each other in a polymerized state to form three second communication holes 80. In the present embodiment, the opening area of the second communication holes 80 for three is formed to be about one-eighth the size of the opening area of the through hole 31, and the opening area of the second communication hole 80 and the first The opening area of the communication hole 70 is the same.

  The mixing process flow path R includes a front opening recess S1 formed in the first-layer through-hole 31, a first communication hole 70, a space S2 formed in the second-layer through-hole 41, and a second It is formed from the communication hole 80 and the rear surface opening recess S3 formed in the through hole 51 in the third layer. The front opening recess S <b> 1 is formed by closing the rear surface of the first through-hole 31 except for the first communication hole 70 by the front surface portion 42 of the second plate-like layer 40. In the space S2, the front and rear surfaces of the second layer through-hole 41 except for the first and second communication holes 70 and 80, the rear surface portion 33 of the first layer 30 and the third layer 50 of the third layer. The front portion 52 is closed. The rear surface opening recess S3 is formed by closing the front surface of the third layer through-hole 51 with the rear surface portion 43 of the second plate layer 40 except for the second communication hole 80.

  And the mixing process flow path R connects front opening recessed part S1, space part S2, and rear surface opening recessed part S3 via each communicating hole 70,80 toward the downstream side (from the 1st layer to the 3rd layer) from the upstream side. At the same time, it is formed so as to extend in a meandering manner and in a diffusing manner.

  The mixed processing body 20 having the mixing processing flow path R formed as described above is arranged facing the direction in which the fluid F flows in the fluid flow path 60 in which a plurality of different fluids F to be mixed flow. As a result, the fluid F flows into each front opening recess S1 of each mixing treatment channel R.

  The fluid F that has flowed into each front opening recess S1 flows along the front surface portion 42 of the second plate layer 40 that forms a part of each front opening recess S1, and enters each first communication hole 70. Flow into. At this time, the direction in which the fluid F flows into each front opening recess S1 and the direction into which each fluid F flows into each first communication hole 70 is the same direction, but flows along the front surface portion 42 of the plate layer 40. The direction to do is a direction orthogonal to these inflow directions.

  The fluid F divided through the first communication holes 70 flows into the spaces S2 and merges with the fluid F that flows in through the other first communication holes 70. The fluid F that has flowed into each space S2 flows along the front surface portion 52 of the third plate-like layer 50 that forms a part of each space S2, and flows into each second communication hole 80. To do. At this time, the direction in which the fluid F flows into each first communication hole 70 and the direction into which each fluid F flows into each second communication hole 80 are the same direction, but along the front surface portion 52 of the plate-like layer 50. The flowing direction is a direction orthogonal to these flowing directions.

  The fluid F branched through the second communication holes 80 flows into the rear opening recesses S3 and merges with the fluid F flowing in through the other second communication holes 80. The fluid F mixed in the mixing process flow path R in this manner flows out into the fluid flow path 60 from each rear opening concave portion S3.

  As described above, the mixing process flow path R has a direction flowing into each front opening recess S <b> 1, a direction flowing into each first communication hole 70, and a direction flowing into each second communication hole 80. Although the same direction, the direction flowing along the front surface portion 42 of the plate-like layer 40 and the direction flowing along the front surface portion 52 of the plate-like layer 50 are directions orthogonal to these flowing directions, It is bent at a right angle and meanders in a bent shape. The opening areas of the first and second communication holes 70 and 80 are extremely small compared to the opening areas of the through holes 31 and 41. For this reason, the fluid F flowing while meandering in the mixing processing flow path R is given a shearing force caused by the velocity difference between the fluids, and the dispersed phase of the fluid F is steadily refined to the nano level. .

  Note that the shape of the through holes 31, 41, 51 is not limited to a regular hexagon as in the present embodiment, and may be formed in, for example, a rhombus. In this case, two first communication holes 70 and two second communication holes 80 are formed.

  The mixed processing body 20 configured as described above has its axis lined in a direction intersecting (preferably orthogonal) to the axial direction in the fluid flow path 60 in which a plurality of different fluids F to be mixed flow. Deploy. When the fluid F flows into one through hole 31, the fluid F diverts from the three corners of the through hole 31 to the three through holes 41 through the first communication holes 70. The divided fluid F flows and merges in each through hole 41 in a direction orthogonal to the direction in which the fluid F flows into the through hole 31. Then, the joined fluid F re-distributes to the three through holes 51 through the second communication holes 80 that are orthogonal to the three corners of the through hole 41. As described above, the fluid F flowing in from all the through holes 31 similarly repeats the diversion, merging, and re-division continuously in the orthogonal directions in the through holes 31, 41, 51.

  Therefore, the dispersed phase of the fluid F flowing out from the through-hole 51 flows in a meandering manner and a diffusing manner while repeating the diversion and merging, so that it is refined while receiving a shearing force caused by the fluid velocity difference multiple times. Is done. Therefore, micron-order or nanometer-order refinement generation is performed steadily and efficiently. At this time, since the mixing process flow path R is formed by extending in a meandering manner and diffusing from the upstream side to the downstream side (from the first layer to the third layer), the fluid F is mixed and processed in a wide range. Can diffuse. As a result, the dispersed phase of the fluid F is refined to the nano level, and the dispersed phase of the fluid F is made uniform into a continuous phase.

[Explanation of mixing method]
In the mixing processing method according to the present embodiment, the fluid F is divided into a large number of mixing processing flow paths R in the fluid flow path 60 in which a plurality of different fluids F to be mixed flows, and the divided fluid F Is mixed in the mixing process flow path R so that the mixing process is performed. At this time, each mixing processing flow path R is different in position from the inflow start end portion into which the fluid F flows, the midway portion spaced apart from the projected area of the inflow start end portion, and the inflow start end portion. And an outflow end portion from which the fluid F flows out, and is formed to extend in a meandering manner and in a diffusing manner from the inflow start end portion to the outflow end portion. Then, in each mixing process flow path R, the fluid F is mixed, and the fluid F flowing out from the outflow end portion of each mixing process flow path R is merged in the fluid flow path 60.

  More specifically, the mixing treatment method is such that the mixing treatment body 20 is arranged in the fluid flow path 60 in which the fluid F flows, whereby the inflow start end portions of a large number of mixing treatment flow paths R formed in the mixing treatment body 20. The fluid F flows in from (front opening recessed part S1), and the fluid F is divided into many. At this time, each mixing processing channel R is a rear surface that is an outflow end portion from which the fluid F flows out to the outside of the projected area of the through hole 31 that forms the front opening recess S1 that is an inflow start end portion into which the fluid F flows. A second communication hole 80, which is a midway part communicating with the opening recess S3, is disposed and formed so as to extend in a meandering manner and in a diffusing manner from the upstream front opening recess S1 toward the downstream rear opening recess S3. Has been. Therefore, the dispersed phase of the fluid F flowing in a meandering manner in each mixing treatment channel R is refined to the nano level by receiving the shearing force generated by the fluid velocity difference, and forms the front opening recess S1. Most of the outer periphery of the through hole 31 is diffused to be uniform with the continuous phase. As described above, in the mixing processing method of the present embodiment, the fluid F that has flowed in and separated is mixed in each mixing processing flow path R, and then flows out from the rear opening recess S3 of each mixing processing flow path R. They are merged in the fluid flow path 60.

  A plurality of the mixed processing bodies 20 configured as described above are arranged in series in the fluid flow channel 60 at intervals from the upstream side to the downstream side, and the mixing processing by the mixed processing body 20 is continuously performed a plurality of times. Can be repeated. By doing so, the refinement | miniaturization of the dispersed phase of the fluid F and the equalization with a dispersed phase and a continuous phase can be improved.

  According to the mixing treatment method according to the present embodiment, for example, water as a continuous phase and fuel oil as a dispersed phase are mixed to produce an emulsion fuel oil. And oxygen gas as a dispersed phase are mixed to produce high-concentration oxygen water Wo (see FIG. 6) in which the oxygen gas is dissolved in a supersaturated state. Nitrogen water in which nitrogen gas is mixed and dissolved in water, in other words, the DO value (dissolved oxygen amount) is, for example, low concentration oxygen water that is 1 mg / L or less. Alternatively, hot water or water as a continuous phase and carbon dioxide gas as a dispersed phase can be mixed to produce a high-concentration carbonated spring. Here, the high-concentration carbonated spring is obtained by dissolving 1000 ppm or more of carbon dioxide gas (free carbon dioxide) in hot water or water per liter.

[Description of configuration of fluid mixer]
M shown in FIGS. 1-3 is the fluid mixer which concerns on this embodiment. The fluid mixer M includes the above-described mixing processing body 20 inside. By mixing a plurality of different fluids F to be mixed in the fluid mixer M in a pumping state, mixing is performed. The fluid F is refined and uniformed by the processing body 20 and mixed.

  As shown in FIGS. 1 to 3, the fluid mixer M supplies the fluid F introduced from the introduction port 11 to the mixing case 10 provided with the introduction port 11 for introducing a plurality of different fluids F in a pressurized state. A mixing treatment body 20 to be mixed is disposed, and the mixed fluid Fm mixed by the mixing treatment body 20 is led out through the outlet 12 provided in the mixing case 10.

  The mixed processing body 20 is arranged in a state orthogonal to the fluid flow path 60 that communicates the inlet 11 and the outlet 12 in the mixing case 10. Each plate-like layer 30, 40, 50 is formed with a large number of through holes 31, 41, 51 in a penetrating state and aligned vertically and horizontally. The through holes 31 and 41 (41 and 51) between the plate layers 30 and 40 (40 and 50) stacked adjacent to each other communicate with each other and are arranged at different positions.

  In the mixed processing body 20 configured as described above, a plurality of different fluids F flowing in from the through holes 31 of the first plate-like layer 30 on the upstream side are adjacent to the plate-like layer 30 and communicate with each other. In addition, the second plate-like layer 40 arranged at different positions flows in a meandering manner to the respective through-holes 41 of the second plate-like layer 40, and further communicates with each other adjacent to the plate-like layer 40 and arranged at different positions. The mixing process is performed by flowing into each through hole 51 of the third plate-like layer 50 while meandering.

  The mixed processing body 20 uses three plate-like layers 30, 40, 50 as one unit layer, and a plurality of (three in this embodiment) unit layers are arranged along the fluid flow path 60 in the mixing case 10. In addition, they are arranged in series at intervals.

  The mixed processing body 20 is formed by stacking a plurality of unit layers along the fluid flow path 60 in the mixing case 10 with the three plate-like layers 30, 40, 50 as one unit layer. You can also. That is, in this embodiment, the mixed processing body 20 is formed by using the three plate-like layers 30, 40, and 50 as one unit layer. For example, the two unit layers are arranged along the fluid flow path 60. It is also possible to form a single mixed processing body 20 by laminating, and to arrange a plurality of the mixed processing bodies 20 in the mixing case 10 at intervals.

  More specifically, the mixing case 10 closes the case main body 13 formed in a rectangular cylindrical shape, the square plate-shaped front end wall 14 closing the front end face of the case main body 13, and the rear end face of the case main body 13. A rectangular plate-like rear end wall 15 is formed. A circular introduction port 11 is provided at the center of the front end wall 14, and an upstream end of a midway portion of a circulation pipe Jp, which will be described later, is connected to the introduction port 11 to communicate with the fluid F from the introduction port 11 through the circulation pipe Jp. Is introduced in a pressurized state. A circular outlet 12 having the same diameter and the same diameter as the inlet 11 is provided at the center of the rear end wall 15, and the downstream end of the middle part of the circulation pipe Jp is connected to the outlet 12 in a communicating manner. The mixed fluid Fm mixed by the above is led out from the outlet 12 through the circulation pipe Jp.

  The three plate-like layers 30, 40, 50 that form the mixed processing body 20 are each a quadrangular plate shape that is the same shape as the inner peripheral surface shape of the case body 13, and are formed with the same thickness. These plate-like layers 30, 40, 50 are integrally bonded in a laminated state to form the mixed processed body 20. Then, the mixed processing body 20 is accommodated in the case main body 13 so as to be orthogonal to the fluid flow path 60.

  The shape of the mixing case 10 is not limited to that of the present embodiment. For example, the case main body 13 is formed in a cylindrical shape, and the front and rear end walls 14 and 15 are defined as the outer diameter of the case main body 13. It is also possible to form a disk having the same outer diameter, and to form the plate layers 30, 40, 50 into a disk having the same outer diameter as the inner diameter of the case body 13.

  A relay reservoir space Sh is formed between the mixed processing bodies 20, and an inlet port side reservoir space Su is formed between the inlet port 11 and the mixed processing body 20 disposed on the most upstream side. On the other hand, an outlet port side reservoir space Sd is formed between the mixed processing body 20 disposed on the most downstream side and the outlet port 12. Between the pool spaces Su, Sh, Sh, Sd, the mixed processing body 20 is arranged in communication.

  In the present embodiment, a plurality (three in the present embodiment) of mixed processing bodies 20 are arranged in series in the mixing case 10 with a certain interval from the upstream side toward the downstream side. The through holes 31 of the first plate-like layer 30 of each mixing treatment body 20 are arranged to open toward the introduction port 11 side, while the through-holes 51 of the third plate-like layer 50 of each mixing treatment body 20 are The opening is arranged toward the outlet 12 side. The through hole 41 of the second plate-like layer 40 is disposed in communication between the through hole 31 and the through hole 51. The inner peripheral surface of the mixing case 10 and the outer peripheral surface of the mixed processing body 20 are in a sealed state, so that the fluid F flows through the fluid flow path 60 through the through holes 31, 41, 51.

  In the fluid mixer M configured as described above, the three mixed processing bodies 20 having the three plate-like layers 30, 40, 50 as one unit layer are provided in the mixing case 10 along the fluid flow path 60. Are arranged in series at intervals. That is, between the inlet 11 and the outlet 12 in the mixing case 10, between the inlet-side reservoir space Su and the relay reservoir space Sh, between the relay reservoir space Sh and the relay reservoir space Sh, and between the relay Since the mixed processing bodies 20 are arranged to communicate with each other between the reservoir space Sh and the outlet-side reservoir space Sd, the fluid F flowing in the mixing case 10 flows into the reservoir spaces Su, Sh having no flow resistance. , Sh, Sd and the mixed treatment bodies 20 that become the flow resistance are alternately passed in series, so that the pulsating flow is steadily made uniform. And in each pool space Su, Sh, Sd without flow resistance, since the fluid F is rectified, uniformization is promoted.

  In addition, although the flow rate of the fluid F flowing in each of the pool spaces Su, Sh, Sh, Sd having almost no flow resistance is relatively large, the fluid F flowing in each mixing treatment body 20 having a mixing function is In response to flow resistance, the flow rate is relatively reduced. Therefore, the flow velocity of the fluid F flowing in the mixing case 10 is changed (absolutely changed) from large → small → large → small → large, and the flow of the fluid F becomes a steady pulsating flow. As a result, a shearing effect is generated not only when flowing in each mixing treatment body 20 but also when flowing as a pulsating flow in the mixing case 10, and a synergistic shearing effect is obtained.

  Reservoir spaces Su, Sh, Sh, Sd are arranged on the upstream side and the downstream side of each mixed processing body 20, and the through holes 31 of the first plate-like layer 30 of each mixed processing body 20 are introduced. On the other hand, the through hole 51 of the third plate layer 50 of each mixed processing body 20 is opened toward the outlet port 12 side, so that the pressure in the mixing case 10 is increased. Loss can be reduced. For this reason, it is possible to reduce the power consumption of a circulation pump Pa (described later) that pressurizes and supplies the fluid to the fluid mixer M, and to increase the outflow amount (derived amount) of the mixed fluid Fm that is the mixed fluid. (Efficiency) can be achieved.

  In the present embodiment, fluid F is introduced into the mixing case 10 in a pressurized state through the introduction port 11 by the circulation pump Pa, and the fluid F is mixed and mixed by the mixing treatment body 20 disposed in the mixing case 10. The mixed fluid Fm can be led out of the mixing case 10 through the outlet 12.

[Description of Configuration of High-Concentration Carbonate Spring Generation Device as One Form of Gas-Liquid Mixing Processing Device]
A shown in FIG. 4 is a high-concentration carbonated spring generating device (hereinafter also referred to as “generating device”) as one form of the gas-liquid mixing processing device, and the generating device A includes a fluid mixer M. By mixing hot water or water (hereinafter also referred to as “tub water” or the like) W and carbon dioxide filled in the bathtub B by the fluid mixer M, a high-concentration carbonated spring can be generated.

  As shown in FIG. 4, the generator A immerses the both ends of the circulation pipe Jp as the circulation flow path forming pipe in the bathtub hot water W or the like so as to be freely inserted and removed, so that the circulation pipe Jp and the bathtub B The circulation channel Cy can be formed. A circulation pump Pa is disposed in the middle of the circulation pipe Jp. The bathtub hot water W can be circulated through the circulation flow path Cy by the circulation pump Pa. The circulation pipe Jp is provided with the suction portion 1 at one end (upstream side) and the discharge portion 2 at the other end (downstream side), and the suction portion 1 and the discharge portion 2 are connected to the bathtub. It can be freely put in and out of hot water.

  The generation apparatus A is an apparatus that dissolves 1000 ppm or more of carbon dioxide gas (free carbon dioxide) in hot water or water per liter. Here, what dissolved 250 ppm or more of carbon dioxide (free carbon dioxide) in hot water or water per liter is called “carbonated spring”, and what dissolved 1000 ppm or more of carbon dioxide (free carbon dioxide). It is called “high concentration carbonated spring”.

  That is, when producing a high-concentration carbonated spring, the suction part 1 and the discharge part 2 can be placed in a state of being immersed in the bath water W or the like filled in the existing bathtub B. Further, when a high-concentration carbonated spring is not generated, the suction unit 1 and the discharge unit 2 can be placed in a state (accommodated state) in which the bath water or the like W is taken out. The bather can take a bath in the bathtub B during the generation of the high-concentration carbonated spring, or can take a bath in the bathtub B after the high-concentration carbonated spring is generated. By keeping the part 2 in the stowed state, it is possible to take a relaxing bath.

  A carbon dioxide supply part K2 for supplying carbon dioxide via the carbon dioxide supply pipe K1 is connected to the middle part of the circulation pipe Jp so as to be positioned downstream of the circulation pump Pa. As the carbon dioxide supply unit K2, a carbon dioxide generator or a carbon dioxide cylinder that generates carbon dioxide can be used. A carbon dioxide supply amount adjustment valve V1 for adjusting the supply amount of carbon dioxide is provided in the middle of the carbon dioxide supply pipe K1. The carbon dioxide gas generated in the carbon dioxide gas supply unit K2 can be supplied into the circulation pipe Jp through the carbon dioxide gas supply pipe K1 by the amount adjusted by the carbon dioxide supply amount adjustment valve V1.

  A three-way valve V6 is provided in the middle of the carbon dioxide gas supply pipe K1 located downstream of the carbon dioxide supply amount adjusting valve V1, and a compressor Cp is connected to the three-way valve V6 via a compressed air supply pipe K3. Yes. The compressor Cp is able to supply compressed air into the circulation pipe Jp via the compressed air supply pipe K3 and the three-way valve V6 by taking in outside air and entering a compressed state. That is, compressed air or carbon dioxide gas can be selectively supplied to the circulation pipe Jp via the three-way valve V6.

  With this configuration, when bath water W or the like W discharged from the discharge port of the circulation pump Pa is pumped into the circulation pipe Jp, the carbon dioxide supply pipe K1 and the carbon dioxide supply amount adjustment valve are connected to the circulation pipe Jp. Carbon dioxide gas can be supplied into the circulation pipe Jp in a pressurized state from the carbon dioxide supply part K2 connected via V1 and the three-way valve V6. As a result, it is possible to ensure a constant amount of carbon dioxide mixed into the bathtub hot water W through the carbon dioxide supply amount adjusting valve V1. At this time, the supply amount of carbon dioxide gas can be appropriately adjusted via the carbon dioxide supply amount adjustment valve V1.

  Then, before supplying the carbon dioxide gas, the compressed air is supplied in a pressurized state into the circulation pipe Jp through the three-way valve V6 for a certain period of time (for example, 1 minute), so that the air is fined by the fluid mixer M. Thus, the bath water W can be clouded, that is, visualized. Immediately thereafter, carbon dioxide is supplied into the circulation pipe Jp in a pressurized state via the three-way valve V6, so that the carbon dioxide is refined and invisible by the fluid mixer M, and a high-concentration carbonate spring is generated. . In other words, a visualized high-concentration carbonated spring can be generated by adding a refined and invisible carbon dioxide gas to the visualized air bubbles.

  Therefore, the bather can enjoy the high-concentration carbonated spring visually. Moreover, in this embodiment, since the circulation pump Pa with small power consumption can be used, ensuring the production | generation capability of a high concentration carbonated spring, the manufacturing cost and running cost of the production | generation apparatus A can be reduced.

  In the middle part of the circulation pipe Jp, a carbon dioxide gas is refined to a particle size including less than 1 μm, and a fluid mixer M that is uniformly mixed with bath water or the like W to become a gas-liquid mixed fluid is provided with a carbon dioxide gas supply unit. It is located downstream of K2. Sp is a discharge port portion such as a faucet that discharges bathtub water W or the like into the bathtub B, and 3 is a drain pipe connected to the bottom of the bathtub B.

  A pressure regulating valve V2 is provided on the fluid introduction side or the fluid outlet side of the fluid mixer M, and the pressure of the fluid (bath hot water W and carbon dioxide) introduced into the fluid mixer M and the fluid mixer are derived from the fluid mixer. The pressure adjustment valve V2 can adjust the difference from the pressure of the fluid (mixed fluid of bathtub water W and carbon dioxide). In this embodiment, the pressure regulating valve V2 is provided on the fluid outlet side of the fluid mixer M. And the particle size distribution of the carbon dioxide gas bubble refine | miniaturized by flowing in the fluid mixer M can be adjusted suitably with the pressure control valve V2, and the density | concentration of a high concentration carbonated spring is adjusted in a high concentration range. be able to.

  As shown in FIG. 5, the generation apparatus A is provided with a controller C. The controller C includes a CPU (Central Processing Unit), a ROM (Read Only Memory), and a RAM (Random) connected to each other via an internal bus. (Access Memory) and the like. The CPU has a built-in timer, reads a control program stored in the ROM into the RAM, and executes calculations such as the opening of the pressure regulating valve V2 according to the control program.

  As shown in FIG. 5, operation information from the operation unit Op is input to the controller C via the input interface. On the other hand, the controller C that has acquired the operation information performs control according to the control program based on the operation information. Information is generated, and the generated control information is output to each of the carbon dioxide supply amount adjusting valve V1, the pressure adjusting valve V2, the three-way valves V3 to V6, and the circulation pump Pa via the output interface.

  That is, the pressure regulating valve V2 is electrically connected to the output side of the controller C, the operation unit Op is electrically connected to the input side of the controller C, and the operation unit Op is operated via the controller C. The opening degree of the pressure regulating valve V2 is adjusted and controlled in each predetermined time zone. The carbon dioxide supply amount adjustment valve V1 is also electrically connected to the output side of the controller C, and the opening degree of the carbon dioxide supply amount adjustment valve V1 is adjusted and controlled via the controller C by operating the operation unit Op. It is constituted so that.

  And the opening degree of each adjustment valve V1 and V2, the selection of each time zone, the setting of the time width, etc. are preliminarily programmed as a bather's option, and the control program is operated via the operation unit Op. When selected, the controller C executes the selected control program. Each of the three-way valves V3 to V6 is adapted to be switched and controlled by the controller C in accordance with the operation of the operation unit Op. By switching the three-way valve V6, the compressed air or carbon dioxide gas selectively to the circulation pipe Jp is selected. Supply is possible. The time (amount) for which the compressed air is supplied is set by controlling the opening and closing of the three-way valve V6 by the controller C according to the control program.

  The controller C is electrically connected to the electric motor that drives the circulation pump Pa and the electric motor that drives the compressor Cp via an output interface, so that the discharge pressure of the circulation pump Pa (fluid mixer M The pressure on the introduction side) and the drive of the compressor Cp can also be controlled by the controller C. In this case, the discharge pressure of the circulation pump Pa can be set by the operation unit Op, or can be adjusted according to the control program.

  For example, the control program for adjusting the opening degree of the pressure regulating valve V2 can be created so that the first time zone, the second time zone, and the third time zone are successively formed. It is also possible to create the time zone, the second time zone, the third time zone, the first time zone, the second time zone, and the third time zone so as to be formed repeatedly and continuously. Making the order in which the second time zone and the third time zone are formed in reverse is also made so that the order in which the first time zone, the second time zone and the third time zone are formed is irregular. In addition, it is also possible to select at least one time zone from the first to third time zones so as to be selectable. That is, by operating the operation unit Op according to the preference of the bather, it is possible to select each time zone, arbitrarily set the time width, and the like.

  Since the generating device A configured as described above has the first time zone, the second time zone, and the third time zone, the generation of the high-concentration carbonated spring is performed for a short time, and the microscopic effect on the surface of the bather's skin is obtained. The adhesion experience of carbon dioxide gas bubbles in the metric order can be realized within a predetermined short time. For example, a high concentration carbonated spring can be generated in a short time by setting the first time zone immediately before bathing, and the bathing person's skin surface can be set by setting the second time zone and / or the third time zone during bathing. It is also possible to realize the adhesion experience of carbon dioxide bubbles in the micrometer order. Then, the pressure adjustment valve V2 is adjusted and controlled by the controller C via the operation section Op in each predetermined time zone, and the set time width of each time zone can be adjusted, so that the bather's favorite options can be selected. The bather can enjoy the benefits of high-concentration carbonated springs and the enjoyment of bubble bathing.

  A backwash channel Bw is connected to the circulation pipe Jp. That is, the backwash flow path Bw communicates and connects one end portion of the backwash bypass pipe U to the portion of the circulation pipe Jp located immediately upstream of the fluid mixer M via the upstream three-way valve V3. On the other hand, one end portion of the backwash bypass pipe U is connected to the circulation pipe Jp located immediately downstream of the fluid mixer M via the downstream three-way valve V4. A midway part three-way valve V5 is provided in the middle part of the backwash detour pipe U, and the drainage accommodating part H is connected via the midway part three-way valve V5.

  The backwash flow path Bw configured in this way is formed by communicating the circulation pipe Jp and the backwash bypass pipe U via the upstream / downstream three-way valves V3 and V4. Then, the cleaning water is circulated as many times as necessary in the backwash flow path Bw by the circulation pump Pa, so that the wash water flows backward from the downstream side of the fluid mixer M to clean the inside of the fluid mixer M (reversely). Washing). After the back washing treatment, the washing waste water can be discharged to the waste water storage portion H through the midway three-way valve V5 provided in the middle of the backwash bypass pipe U. After that, the circulation flow path Cy is restored by restoring the three-way valves V3, V4, and V5, and the hot water generation process of the high-concentration carbonated spring is resumed by containing the bathtub hot water W in the bathtub B. Can do.

  In the present embodiment, the upstream / downstream three-way valves V3 and V4 are operated to form the backwash flow path Bw, whereby the washing water is caused to flow backward from the downstream side of the fluid mixer M to the fluid mixer M. The inside can be washed (backwashed). After the back washing process, the washing waste water can be discharged to the waste water storage portion H through the midway three-way valve V5. Thereafter, the fluid mixing process can be easily restarted by restoring the three-way valves V3, V4, and V5. Thus, the fluid mixing function of the fluid mixer M can be ensured satisfactorily by appropriately performing the backwash process.

  The circulation pump Pa of the present embodiment employs a land pump, but a submersible pump may be employed instead of the land pump. The production | generation apparatus A which employ | adopted the submersible pump can be arrange | positioned in the state immersed in the bath water etc. W in the bathtub B except the carbon dioxide supply part K2.

  When the submersible pump is adopted as the circulation pump Pa, the hot water in the bathtub B is placed in a state in which the generator A is immersed in the hot water in the bathtub B so that the hot water W in the bathtub B is Can be made. In this case, since only the generator A is disposed in the bathtub hot water W or the like, the circulation pipe Jp can be shortened.

[Description of Configuration of Gas-Liquid Mixing Processing Device as Other Embodiment]
Eq shown in FIG. 6 is a gas-liquid mixing apparatus according to the present embodiment. The gas-liquid mixing processing apparatus Eq is one form of a fluid mixing processing apparatus that mixes and processes different types of fluids. As shown in FIG. 6, the liquid as the fluid F and the gas as the fluid F are circulated through the circulation channel. A gas / liquid mixing process is performed while being circulated by a circulation pump Pa which is a pressure pump through J.

  In the circulation flow path J, a liquid storage tank T that stores liquid, a circulation pump Pa, and a fluid mixer M are sequentially arranged in series, and between the circulation pump Pa and the fluid mixer M. In the fluid mixer M disposed on the downstream side of the gas supply unit Gf by connecting the gas supply unit Gf for supplying the gas to the portion of the circulation channel J located through the gas supply pipe Gp, Gas and liquid are mixed and processed. In the middle of the gas supply pipe Gp, a gas supply amount adjusting valve V7 for adjusting the gas supply amount is provided.

  More specifically, the circulation flow path J includes a suction pipe 91 having a base end connected to the suction port of the circulation pump Pa, and a base end connected to the discharge port of the circulation pump Pa, and a fluid in the middle part. A discharge pipe 92 provided with a mixer M and a liquid storage tank T are formed. A suction filter 93 is attached to the tip (free end) of the suction pipe 91, and the suction filter 93 is disposed in the liquid in the liquid storage tank T. On the other hand, a discharge filter 94 is attached to the distal end (free end) of the discharge pipe 92 and disposed in the liquid storage tank T. The suction pipe 91 and the discharge pipe 92 form the above-described circulation pipe Jp. The fluid mixer M can also be disposed so as to be immersed in the liquid stored in the liquid storage tank T with the outlet pipe 56 removed. By doing so, piping space etc. can be reduced.

  Then, the liquid stored in the liquid storage tank T is sucked through the suction pipe 91 and discharged into the liquid storage tank T through the discharge pipe 92 by the circulation pump Pa, so that the liquid is stored in the liquid storage tank T. The liquid can be circulated through the circulation channel J. At this time, the fluid mixer M is disposed on the downstream side of the gas supply unit Gf connected to the middle part of the discharge pipe 92, and the fluid mixer M includes the gas supplied from the gas supply unit Gf. The liquid sucked from the liquid storage tank T is introduced (supplied). In the fluid mixer M, the gas and the liquid are uniformly mixed, and the gas as the dispersed phase is refined and led out into the liquid storage tank T. As described above, the gas and the liquid are circulated through the circulation channel J a certain number of times or for a certain period of time, thereby miniaturizing the gas to the nano level and further uniformly mixing the gas and the liquid. Can do.

  The gas-liquid mixing processing apparatus Eq according to the present embodiment is configured to introduce the culture water as a liquid and the oxygen gas as a gas into the fluid mixer M to generate the high-concentration oxygen water Wo. And it can also comprise so that the above-mentioned low concentration oxygen water, a high concentration carbonated spring, etc. may be produced | generated by changing the combination of the liquid and gas to introduce | transduce. In addition, the above-described emulsion fuel oil or the like may be generated by configuring a fluid mixing processing device that introduces a combination of other fluids F, that is, liquid and liquid, powder and liquid, and mixes them. it can.

[Description of the structure of the seafood aquaculture system]
Sy shown in FIG. 6 is a seafood aquaculture system according to the present embodiment. The seafood aquaculture system Sy aquacultures the above-described gas-liquid mixing apparatus Eq and seafood (hereinafter also referred to as “breeding”). And an aquaculture tank. The seafood aquaculture system Sy refines the oxygen gas as a dispersed phase to a particle size including less than 1 μm by the gas-liquid mixing apparatus Eq, and uniformly mixes it with the aquaculture water as a continuous phase. The high concentration oxygen water Wo in which oxygen gas is dissolved in a supersaturated state is generated in the culture water, and the generated high concentration oxygen water Wo is supplied to the culture tank.

  Here, the aquaculture water is water, seawater, salt water or the like for culturing seafood. The solubility of oxygen has a correlation that it becomes smaller (difficult to dissolve) when the water temperature becomes higher, and the correlation between the amount of saturated dissolved oxygen in water and the water temperature is already known. Therefore, the dissolved oxygen saturation (%) is determined by measuring the dissolved oxygen (DO) concentration (dissolved oxygen amount) of the high-concentration oxygen water Wo at a predetermined water temperature, and calculating the dissolved oxygen amount as the saturated dissolved oxygen amount. The value obtained by dividing can be calculated by multiplying the divided value by 100. When the dissolved oxygen saturation (%) exceeds 100%, it is called supersaturation. In the seafood aquaculture system Sy of this embodiment, the dissolved oxygen amount (DO value) of the high-concentration oxygen water Wo generated by the gas-liquid mixing apparatus Eq, that is, the high-concentration oxygen water Wo in which the oxygen gas is dissolved in a supersaturated state. As a suitable range, for example, the DO value can be adjusted to a range of 9 mg / L to 20 mg / L.

  The seafood aquaculture system Sy of this embodiment will be specifically described. The seafood aquaculture system Sy stores the aquaculture water in the liquid storage tank T of the gas-liquid mixing apparatus Eq, and the aquaculture water is contained in the aquaculture water. The tip of the water supply flow path Ws to be replenished and the base end of the supply flow path Wf for supplying the high-concentration oxygen water Wo are immersed, and the upstream side of the water supply flow path Ws and the downstream side of the supply flow path Wf Are connected via a connection channel Cf.

  The water supply channel Ws is formed in the water supply pipe 95. The base end portion of the water supply pipe 95 is connected to a water supply portion Wh serving as a water supply source, while a water supply filter 96 is attached to the distal end portion of the water supply pipe 95 and the water supply filter 96 is disposed in the liquid storage tank T. Yes. A water supply pump Pb is disposed in the middle of the water supply pipe 95 so that the aquaculture water can be supplied from the water supply portion Wh into the liquid storage tank T by the water supply pump Pb. The aquaculture water in the liquid storage tank T is mixed with oxygen gas by the gas-liquid mixing apparatus Eq, and has a high concentration oxygen water Wo in which the oxygen gas is dissolved in a supersaturated state, that is, has a desired DO value. High concentration oxygen water Wo is used.

  The supply flow path Wf is formed in the supply pipe 97. A supply filter 98 is attached to the base end of the supply pipe 97, and the supply filter 98 is immersed in the high-concentration oxygen water Wo in the liquid storage tank T, while the distal end of the supply pipe 97 discharges the supply water. Connected to the drainage part Wd. In the middle of the supply pipe 97, a biological filtration device Bf, an aquaculture tank Ft, a sedimentation tank Dp, and a physical filtration device Pf are arranged in series from upstream to downstream. A supply pump Pc is disposed in the portion of the supply pipe 97 located upstream of the biological filtration device Bf, and the high-concentration oxygen water Wo stored in the liquid storage tank T by the supply pump Pc is cultured in the culture tank. Ft can be supplied.

  The connection flow path Cf is formed in the connection pipe 99. One end of the connection pipe 99 is connected to a portion of the supply pipe 97 located on the downstream side of the physical filtration device via the first three-way valve V8, while the other end of the connection pipe 99 is a water supply pump. It is connected to the portion of the water supply pipe 95 located upstream of Pb via a second three-way valve V9. Then, the supply pipe 97 and the connection pipe 99 are shut off (set to a non-communication state) via the first three-way valve V8, so that the wastewater discharged from the settling tank Dp is led to the drainage section Wd. be able to.

  In addition, the supply pipe 97 and the connection pipe 99 are communicated with each other via the first three-way valve V8, and the connection pipe 99 and the water supply pipe 95 are communicated with each other via the second three-way valve V9. The connection pipe 99 → the water supply pipe 95 → the circulation type capable of returning a desired amount in the liquid storage tank T. That is, the amount of water exchange in the liquid storage tank T can be adjusted as appropriate. Whether it is a non-recycling type or a recirculating type is selected according to the type of seafood to be cultivated.

  As described above, the gas-liquid mixing device Eq equipped in the seafood aquaculture system Sy is mixed with the aquaculture water by forming oxygen gas into nano-level bubbles (outer diameter less than 1 μm) and mixing it with the aquaculture water. Then, high-concentration oxygen water Wo in which oxygen gas is dissolved in a supersaturated state is generated.

  More specifically, the gas-liquid mixing processing apparatus Eq uses 90% or more of oxygen gas as a dispersed phase to form nano-level bubbles (outer diameter is less than 1 μm, preferably 100 nm or less; hereinafter “nano-bubbles”). It is also possible to mix them by making them uniform in aquaculture water. In the high-concentration oxygen water Wo generated by the gas-liquid mixing apparatus Eq, oxygen gas is dissolved in a supersaturated state. That is, the dissolved oxygen saturation of the high-concentration oxygen water Wo is set to a supersaturated state (for example, 140%) of 100% or more. The dissolved oxygen saturation of the high-concentration oxygen water Wo when supplied from the gas-liquid mixing apparatus Eq can be adjusted as appropriate. This adjustment is based on the amount of oxygen gas introduced into the gas-liquid mixing apparatus Eq. Is performed in accordance with the type, size, number of individuals, etc. of seafood to be cultivated in the aquaculture tank Ft. In addition, the water temperature of the high-concentration oxygen water Wo, which is the environmental condition of the fish and shellfish to be cultivated, is also detected appropriately to ensure a predetermined water temperature or the like.

  The biological filtration device Bf is particularly required when the fish culture system Sy adopts a circulation system. In other words, the biological filtration device Bf is toxic to the ammonia of the highly toxic fishery products contained in the refluxed high-concentration oxygen water Wo via the nitrite by the action of nitrifying bacteria, which are aerobic bacteria. Biofiltration is performed to oxidize to low nitric acid. As a medium for nitrifying bacteria, an immersion filter medium is used. The size of the container of the biological filtration device Bf that performs the biological filtration treatment and the required amount of filter medium vary depending on the size and number of fish and shellfish cultivated in the aquaculture tank Ft. Therefore, the amount of nitrogen excreted by ammonia and the ammonia oxidation of the filter medium Design appropriately based on speed. In addition, oxygen gas is dissolved in a supersaturated state (for example, 120%) also in the high-concentration oxygen water Wo supplied (refluxed) to the aquaculture tank Ft after being subjected to biological filtration by the biological filtration device Bf. . The adjustment of the dissolved oxygen saturation of the high-concentration oxygen water Wo that is refluxed to the aquaculture tank Ft is performed by adjusting the dissolved oxygen saturation of the high-concentration oxygen water Wo when introduced from the gas-liquid mixing device Eq into the biological filtration device Bf in advance. It can be carried out by appropriately adjusting according to the type, size, number of individuals, etc. of the seafood bred in the aquaculture tank Ft.

  The aquaculture tank Ft is a water tank for cultivating seafood, and is formed by stretching a waterproof sheet such as a plastic sheet in a box shape with an upper surface opening. The culture tank Ft is supplied with the high-concentration oxygen water Wo from the upstream side of the supply flow path Wf so that a certain amount of the high-concentration oxygen water Wo is stored in the culture tank Ft. Then, a predetermined amount of high-concentration oxygen water Wo is always supplied from the upstream side of the supply flow path Wf to the culture tank Ft, and a predetermined amount of high-concentration oxygen water Wo is always overflowed from the culture tank Ft to supply the supply flow path Wf. It is made to discharge to the downstream side. That is, the predetermined amount of high-concentration oxygen water Wo is constantly replaced in the culture tank Ft. D1 is a first drainage channel, and the feces, residual food, drainage, etc. of the seafood when the bottom of the aquaculture tank Ft is cleaned can be discharged to a predetermined location outside the system through the first drainage channel D1.

  The sedimentation tank Dp introduces the high-concentration oxygen water Wo that flows out from the aquaculture tank Ft, and sinks and collects fish dung and residual food with a specific gravity greater than that of the high-concentration oxygen water Wo. The high-concentration oxygen water Wo as the treated water that has been collected and separated is allowed to flow out downstream of the supply flow path Wf.

  The physical filtration device Pf filters high-concentration oxygen water Wo as treated water that has flowed out of the precipitation tank Dp. The physical filtration device Pf is made of a plastic net or a screen-like material such as a porous body, a metal net, or a glass filter. D2 is a second drainage channel, and the physical filtered product can be discharged to a predetermined location outside the system through the second drainage channel D2.

  In the seafood culture system Sy configured as described above, the pumps Pa, Pb, Pc and the valves V7, V8, V9 are electrically connected to the output side of the controller C shown in FIG. Then, each pump Pa, Pb, Pc and each valve V7, V8, V9 can be appropriately controlled by the controller C, and the dissolved oxygen supersaturated high-concentration oxygen water Wo adapted to the type of fish in the aquaculture tank Ft. This makes it possible to realize aquaculture with high growth efficiency of seafood. At this time, oxygen gas, which is a major factor for improving the growth efficiency of seafood, is dissolved in high-concentration oxygen water Wo in a supersaturated state. And oxygen gas is refined | miniaturized to the particle size containing less than 1 micrometer.

  Specifically, the oxygen gas particle size of the high-concentration oxygen water Wo generated by the gas-liquid mixing treatment apparatus Eq of the present embodiment is converted into a nanoparticle analyzer “NanoSight (Nanosite) manufactured by Malvern (Malvern): When measured by “product name”, the mode diameter (mode) was refined to 98.7 nm and the average diameter to 132.4 nm. The DO value of the measured high concentration oxygen water Wo was 13 mg / L.

  The high-concentration oxygen water Wo has a synergistic effect between the oxygen nanobubbles refined to the nano level as described above and the high-concentration dissolved oxygen in which oxygen gas is dissolved in a supersaturated state. That is, oxygen nanobubbles are highly permeable to fish and shellfish, and have the property of being negatively charged, and therefore easily attach to sensory nerve sites that are positively charged. As a result, physiologically active effects such as blood flow promotion, growth promotion and adaptability improvement are expressed through stimulation of sensory nerves. On the other hand, it can be inferred that high-concentration dissolved oxygen also has the same effect as follows. That is, live fish and shellfish produce adenosine triphosphate (ATP) through aerobic glycolysis through respiration. Seafoods that live in high concentrations of dissolved oxygen will produce large amounts of ATP. ATP is a so-called energy storage material, and releases its energy by hydrolysis. Therefore, the fish and shellfish containing ATP at a high concentration have higher vitality, and the growth power, adaptability, and immunity against pathogenic bacteria are greater.

  In the seafood aquaculture system Sy, the aquaculture tank Ft filled with the high-concentration oxygen water Wo can be cultivated to efficiently grow from an initial stage in the growth process to a desired growth stage.

[Explanation of seafood culture method]
In the seafood culture method according to the present embodiment, the fluid F is divided into a number of mixing processing channels R in the fluid channel 60 in which the fluid F composed of aquaculture water and oxygen gas flows, and the divided fluid F In the mixing treatment flow path R, the oxygen gas was refined to a particle size including less than 1 μm, and the mixture was uniformly mixed with the aquaculture water, so that the oxygen gas was dissolved in a supersaturated state in the aquaculture water. The growth of seafood is promoted by culturing seafood in the high-concentration oxygen water Wo.

  More specifically, the seafood aquaculture method is equipped with a fluid mixer M in the gas-liquid mixing device Eq provided in the seafood aquaculture system Sy, so that the oxygen gas can be refined to the nano level and cultured. A high-concentration oxygen water Wo is generated by being dissolved in a supersaturated state in water, and the high-concentration oxygen water Wo is supplied to the aquaculture tank Ft provided in the seafood aquaculture system Sy, and the seafood is cultured in the aquaculture tank Ft. It is.

  In the seafood culture method according to the present embodiment, since the seafood is cultivated with the high-concentration oxygen water Wo in which oxygen gas is refined to the nano level and dissolved in the culture water in a supersaturated state, You can grow a kind. In particular, it is possible to realize breeding (cultivation) capable of steadily increasing and growing the weight of the natural fish and shellfish that have been caught by 2.5 times or more in a short period of 2 to 3 months.

[Example 1]
As Example 1, an experiment for generating a high-concentration carbonated spring was performed using the generating apparatus A configured as described above. As the circulation pump Pa, “Magnet Pump” (trade name) manufactured by Elepon Chemical Machinery Co., Ltd. was used. The suction part 1 and the discharge part 2 of the generator A were immersed in 300 liters of bath water, and the circulation pump Pa was driven. The temperature of the bath water at this time was 41 degreeC. When the carbonate concentration of the bath water after 20 minutes from the start of the circulation pump Pa was measured, it was a high concentration carbonate spring of 1028 ppm. Then, when the driving of the circulation pump Pa was stopped and the carbonate concentration of the bath water was measured after 45 minutes, the carbonate concentration was kept in a high concentration carbonated spring state of 1012 ppm. Moreover, the circulation pump Pa was continuously driven over 2 hours, keeping the temperature of the bath water at 40 ° C to 42 ° C. Also in this case, the carbonic acid concentration was maintained in a high concentration carbonated spring state of 1000 ppm or more.

  From the above, according to the generation device A, normal bath water (for example, a bath having a capacity of 300 liters and a bath water temperature of 41 ° C.) can be steadily converted to a high-concentration carbonated spring in less than 25 minutes. It was found that the state of the high-concentration carbonated spring was maintained for 45 minutes or more even after the device A was stopped.

[Example 2]
As Example 2, an experiment was conducted in which flounder was cultivated (stock raising) using the seafood aquaculture system Sy configured as described above. High-concentration oxygen water Wo generated by the gas-liquid mixing apparatus Eq described above (mode diameter (mode) of oxygen gas particle diameter is 98.7 nm, average diameter is 132.4 nm, DO (dissolved oxygen) value is 13 mg / L) was supplied to the aquaculture tank Ft of the seafood aquaculture system Sy. Then, a test was conducted in which 90 caught natural flounder were subdivided into 30 each and cultivated (cultured) in the aquaculture tank Ft.

  As a result, during the short period of 60 days, the remaining 84 flounder increased in average weight by 2.72 times and average total length by 1.42 times. From this, it was found that the seafood aquaculture system Sy of this embodiment is also effective for growing seafood in a short period of time.

A High-concentration carbonated spring generator M Fluid mixer Cy Circulation flow path Jp Circulation pipe K1 Carbon dioxide supply pipe K2 Carbon dioxide supply section F Fluid Fm Mixed fluid Sy Seafood culture system W Hot water or water (tub hot water, etc.)
Wo High-concentration oxygen water 10 Mixing case 11 Inlet 12 Outlet 20 Mixing treatment body 30 First plate layer 40 Second plate layer 50 Third plate layer

Claims (11)

It has a number of mixing process flow paths that are mixed and processed by the flow of a plurality of different fluids to be mixed,
Each mixing treatment channel is connected to the inflow start end portion into which the fluid flows, the midway portion that is in communication with and arranged around the inflow start end portion, and the midstream portion. An outflow end portion which is arranged at a different position and from which the fluid flows out, and is formed so that the inflowing fluid flows in a meandering manner from the inflow start end portion to the outflow end portion through the midway portion .   Each mixing processing channel according to claim 1, wherein the direction in which the fluid flows into the inflow start end portion and the direction in which the fluid flows into the midway portion are the same direction, and the direction in which these fluids flow in, the inflow The direction in which the fluid flows from the start end to the middle is perpendicular to the flow direction, and the inflowing fluid flows in a meandering manner in a meandering manner from the inflow start end to the outflow end portion fluid. Mixed processing body. The mixed treatment body according to claim 1 or 2 is disposed in a fluid flow path through which a plurality of different fluids to be mixed flows.
As the fluid flows in from the inflow start end portion of each mixing processing channel included in the mixing processing body and the fluid flows in each mixing processing channel, the fluid is mixed and processed.
A mixing process method in which the fluid after the mixing process flows out from the outflow end portion of each mixing process flow path and joins in the fluid flow path.   A fluid mixer comprising a mixing case for forming a fluid flow path for disposing the mixed processing body according to claim 1.   In the mixing case of Claim 4, the fluid mixer which has arrange | positioned the some mixing process body along the fluid flow path, and has arrange | positioned serially at intervals.   In the fluid mixer according to claim 4 or 5, a liquid as a fluid and a liquid or a gas as a fluid are introduced, and the liquid and the liquid or the liquid and the gas are mixed in the fluid mixer. A fluid mixing treatment apparatus configured as described above.   The fluid mixing treatment apparatus according to claim 6, wherein water as a liquid and fuel oil as a liquid are mixed to produce an emulsion fuel oil.   The fluid mixing treatment apparatus according to claim 6, wherein water as a liquid and nitrogen gas as a gas are mixed to generate nitrogen water in which nitrogen gas is dissolved in water.   7. The fluid mixing process according to claim 6, wherein the hot water or water as a liquid and the carbon dioxide gas as a gas are mixed to produce a carbonated spring in which the carbon dioxide gas is dissolved in the hot water or water. apparatus.   The fluid mixing treatment apparatus according to claim 6, wherein water as a liquid and oxygen gas as a gas are mixed to generate oxygen water in which oxygen gas is dissolved in water. A fluid mixing treatment device according to claim 10 and a culture tank for culturing seafood,
A seafood aquaculture system in which oxygen water generated by a fluid mixing treatment device is supplied as aquaculture water to an aquaculture tank.

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