WO2016195116A2 - Buse de traitement de liquide, procédé de traitement de liquide utilisant cette buse, procédé et dispositif de dissolution de gaz - Google Patents

Buse de traitement de liquide, procédé de traitement de liquide utilisant cette buse, procédé et dispositif de dissolution de gaz Download PDF

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WO2016195116A2
WO2016195116A2 PCT/JP2016/067152 JP2016067152W WO2016195116A2 WO 2016195116 A2 WO2016195116 A2 WO 2016195116A2 JP 2016067152 W JP2016067152 W JP 2016067152W WO 2016195116 A2 WO2016195116 A2 WO 2016195116A2
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Prior art keywords
liquid
gas
water
flow
nozzle
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PCT/JP2016/067152
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English (en)
Japanese (ja)
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WO2016195116A3 (fr
Inventor
啓雄 加藤
芝塚　全功
英弘 甲斐
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株式会社ウォーターデザイン
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Publication of WO2016195116A2 publication Critical patent/WO2016195116A2/fr
Publication of WO2016195116A3 publication Critical patent/WO2016195116A3/fr

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    • A—HUMAN NECESSITIES
    • A47—FURNITURE; DOMESTIC ARTICLES OR APPLIANCES; COFFEE MILLS; SPICE MILLS; SUCTION CLEANERS IN GENERAL
    • A47K—SANITARY EQUIPMENT NOT OTHERWISE PROVIDED FOR; TOILET ACCESSORIES
    • A47K3/00—Baths; Douches; Appurtenances therefor
    • A47K3/28—Showers or bathing douches
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F21/00—Dissolving
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/20—Mixing gases with liquids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/40—Static mixers
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/50—Treatment of water, waste water, or sewage by addition or application of a germicide or by oligodynamic treatment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/68—Treatment of water, waste water, or sewage by addition of specified substances, e.g. trace elements, for ameliorating potable water
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone

Definitions

  • the present invention relates to a liquid processing nozzle, and more particularly to a liquid processing nozzle excellent in efficient generation of fine bubbles and gas dissolving ability, and also relates to a liquid processing method, a gas dissolving method and a gas dissolving apparatus realized using the nozzle. is there.
  • microbubbles fine bubbles
  • nanobubbles ultra fine bubbles
  • the two-phase flow swirl method disclosed in Patent Document 1 is intended to reduce the size by entraining the outside air into the swirl flow and forcibly pulverizing, and has a disadvantage that the generation efficiency of nanobubbles with a bubble diameter of less than 1 ⁇ m is poor. There is.
  • a so-called cavitation method is used in which a throttle hole is provided in the water flow path by a venturi or an orifice, and the dissolved air is precipitated as fine bubbles by the pressure reducing effect resulting from Bernoulli's theorem when water passes at a high flow rate.
  • Various microbubble generation mechanisms have been proposed (Patent Documents 2 to 10).
  • a screw member is arranged in the middle of the throttle hole, and the water flow is further accelerated by a gap formed between the screw valleys or the opposing screw members.
  • cavitation efficiency can be improved and nanobubbles can be generated at a higher density.
  • Patent Documents 6 and 7 it is shown by bubble measurement using a laser diffraction particle size meter or the like that bubbles in the nano region can be obtained with high density. Further, when the water flow passes through the collision portion formed by the screw member, the water flow is vigorously stirred by the Karman vortex generated based on the flow detour and the reduced-pressure boiling phenomenon due to cavitation. Therefore, when a gas such as air or ozone is mixed with the water flow and supplied to the nozzle in a mixed phase state, the gas is caught in the strong stirring region formed by the screw member, and can be efficiently dissolved. In addition, the gas phase that could not be dissolved can be refined with a stirring flow and coexist with the dissolved gas in the form of nanobubbles. Such a gas dissolution method is disclosed in Patent Document 8 and Patent Document 9.
  • the problem of the present invention is that it has excellent cavitation ability and thus fine bubble generation ability, and also has a liquid treatment nozzle that clearly outperforms the prior art in terms of performance advantages such as improvement of moisture retention and gas dissolution ability of hair,
  • An object of the present invention is to provide a liquid processing method, a gas dissolving method and a gas dissolving apparatus using the same.
  • the liquid processing nozzle of the present invention is: A nozzle body in which a liquid channel having a liquid inlet at one end and a liquid outlet at the other end is formed; A processing core portion having a collision portion formed so that a plurality of circumferential ridges and valleys that become high flow velocity portions are alternately connected to the outer peripheral surface while projecting from the inner surface of the liquid flow path, In the projection onto the plane orthogonal to the central axis of the liquid flow path, the entire area inside the outer peripheral edge of the projection area of the liquid flow path in the processing core portion is S1, and the projected area area of the collision portion is S2.
  • Distribution cross section St St S1-S2 (unit: mm 2 )
  • the depth h of the valley appearing in the projected outline of the collision portion is secured to 0.2 mm or more
  • the inner periphery of the liquid flow path centering on the projection point of the central axis among the valley points representing the bottom position of the valley portion N is the number of objects located inside the reference circle drawn with a radius equivalent to 70% of the distance to the distance
  • Nc is the number of objects located outside the reference circle
  • the valley depth correction coefficient ⁇ ⁇ 1 when h ⁇ 0.35 mm.
  • the liquid processing method of the present invention is characterized in that a liquid is supplied to the liquid inlet of the liquid processing nozzle of the present invention, and the liquid is brought into contact with the collision portion and flows out from the liquid outlet.
  • a liquid is supplied to the liquid inlet of the liquid processing nozzle of the present invention, and the liquid is brought into contact with the collision portion and flows out from the liquid outlet.
  • the decompression area where the bubbles are deposited is limited to the vicinity of the valley bottom around the collision part, and the high-speed liquid flow passes through the area almost instantaneously. It will be caught in and will generate fine bubbles.
  • cavitation occurs mainly in the valleys of the collision part, and it is important to increase the generation efficiency of microbubbles by bringing at least one of these valleys into contact with the flow. Therefore, increasing the number of screw valleys arranged in the cross section of the processing core portion seems to be effective for improving the generation efficiency of cavitation and, in turn, fine bubbles.
  • the present inventors examined in detail, it turned out that a problem is not so simple and even if the number of troughs is increased mechanically, it does not simply lead to improvement in the generation efficiency of fine bubbles.
  • the present inventors examined the factors by dividing them into the following items. (1) If the formation interval of the valley part of the collision part is made constant, the cross-sectional dimension of the liquid channel in the processing core part is increased, and the protrusion height from the inner surface of the flow path of the collision part is increased. The number of valley points that exist increases.
  • the number of valleys allocated per unit flow rate does not necessarily increase, and in some cases, the flow rate per unit flow rate It is actually possible that the number of valleys will decrease and the cavitation efficiency will decrease instead. Therefore, it is not the absolute number of valley points formed in the processing core part, but the valley point density normalized by the channel cross-sectional area that dominates the cavitation efficiency and hence the fine bubble generation efficiency. This is also closely related to how many valley points the liquid per unit flow rate contacts.
  • the flow velocity in the pipe line has a parabolic distribution in the radial direction in a form that becomes maximum near the center of the cross section of the pipe axis and becomes minimum at the position of the inner wall surface of the pipe. Therefore, the position of the valley in the cross section of the flow path does not contribute to the generation of fine bubbles equivalently, but the valley close to the center of the cross section is easier to secure the flow rate necessary for cavitation, Great contribution. Therefore, when evaluating the number of valley points, it is necessary to consider different weights depending on the distance from the center of the cross section. (3) The valley point located near the cross-sectional center actually contributes effectively to the cavitation effect only when the expected flow velocity is obtained near the cross-sectional center.
  • the number of valley points arranged in the vicinity of the cross-sectional center needs to be evaluated by giving a weight to the distribution area near the cross-sectional center.
  • the formation interval of the valleys formed in the collision part is narrowed, the number of valleys can be increased even with the same flow path cross-sectional area.
  • the depth of the valley portion decreases with the formation interval of the valley portion, there is a concern that the flow restricting effect at the valley bottom is reduced, leading to a reduction in cavitation efficiency. Therefore, when adopting a collision portion having a small valley depth in order to secure a larger number of valley points, it is necessary to evaluate the number of valley points by weighting according to the valley depth.
  • the present inventors have made a number of liquid treatments in which the size of the collision part and the formation depth of the valley part, the number and arrangement of the collision parts, and the flow path cross-sectional dimensions in the processing core part where the collision parts are arranged are variously set.
  • a nozzle was manufactured, and the concentration of fine bubbles, characteristics of the treated liquid containing fine bubbles, and gas dissolution efficiency were examined in detail.
  • the inventors have found that there is a numerical range that is clearly superior to the liquid processing nozzle disclosed in the above-mentioned patent document in terms of the cavitation efficiency and thus the fine bubble generation efficiency. It is a thing. Hereinafter, it demonstrates in order.
  • the cross-sectional areas of the liquid inlet and the liquid outlet are set larger than the total flow cross-sectional area St of the processing core part. This is because if the cross-sectional areas of the liquid inlet and the liquid outlet are smaller than St, the flow rate loss at the liquid inlet and the liquid outlet becomes too large, and a flow velocity for generating sufficient cavitation at the processing core can be secured. Because it disappears.
  • the cross-sectional areas of the liquid inlet and the liquid outlet are set to be larger than the entire area S1 inside the outer peripheral edge of the projection region of the liquid channel in the processing core.
  • circulating a liquid to a liquid processing nozzle about 0.03 MPa to about 0.4 MPa is assumed centering on 0.1 MPa which is a standard water supply pressure.
  • a reference circle is set with a radius corresponding to 70% of the distance from the center axis projection point to the inner peripheral edge of the liquid channel.
  • the ratio of the average flow velocity outside the reference circle to the flow velocity inside the reference circle is approximately 0.38: 1.
  • Number of valleys on the outside Nc 70 Is the number of valleys N inside the reference circle. 70 It has been found that it is appropriate to weight such that the contribution is reduced to about 0.38 times the contribution of.
  • 70% section ratio ⁇ 70 S 70
  • the value of / St ⁇ 100 (%) is 50% if there is no collision part. Therefore, even when the collision part is arranged, the value of the 70% cross-section ratio becomes closer to 50% and becomes closer to the inner side of the reference circle. The trough will receive a higher flow velocity. Therefore, the number N of valleys inside the reference circle 70 For ⁇ 70 We thought it appropriate to weight by the value of / 50.
  • the quadratic expression of h according to the second expression of (1) is 0.5, 0.00 as the values of ⁇ when h is 0.25 mm, 0.3 mm to 0.35 mm, respectively.
  • An empirical rule that 9 to 1.0 is appropriate is approximated by a quadratic equation, and h takes a value other than the above within a relatively narrow numerical range of 0.2 to 0.35 mm. In this case, an appropriate value of ⁇ can be reasonably calculated.
  • the number of valleys Ne weighted by the coefficients optimized for each of the three factors is as shown in the above-described equation (2).
  • the effective valley point density Ne / St obtained by standardizing the effective valley point number Ne with the total flow cross-sectional area St of the processing core portion is an index for objectively quantifying the fine bubble generation capability of the liquid processing nozzle. . And the value is 1.5 / mm 2
  • the effective valley point density is more desirably 1.8 pieces / mm. 2 It is good to secure the above.
  • the axial cross-sectional shape of the liquid channel is preferably circular, for example, but it should be formed as having an elliptical or regular polygonal (square, regular hexagon, regular octagon, etc.) axial cross section unless excessive loss occurs. Is also possible.
  • a plurality of ridges formed in the collision portion can be integrally formed in a spiral shape. In this way, the formation of the peak is facilitated, and the peak is inclined with respect to the flow, so that the flow component crossing the ridge line of the peak increases, and the turbulent flow generation effect accompanying flow separation becomes significant. Therefore, the bubbles can be further miniaturized.
  • the collision part is formed by a screw member whose leg end side protrudes into the flow path
  • the thread of the screw member can be used as a thread part, and the manufacturing is easy.
  • the upper limit of the effective valley point density in the processing core part as described above, it is necessary to secure a valley depth of 0.20 mm or more from the viewpoint of ensuring cavitation efficiency, so it is realistic to increase it indefinitely. It is difficult to do.
  • the depth of the valley portion the flow throttling effect is saturated at 0.35 mm or more as described above, and the valley depth correction coefficient ⁇ is uniformly set to 1.0, so that the valley point density is increased.
  • the upper limit of the depth of the valley portion is limited to about 0.4 mm slightly exceeding 0.35 mm. That is, the depth of the valley portion of the collision portion is preferably set to 0.20 mm or more and 0.40 mm or less, and more preferably 0.25 mm or more and 0.35 mm or less.
  • the cross-sectional shape of the liquid flow path in the processing core portion is circular, and the effective valley point density Ne is 1.5 / mm. 2
  • the inner diameter D should be 2 mm or more and 7 mm or less (preferably 2 mm or more and 6 mm or less), and the total cross-sectional area St is 1.2 mm at this time.
  • the flow rate per one liquid flow path is approximately 0.5 L / min to 26 L / min (desirably Is 0.5 L / min or more and 15 L / min or less), and can form a wide flow spectrum suitable for various applications.
  • the collision part is formed of a screw member having a JIS coarse pitch, the collision part has an outer diameter M of 1.0 mm (the depth of the valley is 0.25 mm) or more and 2.0 mm (the depth of the valley is 0. 0).
  • the collision part in the liquid channel for example, as one of the simplest ones, a form in which the cross section of the channel is bisected and arranged in the diameter direction can be exemplified.
  • This configuration can increase the number of valleys inside the reference circle by, for example, not forming a gap in the vicinity of the center of the cross section or setting the gap interval to a small value even if it is formed. It has the geometric property that the point density decreases rapidly. Therefore, this configuration is effective when it is desired to improve the fine bubble generation efficiency of the liquid processing nozzle with a small flow rate.
  • the inner diameter D of the liquid channel is set to 2 mm to 4.5 mm (preferably 2 mm to 3.5 mm), and the total flow cross section St is 1.2 mm. 2 10 mm or more 2 Below (desirably 1.2mm 2 More than 5mm 2 It is better to set it to the following), and the effective valley point density is 1.5 / mm. 2
  • the flow rate per one liquid flow path is approximately 0.5 L / min to 7.5 L / min. (Desirably 0.5L / min to 5L / min).
  • a set of cross-shaped collision portions respectively formed in the throttle holes can be easily formed by, for example, a plurality of screw members that are screwed so that the front ends protrude into the throttle holes from the wall outer peripheral surface side of the nozzle body.
  • Other than 4 it is possible to select from 3, 5, 6, 7, and 8.
  • the inner diameter D of the liquid flow path is set to 2.5 mm to 7 mm (preferably 2.9 mm to 5.5 mm), and the entire flow is interrupted.
  • the flow rate per one liquid flow path is approximately 2 L / min to 25 L / min (preferably 3 0.5 L / min to 13 L / min).
  • the liquid flow gap can be formed at the center position of the cross section where the tips of the plurality of collision portions gather.
  • the flow at the center of the cross section (center flow) at which the flow velocity is the highest is not easily obstructed by the formation of the liquid circulation gap. 70 As a result, the number of effective valleys increases even with the same number of valleys, and the generation efficiency of fine bubbles is further improved.
  • the 70% cross-sectional ratio ⁇ 70 It is easy to secure 40% or more.
  • the above-mentioned effect due to the formation of the liquid flow gap is particularly remarkable when the front end surface forming the liquid flow gaps of the four collision parts is formed flat and the liquid flow gap is formed in a square shape in the above-described projection. is there.
  • a plurality of collision parts are arranged in the liquid channel in the processing core part, it is also possible to arrange the plurality of collision parts at positions shifted from each other in the axial direction (flow direction) of the liquid channel.
  • a plurality of collision parts can be provided in the flow direction, and the flow can be repeatedly brought into contact with the troughs serving as cavitation points, so that the generation efficiency of microbubbles and the gas dissolution efficiency described later can be improved. Contributes to improvement.
  • a single liquid flow path formed in the nozzle body can be provided.
  • a plurality of nozzles can be connected in parallel by a branch joint or the like. In this way, even if the flow rate per nozzle is small, the entire flow rate can be secured without sacrificing the cavitation effect.
  • a partition that partitions the liquid flow path into an inflow chamber on the liquid inlet side and an outflow chamber on the liquid outlet side, and a plurality of throttles that are formed through the partition and communicate with each other through different paths. It is also possible to form a collision part in a form that includes a hole and the processing core part protrudes from the inner surface of the throttle hole. In other words, when a plurality of nozzles are connected in parallel, the flow path before and after the processing core part where the collision part is arranged is arranged independently for each nozzle.
  • the throttle section is formed, and the flow path sections before and after the throttle section are aggregated into an inflow chamber or an outflow chamber defined by the partition wall and shared by the plurality of throttle sections.
  • the section where the flow path branches into a plurality of systems can be shortened only to the throttle hole formed in the partition wall, which contributes to the prevention of the occurrence of drift due to the length of the branch flow path.
  • the throttle hole has a diameter of a circle equivalent to the sum of the axial cross-sectional areas of the throttle holes, de and the length of the throttle hole is L, and the throttle hole aspect ratio defined by L / de is 3.5.
  • the distance T from the reference point defined at the center position of the projection area of the partition wall to the inner periphery of the plurality of throttle holes is the throttle hole.
  • the length of the throttle hole itself having a small cross-sectional area increases, and even if the sections before and after it are concentrated in the inflow chamber or the outflow chamber, drift may be likely to occur.
  • the plurality of throttle holes formed in the partition wall are formed in the outer peripheral region of the partition wall where the flow velocity is reduced by fluid friction with the inner wall of the tube, drift may easily occur due to the effect of the decrease in the flow velocity. . Therefore, by setting the throttle hole aspect ratio to 3.5 or less as described above, the length of the branch section that causes the drift, that is, the length of the throttle hole in which the collision portion is arranged is sufficiently shortened.
  • the throttle holes are collected at the center of the partition wall portion where the flow velocity is high. In other words, all the throttle holes are gathered and arranged at a position close to the center of the partition wall. As a result, the reduction or non-uniformization of the flow velocity in the throttle hole is suppressed, and drift can be reliably prevented.
  • the value of the aperture hole aspect ratio L / de is desirably 3 or less, and more desirably 2.5 or less.
  • the throttle hole displacement T is desirably 1/2 or less of the inner diameter D of the throttle hole.
  • the value of the throttle hole aspect ratio defined by L / de is a space required for arranging the collision portion. It can be said that it is desirable to set it as small as possible within the range that can be secured on the inner surface of the throttle hole (as will be described later, when the inner surfaces of the inflow chamber and the outflow chamber are tapered surfaces that are reduced in diameter toward the partition wall, There may be a configuration in which the tapered surface is directly connected and the collision portion is formed at the coupling position, but the length of the throttle hole in this case is defined as a value equal to the outer diameter at the protruding proximal end position of the collision portion).
  • the value of the throttle hole displacement T is preferably set as small as possible from the viewpoint of increasing the flow velocity in the throttle hole.
  • the throttle hole may be a hole having a uniform cross section in the flow axis direction or a hole having a non-uniform cross section that is reduced in diameter at the intermediate portion.
  • the axial cross-sectional area of the throttle hole means an axial cross-sectional area at a position where the value is the smallest in the flow axis direction.
  • the plurality of throttle holes can have different axial cross-sectional areas, but in this case, the inner diameter D of the throttle hole means an average value for the plurality of throttle holes.
  • the center position of the projection area of the partition wall means the center when the projection area is circular.
  • the projected area of the partition wall is allowed to be a regular polygonal shape or an elliptical shape from the concept of the invention. In this case, the geometric gravity center position of the projected area is determined as the center position.
  • the remaining section when the length of the section located downstream from the collision portion of the throttle hole (hereinafter referred to as the remaining section) is Lp, and the diameter of a circle equivalent to the sum of the axial sectional areas of the throttle holes is de, Lp / The remaining section aspect ratio defined by de is preferably set to 1.0 or less.
  • the requirement for the proximity arrangement near the center of the partition wall (around the reference point) can be further embodied as follows. That is, in the projection onto the plane orthogonal to the axis of the nozzle body, when St is the area of the circumscribed circle with respect to the inner periphery of the plurality of throttle holes and Sr is the total area of the projection areas of the throttle holes, K ⁇ Sr / St
  • the aperture hole aggregation rate K defined as follows is 0.2 or more. For example, in the case of a set of a plurality of throttle holes having the same size and the same number of formations, the circumscribed circle area increases as the throttle hole displacement T increases.
  • the throttle hole concentration ratio K can be a parameter representing the concentration degree of the throttle holes in the central region of the partition wall, and by setting the K to 0.2 or more, the drift suppression effect becomes more remarkable, and the generation of fine bubbles Contributes to further improvement in efficiency and gas dissolution efficiency.
  • the “circumscribed circle” is defined as a circle circumscribing all of the inner peripheral edges of the plurality of aperture holes (minimum diameter portions) in the projection. If the circle circumscribing the inner periphery of all the apertures cannot be drawn geometrically, “the largest circle that circumscribes the inner periphery of one or more apertures and does not intersect the inner periphery of the remaining apertures. ".
  • the area St of the circumscribed circle is desirably 90% or more of the projected area of the partition wall. Thereby, the area of the flow blocking region formed outside the throttle hole in the partition wall can be reduced, and the flow stagnation and the loss due to the vortex generated in these regions can be reduced.
  • the projected area of the partition wall is set to 90% or more, and the inner peripheral surface of the inflow chamber following the liquid inlet is defined as the partition wall. It is effective to use a tapered surface that decreases in diameter toward the surface.
  • the area St of the circumscribed circle can be made equal to the projected area of the partition wall.
  • a set of cross-shaped collision portions formed in the respective restriction holes can be easily formed by four screw members that are screwed so that the tip protrudes into the restriction hole from the wall outer peripheral surface side of the nozzle body.
  • you try to screw as many as four screw members from the outside of the nozzle body into each of a plurality of throttle holes mistaken geometrical layout may cause interference between the screws, or to a certain throttle hole.
  • the number of throttle holes arranged in this case is preferably 2 to 3, and is optimally 2 in consideration of the ease of nozzle fabrication.
  • the gas dissolving method of the present invention is characterized in that a mixed phase flow of liquid and gas is supplied to the collision portion of the liquid processing nozzle of the present invention, and the gas is discharged from the liquid outlet in a state of being dissolved in the liquid.
  • the gas dissolving apparatus of the present invention includes the liquid processing nozzle of the present invention, and a multiphase flow supply means for supplying a multiphase flow of liquid and gas to a collision portion of the liquid processing nozzle, and converts the gas into a liquid.
  • one of the major factors for creating a strong stirring area in the downstream area of the collision part is the gas dissolved in the liquid to be supplied (Note: The gas introduced from the outside to create a multiphase flow is once dissolved. (Which may also be included) under reduced pressure boiling by cavitation.
  • the stirring / dissolution of the gas introduced from the outside proceeds on a scale exceeding the amount of gas impaired by the boiling under reduced pressure.
  • the gas that could not be dissolved in the liquid remains in the liquid as microbubbles with a very low ascending speed, and various known effects peculiar to microbubbles (for example, cleaning effect, liquid permeability promoting effect, etc.)
  • various known effects peculiar to microbubbles for example, cleaning effect, liquid permeability promoting effect, etc.
  • the same gas coexists in the liquid in the form of both dissolved gas and fine bubbles, when exposed to an atmosphere that does not have a partial pressure of the same type of gas as the dissolved gas, the liquid that contains only the dissolved gas In comparison, the apparent rate of decrease in dissolved gas concentration decreases and the high concentration state is maintained for a longer time.
  • the flow cross-sectional area is reduced due to the arrangement of the collision part in the processing core part, the flow is restricted, and the gas to be dissolved can be sucked in at a relatively low pressure due to the vacuum suction effect by the venturi effect. Since the gas is supplied at a position close to the part, the introduced gas bubbles are quickly pulverized, and there is an advantage that the dissolution efficiency is easily improved.
  • a gas introduction hole that opens to the outer peripheral surface of the nozzle body and communicates with the throttle hole upstream of at least one of the plurality of collision portions is provided in the nozzle body. The formed one can be used.
  • the multiphase flow supply means of the gas dissolving device of the present invention is configured to include a liquid supply unit that supplies liquid to the liquid inlet of the liquid processing nozzle and a gas supply unit that supplies gas to the gas introduction hole. Just keep it.
  • a method is adopted in which gas is allowed to flow in the liquid flow path of the liquid processing nozzle upstream of the processing core portion or the liquid supply path upstream of the liquid inlet of the liquid processing nozzle. It may be adopted.
  • the multiphase flow supply means of the gas dissolving apparatus of the present invention includes a liquid supply unit that supplies liquid to the liquid inlet of the liquid processing nozzle, and a gas that includes a gas supply nozzle independent of the nozzle body connected to the liquid inlet. What is necessary is just to comprise as a thing provided with a supply part. Since the liquid processing nozzle of the present invention is excellent in gas dissolution efficiency, the simplest method can be used to dissolve the gas while flowing the liquid through the liquid processing nozzle for only one pass.
  • the multiphase flow supply means (specifically, the liquid supply unit) of the gas dissolving apparatus of the present invention includes a liquid supply pipe connection unit for connecting a liquid supply pipe connected to an external liquid supply source, Liquid discharge for connecting a gas-dissolved liquid discharge pipe to the liquid outlet side so that the gas-dissolved liquid in which gas is dissolved in one pass by the liquid processing nozzle flows out from the liquid outlet of the liquid processing nozzle What is necessary is just to set it as the structure which provided the pipe connection part. Even with such a simple one-pass dissolution apparatus, the gas can be dissolved at a high concentration by using the liquid treatment nozzle of the present invention.
  • the multiphase flow supply means (specifically, the liquid supply unit) of the gas dissolving apparatus includes a circulation pipe that returns from the liquid storage part that stores the liquid to the liquid storage part via the liquid processing nozzle, and the circulation pipe.
  • a liquid feed pump that circulates and feeds the liquid in the liquid storage part in a form that circulates the liquid processing nozzle while mixing with the gas from the gas supply part and then returns to the liquid storage part can be provided.
  • the type of the liquid in which the gas is dissolved is not particularly limited.
  • water including an aqueous solution and a colloidal solution containing water as a solvent
  • it can.
  • it is an organic liquid such as alcohol (and a diluted product thereof) and fossil fuel (gasoline, light oil, heavy oil, etc.).
  • the type of gas to be dissolved is not limited in the same manner, but may be, for example, oxygen, nitrogen, carbon dioxide, ozone, chlorine, argon, helium, hydrogen, etc., and may be a mixed gas of two or more selected from them. .
  • the mixed phase flow supply means of the gas dissolving apparatus of the present invention is configured to supply a mixed phase flow of carbon dioxide gas and water.
  • Carbon dioxide has a very high solubility in water, and the saturation solubility at 1 atm (normal pressure: 0.1 MPa) in the case of 20 ° C. water reaches 1800 ppm.
  • carbon dioxide gas exceeding 30% of the volume of water must be dissolved at room temperature, and usually a hollow fiber gas separation membrane is reversely used.
  • the gas dissolution unit using the carbon dioxide separation membrane is very expensive and has a short life.
  • the dissolution efficiency of carbon dioxide gas is low, and it is very difficult to dissolve carbon dioxide gas exceeding 30% of the volume flow rate of water in one pass.
  • the liquid processing nozzle of the present invention simply supplies a mixed phase flow of carbon dioxide gas and water to the nozzle. For example, even with a water pressure of about 0.1 MPa or a carbon dioxide gas of about 30% of the volume of water, even one pass Demonstrate the ability to dissolve easily.
  • Standardized water flux Q / St is 0.5L ⁇ mm 2 (Hereinafter, the liquid processing nozzle of the present invention configured in this way is referred to as “standard configuration liquid processing nozzle”).
  • the carbon dioxide flow rate for forming the multiphase flow is Q1 and the water flow rate is Q2
  • the dynamic water pressure on the liquid inlet side is 0.015 MPa to 0.3 MPa
  • the carbon dioxide / water flow ratio Q1 / Q2 is 0.
  • Efficient dissolution of carbon dioxide keeps the pH value of the sodium hypochlorite aqueous solution weakly acidic, for example, around 4.3-6, greatly increasing the concentration of hypochlorous acid in a dissociated state effective for sterilization and disinfection.
  • the fluctuation of the pH value can be reduced by the pH buffering action peculiar to carbonic acid.
  • the phenomenon of undershooting to a low value of 3.5 or less is extremely less likely to occur, thereby suppressing the generation of harmful free chlorine gas. Can do.
  • the sodium hypochlorite aqueous solution is adjusted to have a hypochlorite ion concentration of 10 ppm to 1000 ppm, and the dissolved concentration of carbon dioxide gas is adjusted to 200 ppm to 1500 ppm. Is desirable.
  • the hypochlorite ion concentration is less than 10 ppm, the disinfection action is insufficient, and when it exceeds 1000 ppm, the cost of the sodium hypochlorite aqueous solution is increased.
  • the pH value of the aqueous sodium hypochlorite solution should be stably maintained in the range of 4.3 to 6 where the disinfection effect is optimized by adjusting the dissolution concentration of carbon dioxide gas to 200 ppm to 1500 ppm. Can do.
  • carbon dioxide gas may be dissolved in normal water by the method of the present invention, and a sodium hypochlorite aqueous solution may be added later. In this way, the chemical resistance required especially for the material of the collision part of the liquid processing nozzle can be greatly reduced.
  • the gas dissolving apparatus of the present invention is provided with a sodium hypochlorite aqueous solution supply unit for quantitatively supplying a sodium hypochlorite aqueous solution to the water in which the carbon dioxide gas delivered from the liquid processing nozzle is dissolved.
  • a sodium hypochlorite aqueous solution supply unit for quantitatively supplying a sodium hypochlorite aqueous solution to the water in which the carbon dioxide gas delivered from the liquid processing nozzle is dissolved.
  • the multiphase flow supply means of the gas dissolving apparatus of the present invention is configured to supply a multiphase flow of nitrogen and water.
  • water is deoxygenated in order to prevent corrosion of boilers and piping caused by dissolved oxygen in the water, and one method is nitrogen.
  • the nitrogen-type deoxygenation device removes dissolved oxygen in raw water by bringing the raw water into contact with nitrogen gas, that is, by dissolving the nitrogen gas, in a form replacing nitrogen (referred to as oxygen stripping). .
  • nitrogen gas has a higher melting efficiency, thereby reducing the nitrogen gas flow rate and the circulation time.
  • the oxygen concentration of raw water can be reduced.
  • the nitrogen-dissolved water is brought into contact with the atmosphere again, the re-dissolution of oxygen in the atmosphere starts immediately. Therefore, when the conventional method is used to dissolve and deoxygenate nitrogen, the rate of increase in dissolved oxygen concentration is quite fast. .
  • the introduced nitrogen is contained not only in a dissolved state but also in the form of fine bubbles having a bubble diameter of 1 ⁇ m or less, and the dissolution of nitrogen from the bubbles is caused by oxygen from the atmosphere.
  • the low dissolved oxygen concentration state can be maintained for a long time from several times to several tens of times the conventional one.
  • the dynamic water pressure on the liquid inlet side is 0.015 MPa or more and 0.3 MPa or less when the nitrogen flow rate for forming the multiphase flow having the above configuration is Q1 and the water flow rate is Q2.
  • the dissolved oxygen concentration of water can be reduced to 1 ppm or less by supplying the nitrogen / water flow rate ratio Q1 / Q2 to 0.1 or more and 0.3 or less and supplying the liquid treatment nozzle in one pass or circulating supply.
  • the number of passes for circulating supply means that the pump liquid flow rate is QP (L / min), the circulation time is T (min), and the water volume in the tank is V (L).
  • the multiphase flow supply means of the gas dissolving apparatus of the present invention is configured to supply a multiphase flow of oxygen and water.
  • the dynamic water pressure on the liquid inlet side is 0.015 MPa or more and 0.3 MPa when the hydrogen flow rate for forming the multiphase flow having the above-described configuration is Q1 and the water flow rate is Q2.
  • the hydrogen / water flow ratio Q1 / Q2 is set to 0.1 or more and 0.3 or less, and the dissolved hydrogen concentration of water is set to 0.3 ppm or more and 1.8 ppm or less by supplying the liquid treatment nozzle in one pass or circulation.
  • the gas to be used pure oxygen may be used, or a mixed gas of nitrogen and oxygen such as air may be used.
  • the dissolved oxygen concentration of the resulting water can be made higher than the atmospheric equilibrium dissolved concentration (about 8 ppm) at room temperature and normal pressure.
  • the level near the equilibrium dissolved oxygen concentration with air can be maintained by dissolving air.
  • water in which oxygen is dissolved at a concentration higher than the atmospheric equilibrium dissolved concentration is brought into contact with the atmosphere again, the evaporation of oxygen proceeds until the concentration decreases to the atmospheric equilibrium dissolved concentration.
  • fish or shellfish are raised or cured in water, oxygen is consumed by these fish and shellfish, and the oxygen concentration decreases more rapidly. In these cases, when oxygen is dissolved by the conventional method, the rate of decrease in the dissolved oxygen concentration is considerably fast.
  • the introduced oxygen is contained not only in a dissolved state but also in the form of fine bubbles having a bubble diameter of 1 ⁇ m or less, and oxygen depleted by evaporation or consumption is bubbled.
  • the high dissolved oxygen concentration state can be maintained for a long time, for example, several times to several tens of times the conventional one.
  • the oxygen dissolution efficiency is high, the oxygen supply flow rate required to maintain a high dissolved oxygen concentration state can be greatly reduced even when an oxygen consumer is present.
  • the dynamic water pressure on the liquid inlet side is 0.015 MPa or more and 0.3 MPa when the oxygen flow rate for forming the multiphase flow having the above configuration is Q1 and the water flow rate is Q2.
  • the oxygen / water flow ratio Q1 / Q2 is set to 0.1 or more and 0.3 or less, and the dissolved oxygen concentration of water can be set to 10 ppm or more and 40 ppm or less by supplying the liquid treatment nozzle in one pass or circulation.
  • the fourth case is when hydrogen is dissolved.
  • the multiphase flow supply means of the gas dissolving apparatus of the present invention is configured to supply a multiphase flow of hydrogen and water.
  • Dissolved hydrogen in water exhibits remarkable reducibility, exhibits an antioxidant effect and an inactivating effect of active oxidative species, and there are many products that are presumed to be taken into the body by drinking or ingestion.
  • hydrogen not only has a low saturation solubility in water, but also has the lowest specific gravity among all gases, so the re-evaporation of dissolved hydrogen is significant, so that high-concentration hydrogen water can be obtained. It has been considered that a pressure dissolution process is essential.
  • the gas dissolution method of the present invention when used, high-concentration hydrogen water can be obtained very simply by passing the liquid treatment nozzle as a mixed phase flow of water and hydrogen without performing pressurization. .
  • the introduced hydrogen is contained not only in a dissolved state but also in the form of fine bubbles having a bubble diameter of 1 ⁇ m or less, so that hydrogen depleted by evaporation dissolves from the bubbles.
  • the high dissolved hydrogen concentration state is, for example, several times to several tens of times longer than conventional. Will be able to keep.
  • Hydrogen like nitrogen, has a stripping effect of dissolved oxygen, which can contribute to reducing corrosion of boilers and piping. At this time, dissolved hydrogen exhibits reducibility, and the oxidative corrosion reduction effect is even more remarkable than when nitrogen is used.
  • FIG. 1 is a cross-sectional view and a side view showing a first embodiment of a liquid processing nozzle of the present invention.
  • FIG. 2 is a side view showing details of a processing core part of the liquid processing nozzle of FIG. 1.
  • FIG. 3 is an explanatory diagram illustrating the valley arrangement of FIG. 2.
  • FIG. 4 is an explanatory diagram of the operation of the peaks and valleys in the collision portion.
  • FIG. 5 is a plan view showing the operation of the collision portion.
  • FIG. 6 is a side view showing a first modification of FIG.
  • FIG. 7 is an explanatory diagram showing the valley arrangement of FIG.
  • FIG. 8 is a side view showing a second modification of FIG.
  • FIG. 9 is a side view showing a third modification of FIG. FIG.
  • FIG. 10 is a side view showing a fourth modification of FIG.
  • FIG. 11 is a diagram illustrating a modified example of the formation form of the peaks and valleys.
  • FIG. 12 is a diagram illustrating an example of a unit in which a plurality of liquid processing nozzles are connected in parallel.
  • FIG. 13 is a figure which shows the cross section which shows 2nd embodiment of the liquid processing nozzle of this invention with the A arrow expansion.
  • 14 is a cross-sectional view showing details of a processing core portion of the liquid processing nozzle of FIG.
  • FIG. 15 is an enlarged view of the arrangement in the flow axis direction of the screw member in the processing core portion of FIG. 13.
  • FIG. 16 is a diagram showing a modified arrangement example of FIG. FIG.
  • FIG. 17 is a diagram showing an embodiment in which a part of a plurality of throttle holes are overlapped and integrated.
  • FIG. 18 is a view showing a modification in which four screw members of each throttle hole of the liquid processing nozzle of FIG. 13 are arranged on the same plane.
  • FIG. 19 is a schematic diagram illustrating an example in which three throttle holes are formed in the processing core portion.
  • FIG. 20 is a view showing a modification in the case where the collision portion and the nozzle body are integrally formed by injection molding.
  • FIG. 21 is a diagram showing a modification in which four throttle holes are provided and only one screw member that forms a collision portion is disposed in each throttle hole.
  • FIG. 22 is a view showing a modified example of the arrangement of the screw members in the processing core part.
  • FIG. 23 is a diagram illustrating an example in which no crest is formed on the entire circumference of the collision portion.
  • FIG. 24 is a schematic view showing an example in which the liquid processing nozzle of the present invention is incorporated in the middle of a shower hose.
  • FIG. 25 is a schematic view showing an example in which the liquid treatment nozzle of the present invention is used for toilet flushing of a toilet.
  • FIG. 26 is a side view showing an example in which a gas introduction hole is provided in the liquid processing nozzle of FIG. 1.
  • FIG. 27 is a three-view diagram illustrating an example in which a gas introduction hole is provided in the liquid processing nozzle of FIG. 13.
  • FIG. 28 is a cross-sectional view showing an example of a gas dissolving apparatus that uses the liquid processing nozzle of the present invention to perform dissolution in one pass.
  • FIG. 29 is a schematic diagram showing an example of how to use the gas dissolving apparatus of FIG. 30 is a cross-sectional view showing an example in which a liquid feed pump is incorporated in the gas dissolving apparatus of FIG.
  • FIG. 31 is a schematic diagram showing an example of a method of using the gas dissolving apparatus of FIG.
  • FIG. 32 is a schematic diagram showing an example of an apparatus that uses the liquid processing nozzle of the present invention to perform gas dissolution while pumping liquid.
  • FIG. 33 is a schematic view showing an example in which the apparatus of FIG. 32 is modified so that ozone can be dissolved.
  • FIG. 32 is modified so that ozone can be dissolved.
  • FIG. 34 is a cross-sectional view showing an example in which a mechanism capable of quantitatively supplying a sodium hypochlorite aqueous solution is added to the gas dissolving apparatus of FIG.
  • FIG. 35 is a graph showing a weight reduction curve by heating a human hair sample immersed in the treated water of the present invention together with the treated water of the comparative example.
  • FIG. 36 is a graph showing a weight reduction curve of treated water (Example) of No. 106 in Table 4 together with calculation results of bound water and free water.
  • FIG. 37 is a graph showing a weight reduction curve of treated water (Example) of No. 107 in Table 4 together with calculation results of bound water and free water.
  • FIG. 38 is a graph showing a weight reduction curve of treated water of No. 110 in Table 4 (comparative example) together with calculation results of bound water and free water.
  • FIG. 1 shows a cross section of a liquid processing nozzle and a side surface on the liquid inlet side, showing the first embodiment of the present invention.
  • the liquid processing nozzle 1 includes a nozzle body 2 in which a liquid channel 3 is formed.
  • the nozzle body 2 is formed in a cylindrical shape, and a liquid passage having a circular cross section is formed in the direction of the central axis O thereof.
  • the liquid channel 3 has a liquid inlet 4 at one end (right side in the drawing) and a liquid outlet 5 at the other end, and has a diameter smaller than that of the liquid inlet 4 and the liquid outlet 5 at an intermediate position in the flow direction.
  • a throttle hole 9 is formed.
  • the liquid flow path 3 has an inflow chamber 6 on the liquid inlet 4 side than the throttle hole 9 and an outflow chamber 7 on the liquid outlet 5 side, and a collision portion 10 is provided in a protruding form from the inner surface of the throttle hole 9.
  • the core part CORE is formed.
  • the collision part 10 is a screw member (hereinafter, also referred to as “screw member 10”) whose leg end side protrudes into the flow path, and as a result, a plurality of ridges 11 formed in the collision part.
  • screw member 10 a screw member whose leg end side protrudes into the flow path, and as a result, a plurality of ridges 11 formed in the collision part.
  • the material of the nozzle body 2 is, for example, a resin such as ABS, nylon, polycarbonate, polyacetal, or PTFE, but may be a metal such as stainless steel or brass, or a ceramic such as alumina, and is appropriately selected depending on the application.
  • the material of the screw member 10 is, for example, stainless steel.
  • a heat-resistant alloy such as titanium, hastelloy, or Inconel (both are trade names) having higher corrosion resistance may be used.
  • a ceramic material such as quartz or alumina.
  • the nozzle body 2 made of resin is preferably made of PTFE, for example.
  • the set of collision parts formed in the throttle hole 9 protrudes into the throttle hole 9 from the outer peripheral surface side of the wall part with respect to the screw hole 19 formed in the nozzle body 2. It is formed by four screw members screwed in. The setting between the screw hole 19 and the screw member 10 is fixed by an adhesive or the like. As shown in FIG. 2, a main flow region 21 is formed between the screw member (impact portion) 10 and the inner peripheral surface of the throttle hole 9.
  • a liquid flow gap 15 is formed at the center position of the cross formed by the four collision portions 10.
  • the front end surfaces of the four collision portions 10 forming the liquid flow gap 15 are formed flat, and the liquid flow gap 15 is formed in a square shape in the above-described projection.
  • FIG. 2 the total area inside the outer peripheral edge of the projection region of the liquid flow path in the processing core part, here, the area of the circular axis cross section of the throttle hole 9 in FIG.
  • the total area of the main flow area 21 and the liquid flow gap 15 corresponds to the total flow cross section St.
  • the opening diameters of the liquid inlet 4 and the liquid outlet 5 are larger than the inner diameter of the throttle hole 9. That is, the cross-sectional areas of the liquid inlet 4 and the liquid outlet 5 are set larger than the total flow cross-sectional area St.
  • the inner peripheral surfaces of the inflow chamber 6 and the outflow chamber 7 connected to the throttle hole 9 are tapered portions 13 and 14, respectively.
  • FIG. 3 is the same projection view as FIG. 2, and the reference numerals are omitted (therefore, the reference numerals of the respective parts are the same as those in FIG. 2).
  • the depth h of the valley portion 21 that appears in the projected outline of the screw member (impact portion) 10 is secured to 0.2 mm or more.
  • a circle drawn with a radius corresponding to 70% of the distance from the projection point of the central axis O to the inner peripheral edge of the liquid channel is a reference circle C.
  • the reference circle C 70 N is the number of items located inside (hereinafter referred to as 70% valley score: indicated by ⁇ ) 70 (Pieces), standard circle C 70 Nc is the number of those located outside (hereinafter referred to as 70% complement valley points: indicated by ⁇ ) 70 (Pieces).
  • This water is, for example, tap water, and it is assumed that air is dissolved at a concentration that is in equilibrium with the atmosphere (for example, the oxygen concentration at 20 ° C. (normal temperature) is about 8 ppm).
  • the water flow is first squeezed by the taper portion 13 and the throttle hole 9, and then into a liquid circulation region composed of the main circulation region 21 and the liquid circulation gap 15 of FIG. 2 formed between the screw member 10 and the inner peripheral surface of the throttle hole 9. And passes through the screw member 10 while colliding with it.
  • the flow forms a high speed region in the valley portion 12 and a low speed region in the peak portion 11.
  • the high-speed region of the valley portion 12 becomes a negative pressure region by Bernoulli's theorem, and bubbles FB are generated by cavitation, that is, decompression precipitation of dissolved air.
  • a plurality of valleys are formed on the outer periphery of the screw member 10, and four screw members 10 are arranged in the throttle hole 9, so this reduced pressure deposition occurs simultaneously and frequently in the valleys in the throttle hole 9. Will happen.
  • the reduced pressure precipitation in the valley portion occurs violently, and this is further entangled in the vortex generated when detouring downstream of the screw member 10. Stir vigorously.
  • FIG. 1 The reduced pressure region where the bubbles are deposited is limited to the vicinity of the valley bottom around the collision part 10, and the high-speed liquid flow passes through the region almost instantaneously. Fine bubbles with a bubble diameter of less than 1 ⁇ m are efficiently generated by being caught in the stirring region.
  • the cavitation efficiency, and therefore the fine bubble generation efficiency dominates the valley density obtained by normalizing the absolute number of valleys with the channel cross-sectional area, but the flow velocity in the pipe is maximum near the center of the pipe axis cross section.
  • the parabolic distribution is shown in the radial direction in a shape that becomes the minimum at the inner wall surface position.
  • it is ideal to calculate the flow velocity distribution in the entire cross section by computer simulation using the finite element method, etc., and to determine the weighting factor according to the flow velocity for each valley point position, but it takes a very long time for the simulation. Cost. Therefore, in the present invention, as a simple method, the reference circle C is positioned at a position where the flow velocity is approximately 50% of the maximum value at the center of the cross section in the cross section without the collision portion.
  • the effective valley point density Ne / St obtained by normalizing the effective valley point number Ne with the total flow cross-sectional area St of the processing core portion is an index for objectively quantifying the fine bubble generation capability of the liquid processing nozzle. 1.5 / mm 2 Or more (preferably 1.8 pieces / mm 2 When the above is ensured, the cavitation efficiency and thus the generation efficiency of fine bubbles are remarkably improved.
  • the collision portion may be formed by two screw members 10 screwed in the diameter direction.
  • the liquid flow gap 15 is formed between the tip surfaces of the two screw members 10 and 10.
  • the reference circle C is equivalent to the amount that the tip of the screw member 10 approaches the center of the cross section of the throttle hole 9. 70 It can be seen that a valley point can be arranged at a position closer to the center on the inside. However, when the cross-sectional diameter of the throttle portion 9 increases, the effective valley point density Ne tends to be low, so that it can be said that the total flow cross-sectional area St is relatively small and suitable for a small flow rate liquid processing nozzle.
  • FIGS. 9 and 10 show an example in which the collision portion is constituted by one screw member 110 in the diameter direction.
  • a plurality of crests 111 and troughs 112 (which can be formed by rolling, for example) that are not spirally integrated are closed in the axial direction of the collision parts 120 and 130. You may arrange.
  • the crest 111 is formed in parallel with the plane orthogonal to the axis of the collision part 120
  • the crest 111 is formed in parallel with the plane intersecting with the axis of the collision part 120.
  • a nozzle unit 600 is formed by connecting a plurality of liquid processing nozzles 1 of FIG.
  • both ends of the liquid processing nozzle 1 are formed in a straight shape, and the branch joint 602 is configured such that the branch side connection portion connects the ends of the nozzle with one touch, and the connection portion on the flow unification side is a normal screw joint. It is configured as.
  • the crests and troughs do not necessarily have to be formed all around in the circumferential direction of the collision part, as shown in FIG.
  • FIG. 11 is a three-dimensional conceptual diagram showing an example of the collision part 140 in which the mountain parts 141 are intermittently formed in the circumferential direction.
  • the peak portion 141 is formed as a series of pyramidal protrusions in FIG. 11, there is no change in that a valley portion 142 is formed at the projection side edge of the collision portion 140.
  • the tip of the screw member (impact portion) is not limited to that shown in FIG. 2, and other various forms can be adopted.
  • the tip of the screw member 10 may be formed in a conical shape, and in this case, the liquid flow gap is formed in a cross shape.
  • FIG. 13 shows the cross section of the liquid processing nozzle which shows the 2nd of embodiment of this invention with the enlarged side surface from the axial direction (A arrow) on the liquid inlet side.
  • the liquid processing nozzle 151 includes a nozzle body 2 in which a liquid channel 3 is formed.
  • the nozzle body 2 is formed in a cylindrical shape, and a liquid passage having a circular cross section is formed in the direction of the central axis O thereof.
  • the nozzle body 2 includes a partition wall 8 that divides the liquid flow path 3 into an inflow chamber 6 on the liquid inlet 4 side and an outflow chamber 7 on the liquid outlet 5 side, and an inflow chamber 6 and an outflow chamber formed through the partition wall 8.
  • a processing core portion CORE is formed that includes a plurality of throttle holes 9 that communicate with each other through different paths and a collision portion 10 that protrudes from the inner surface of the throttle hole 9.
  • two throttle holes 9 are formed in the partition wall portion 8 with the same inner diameter so as to be an axial object with respect to the central axis O.
  • the impinging portion 10 is formed in each of the plurality of restricting holes 9 in the processing core portion CORE.
  • Four are arranged in a cross shape surrounding the central axis 9.
  • the effective valley point density Ne defined by the above equation (1) is 1.5 / mm. 2 Or more (preferably 1.8 pieces / mm 2 This is ensured.
  • Each set of collision portions formed in the throttle hole 9 is formed by four screw members that are screwed so that the tip protrudes into the throttle hole 9 from the wall outer peripheral surface side of the nozzle body 2.
  • the screw member 10 is screwed into a screw hole 19 formed through the wall portion of the nozzle body 2, and the screw head lower surface is located in the middle of the screw thrust direction of each screw hole 19.
  • a stepped surface 19r is formed to support the. The formation position of the stepped surface 19r is such that when the screw member 10 is screwed in, the length of the screw leg portion protruding into the throttle hole 9 (that is, the portion serving as the collision portion) forms the liquid flow gap 15. It has been adjusted to be appropriate.
  • the setting between the screw hole 19 and the screw member 10 is fixed by an adhesive or the like.
  • the cylindrical cover 18 which covers the outer peripheral surface of the nozzle main body 2 is attached by adhesion etc. in order to conceal this.
  • the outer peripheral surface of the cover member 18 may be decorated by plating or painting.
  • an inflow side connection portion 16 and an outflow side connection portion 17 are formed on the outer peripheral surfaces of both ends of the nozzle body 2.
  • a set of four screw members 10 incorporated in each throttle hole 9 is arranged between the throttle holes 9. They are arranged at positions shifted from each other in the axial direction. Further, in FIG.
  • the plurality of screw members 10 ⁇ / b> A, 10 ⁇ / b> B, 10 ⁇ / b> C, 10 ⁇ / b> D in the same throttle hole 9 are arranged at positions shifted from each other in the axial direction (flow direction) of the throttle hole 9. .
  • screw member pairs 10A, 10B and 10C, 10D arranged at positions orthogonal to each other on the same plane are different from each other in the flow direction (in FIG.
  • the holes 9 are arranged at positions A and B on the downstream side, and the positions of the lower throttle holes are arranged at positions C and D on the upstream side.
  • each pair of screw members 10 is in contact with the outer peripheral edge of the front end surface (or in a form in which the outer peripheral edge of the front end surface is brought closer through a gap narrower than the liquid flow gap).
  • a square liquid flow gap is formed together with the screw member 10 shown in FIG. 22, and FIG. 22 shows a modification of the arrangement of each screw member pair.
  • the leg end 10b of one screw member is positioned at the center of the throttle hole 9, while the other screw is provided on the peripheral side surface of the leg end 10b.
  • the tip end face 10e of the member is brought into contact (or opposed through a gap), and the leg end 10b on the side located in the center of the throttle hole 9 is placed between the pair in the axial direction of the nozzle body 2 (FIG. 13). They are shifted from each other. In this way, the valley portion of the leg end 10b can be arranged near the center of the throttle hole 9 having a high flow velocity, and the cavitation effect and, consequently, the bubble refining effect can be further enhanced.
  • the aperture 9 is defined as L / de, where de is the diameter of a circle equivalent to the sum of the axial cross-sectional areas of the apertures 9 and L is the length of the aperture 9.
  • the hole aspect ratio is set to 3.5 or less.
  • the throttle hole aspect ratio is L / (d12 + d22) 1/2.
  • the two throttle holes 9 are formed to have a cylindrical surface having the same inner diameter and the same length, and the inner diameter of the two throttle holes 9 is d, and the throttle hole aspect ratio is 0.71 L / d. It is.
  • the value of the aperture hole aspect ratio L / de is desirably 3 or less, and more desirably 2.5 or less.
  • the plurality of throttle holes 9 are arranged around the reference point O so that the displacement (T) is smaller than the inner diameter D of the throttle hole 9.
  • the throttle hole displacement T is desirably 1 ⁇ 2 or less of the inner diameter D of the throttle hole 9.
  • the area of the circumscribed circle 20 with respect to the inner periphery of the plurality of apertures 9 is St and the total area of the projection area of the apertures 9 is Sr in the same projection, K ⁇ Sr / St
  • the defined aperture hole aggregation rate K is 0.2 or more. That is, the liquid processing nozzle 151 satisfies the following conditions.
  • a throttle hole aspect ratio defined by L / de is 3.5 or less;
  • the throttle hole displacement T is smaller than the inner diameter D of the throttle hole 9; -The throttle hole aggregation rate K is 0.2 or more.
  • the area St of the circumscribed circle 20 is 90% or more (100% in FIG. 13) of the projected area of the partition wall 8.
  • the diameter of the circumscribed circle 20 with respect to the throttle hole 9 is narrower than the opening diameter of the liquid inlet 4, and the inner peripheral surface of the inflow chamber 6 following the liquid inlet 4 faces the partition wall portion 8.
  • the tapered surface 13 is reduced in diameter.
  • the length of the section located downstream of the collision portion 10 of the throttle hole 9 (hereinafter referred to as the remaining section) is Lp (average value of Lp2 to Lp4), and the axial break of the throttle hole 9 is performed.
  • the remaining section aspect ratio defined by Lp / de is set to 1.0 or less, where de is the diameter of the circle equivalent to the total area.
  • the inner peripheral surface of the outflow chamber 7 is also a tapered surface 14 that expands toward the liquid outlet 5.
  • the length of the remaining section is zero for the screw member 10A located on the most downstream side, but as shown in FIG. 16, when the remaining section has a non-zero length Lp1 for the screw member 10A,
  • the remaining section length Lp is an average value of Lp1 to Lp4.
  • a plurality of constricted portions are formed in the partition wall portion 8, and the flow path sections before and after the constriction portion are aggregated into the inflow chamber 6 or the outflow chamber 7 defined by the partition wall portion 8.
  • the section where the flow path branches into a plurality of systems is only the throttle holes 9 formed in the partition wall portion 8.
  • the throttle hole aspect ratio defined by L / de (see FIG. 15) is set to 3.5 or less, and the length of the branch section that causes the drift, that is, the collision portion 10 Can be sufficiently shortened.
  • the throttle holes 9 are arranged close to the reference point O to such an extent that the throttle hole displacement T (see FIG.
  • the remaining section aspect ratio (see FIG. 15) defined by Lp / de is set to 1.0 or less.
  • the plurality of throttle holes 9 may be integrally formed so as to partially overlap in a region including the center of the partition wall portion 8 in the above-described projection. It is desirable that the projected area of the overlap region be within 30% of the area of each aperture 9.
  • a set of four screw members 10 arranged in each throttle hole 9 is arranged on the same plane as shown in the sections AA and BB.
  • FIG. 19 shows an example in which three throttle holes 9 are formed in the partition wall portion 8. The positions of the screw members 10 in the flow direction between the three throttle holes 9 are determined to be shifted from each other.
  • the three aperture holes 9 are arranged at positions that form the vertices of the equilateral triangle with a distance larger than the inner diameter of the screw hole 9, and the four screw members 10 having a cross-like arrangement are arranged.
  • the arrangement angle of the set of the screw members 10 is determined so that the screw holes 19 extending toward the pair of the remaining throttle holes 9 pass through the pair of the throttle holes 9 in one throttle hole 9. Yes. Accordingly, all the screw holes 19 can be formed so as to open to the outer peripheral surface of the nozzle body 2 without interfering with the throttle hole 9.
  • FIG. 20 shows an example in which the collision part 10F is formed integrally with the partition part 8 of the nozzle body 2 by injection molding.
  • the material of the collision part 10F is a resin (for example, ABS or nylon) that can be injection-molded, it is necessary to limit the flux within a range where wear due to cavitation is not a problem.
  • the first mold core for forming the inflow chamber so that the central axes of all the collision portions 10F are located on the same plane
  • a mold cavity of the collision portion 10F and the partition wall portion 8 is provided on each tip surface of the second mold core for forming the outflow chamber, and the mold core is molded in a state where the mold cores are abutted with each other using the plane as a dividing surface. You can do that.
  • FIG. 21 shows an example in which four throttle holes 9 are formed in the partition wall portion 8.
  • Each of the four throttle holes 9 has a collision portion formed by screwing one screw member 10 in the diameter direction.
  • the four throttle holes 9 are arranged at positions that form the vertices of squares in the above-described projection, and the central axis O of the nozzle body 2 from the outer peripheral surface side of the nozzle body 2 to each throttle hole 9.
  • the screw member 9 is screwed in the diameter direction of the throttle hole 9 toward.
  • the screw member 10 may be incorporated into the nozzle body 2 by insert molding, and the collision portion may be integrated with the nozzle body 2 by injection molding, as in FIG.
  • 24 may be the liquid processing nozzle 1 of FIG. 1 (the liquid processing nozzle 151 of FIG. 13 or the liquid processing nozzle 51 of FIG. 18) in the middle of a shower hose flow path for a general bathroom (or for a business such as a beauty salon). : The following is the same), and the treated hot water (that is, hot water containing fine bubbles) can be ejected from the shower head.
  • a second hose connection screw for connecting the shower head 401 and the liquid processing nozzle 1 by the outflow side hose 402 as the outflow side connection portion 17 on the liquid outlet 5 side is a thread portion (hereinafter referred to as reference numeral 16).
  • Each part (hereinafter referred to as reference numeral 17) is formed.
  • Each screw portion 16 and 17 is formed as a male screw portion (for example, R1 / 2 to G1 / 2), and the hoses 402 and 405 are connected to the shower head 401, the faucet fittings 403, 404, 406, and 407, respectively.
  • the liquid processing nozzle 1 and the hot / cold water mixing tap 408 are connected. If the hot and cold mixing tap 408 is opened in this state, hot water is supplied to the liquid nozzle 1 and sprayed from the shower head 401. Even when using an existing shower head that does not have the function of generating bubbles, a large amount of fine bubbles can be mixed into the hot water when passing through the liquid processing nozzle 1, increasing the water permeability to the human skin and hair and keeping the moisture. You can enjoy the effects of improving the skin, effectively removing dirt on the scalp and body surface. And even if the nozzle 1 is connected to the middle of the shower hose, it is difficult to be affected by the drift, and the effect of generating fine bubbles can be stably enjoyed. FIG.
  • a flush water supply pipe 103 is connected to the toilet bowl 105 of the toilet, and washing is performed by supplying and flowing flush water 109 along the inner surface of the toilet bowl via the pipe 103.
  • the liquid treatment nozzle 1 of the present invention is provided in the middle of the washing water supply pipe 103, and the washing water in the pipe is supplied to the toilet 105 after becoming the fine bubble-containing water 109 when passing through the liquid treatment nozzle 1.
  • the toilet 105 and the sewage drain pipes 107 and 108 of the toilet 105 are washed.
  • the toilet bowl 105 and the sewage drain pipes 107 and 108 can be kept clean for a long period of time, and adhesion and accumulation of urinary stones and the like are less likely to occur.
  • the toilet 105 is configured as a urinal, and a well-known valve unit 104 with a sensor is provided at a position where the user of the toilet 105 can be detected on the way of the washing water supply pipe 103.
  • Clean water from the water pipe 102 is stored in a wash water tank 101 provided above, and a supply pipe 103 is connected to the wash water tank 101.
  • the sensor-equipped valve unit 104 transitions from the standby state to the cleaning preparation state when the detection state of the user approaching the toilet 105 is continued for a predetermined time or more.
  • FIG. 26 shows an example of a liquid processing nozzle in which the liquid processing nozzle 1 and the processing core unit CORE of FIG.
  • the liquid processing nozzle 171 is opened to the nozzle body 2 on the outer peripheral surface of the nozzle body 2 and, as shown in FIG. 1, introduces gas that communicates with the throttle holes 9 upstream of the plurality of collision portions 10.
  • a hole 28 is formed.
  • the gas forming the mixed phase flow is strongly downstream of the collision unit 10.
  • the factor that forms the strong stirring region SM in the downstream region of the collision unit 10 is reduced-pressure boiling precipitation caused by cavitation of gas originally dissolved in the liquid supplied from the liquid inlet 4.
  • a strong stirring region SM is formed in the downstream region of the collision unit 10 due to the decompression boiling of the dissolved gas, and an infinite number of fine vortex flows FE are formed, and the gas introduced from the gas introduction hole 28 is entrained therein.
  • the stirring and dissolution of gas proceeds on a scale that is orders of magnitude greater than the amount of gas damaged by boiling under reduced pressure. And the gas that could not be dissolved in the liquid also stays in the liquid as microbubbles with very low ascending speed, and various known effects peculiar to microbubbles (for example, cleaning effect, liquid permeability promoting effect, etc.) Will be exhibited according to the type of gas.
  • various known effects peculiar to microbubbles for example, cleaning effect, liquid permeability promoting effect, etc.
  • the same gas coexists in the liquid in the form of both dissolved gas and fine bubbles, when exposed to an atmosphere that does not contain dissolved gas, compared to a liquid in which only dissolved gas exists, apparent dissolved The rate of decrease in gas concentration decreases, and a high concentration state is maintained for a longer time.
  • the structure which does not provide a gas introduction hole in the nozzle main body 2 like the liquid processing nozzle 1 of FIG. 1 is adopted, and gas flows in on the liquid supply path upstream from the liquid inlet 4 to form a multiphase flow. It is good also as a system.
  • the liquid processing nozzle 71 of FIG. 27 has the same configuration as that of FIG. 13, and the screw members 10 arranged at positions orthogonal to each other on the same plane in each throttle hole 9 as shown in FIG. 14. Are arranged at different positions in the flow direction (in the drawing, the positions of A and B on the downstream side for the upper throttle hole 9 and the positions C and D on the upstream side for the lower throttle hole). Yes.
  • the gas introduction hole 28 is the most downstream screw member with respect to the nozzle hole 9 on the upper side of the drawing in which the screw member 10 is attached to the position A or B on the downstream side of the two throttle holes 9.
  • a hole is formed in the radial direction with respect to the wall portion of the nozzle body 2 so as to open upstream from the 10A position.
  • a female screw hole 29 for attaching a gas introduction joint 30 for connecting a gas supply pipe is formed in the opening of the gas introduction hole 28 on the outer peripheral surface side of the nozzle body 2.
  • the gas introduction hole 28 is opened upstream of any of the screw member pairs 10A and 10B.
  • both end portions of the nozzle body 2 of the liquid processing nozzle 71 are a straight inflow side connection portion 26 and an outflow side connection portion 27 for connecting a one-touch fitting (not shown).
  • An intermediate portion in the axial direction connecting the gas introduction joint 30 is a bowl-shaped portion 2 a having a larger diameter than the inflow side connection portion 26 and the outflow side connection portion 27.
  • the throttle hole aspect ratio of the throttle hole 9 formed in the partition wall portion 8 is set to 3.5 or less, and the throttle hole displacement is set to the inner diameter D of the throttle hole 9, just like the nozzle 151 in FIG. It is arranged close to the center of the partition wall 8 (around the reference point) so as to be smaller. Further, the length Lp of the remaining section located downstream from the collision portion 10 of the throttle hole 9 is set so that the aforementioned remaining section aspect ratio is 1.0 or less. In this embodiment, since the gas introduction hole 28 is formed only in one of the two throttle holes 9, the gas phase to be dissolved is supplied to the one throttle hole 9 in a biased manner.
  • the throttle hole aspect ratio is set to 3.5 or less, the flow loss in the entire processing core part CORE is small, and gas is also introduced into the flow F2 in the throttle hole 9 on the gas introduction side. As a result, the flow rate is lower than the flow F1 in the other throttle hole 9, but this is not excessively impaired. And since the remaining section length Lp is small, the introduced gas can be promptly guided to the strong stirring region combined and enlarged downstream of the collision portion 10. That is, the flow from the throttle hole 9 on the gas introduction side can be shared by the outflow chamber 7 in the strong stirring region SM mainly formed on the throttle hole 9 side where the gas is not introduced.
  • the gas introduction holes 28 may be provided for all the throttle holes 9, and in this case, the gas is supplied while being distributed to the respective throttle holes 9 (impact portions 10 thereof). Also here, as shown in FIG. 13, a configuration in which a gas introduction hole is not provided in the nozzle body 2 is adopted, and a gas is caused to flow in a liquid supply path upstream from the liquid inlet 4 to form a multiphase flow. Also good.
  • the gas dissolving method of the present invention the simplest method is to dissolve the gas while flowing the liquid through the liquid processing nozzle for only one pass.
  • FIG. 28 shows an example of the gas dissolving apparatus of the present invention that can embody the method
  • FIG. 29 shows an example of its use.
  • a liquid supply pipe (inflow hose) 405 (a liquid supply unit that forms a mixed phase flow supply means) is connected to an external liquid supply source (for example, a hot-water mixing tap 408 of a water supply or a water heater) (FIG. 27).
  • an external liquid supply source for example, a hot-water mixing tap 408 of a water supply or a water heater
  • a liquid supply pipe connecting portion 202B (having a mounting screw portion 202r) is connected.
  • a liquid processing nozzle 71 shown in FIG. 20 is provided at the tip of the liquid supply pipe connecting portion 202B, and gas is supplied from the liquid outlet to the liquid processing nozzle 71 (or the liquid processing nozzle 171 shown with the aid of FIG. 1).
  • a liquid discharge pipe connecting portion 202A (having a mounting screw portion 202r) for connecting a gas-dissolved liquid discharge pipe (outflow side hose) 408 (FIG. 29) is provided.
  • the gas dissolving apparatus 200 is a simple one-pass, the gas can be dissolved at a high concentration by using the liquid processing nozzle of the present invention.
  • the gas dissolving apparatus 200 includes a main body case 201, and a liquid discharge pipe connecting portion 202A and a liquid supply pipe connecting portion 202B each made of a metal threaded pipe joint are attached to the surface of the main body case 201.
  • An internal liquid pipe 205 is connected to the liquid supply pipe connecting portion 202B, and further, the liquid inlet side of the liquid processing nozzle 71 of FIG. 20 is connected via a flow sensor (flow switch) 204 and a pipe joint 203. Is connected to the liquid discharge pipe connecting portion 202A.
  • a gas supply port joint 211 for connecting a gas supply pipe connected to an external gas supply source is attached to the surface of the main body case 201.
  • the gas introduction joint 30 and the gas supply port joint 211 of the liquid processing nozzle 71 are connected to each other by a gas supply pipe 210.
  • the check valve 207 and the electromagnetic valve 208 are connected from the liquid processing nozzle 71 side.
  • the pressure sensor 209 are arranged in this order.
  • the check valve 207 is for preventing a reverse flow of the liquid flow from the liquid processing nozzle 71 side when the gas supply flow in the gas supply pipe 210 is interrupted, and the electromagnetic valve 208 is in the gas supply pipe 210. This is for switching the gas supply flow between the cutoff state and the supply state.
  • the pressure sensor is for detecting the gas pressure in the gas supply pipe 210 to determine the presence or absence of the gas supply flow.
  • the main body case 201 is further provided with a control board 212 that constitutes a gas supply control means for switching and controlling the power supply circuit 213 and the gas supply flow in the gas supply pipe 210 between a cut-off state and a supply state.
  • a power switch 214 and a power lamp 215 are attached to the surface of the battery.
  • the switch signal SS from the power switch 214 and the detection signals SF and SP from the flow sensor 204 and the pressure sensor 209 are input to the control board 212.
  • An operation signal from the gas flow control operation unit 216 is also input to the control board 212.
  • the power supply circuit 213 receives the drive power supply voltage from the commercial power supply via the power supply cord 217c and the power supply plug 217 (or an AC adapter with a plug), and outputs the drive voltage and signal source voltage of each place to the control board.
  • the control board 212 performs the following control operation. (1) As the power switch 202 is turned on, power supply voltage 215 is detected and the power lamp 215 is turned on.
  • the drive signal SVD is output to the solenoid valve 208 to drive the solenoid valve 208 to the open state (thereby supplying gas to the liquid processing nozzle).
  • Gas is supplied through the pipe 210).
  • the flow sensor 204 outputs a detection signal SF for detecting the liquid flow in the internal liquid pipe 205;
  • the pressure sensor 209 outputs a gas supply pressure detection signal Sp in the gas supply pipe 210, and c.
  • the gas flow control operation unit 216 is in an operation state permitting gas supply.
  • the application destination of the gas dissolving apparatus 200 is a hair washing table such as a beauty salon, and a mode in which carbon dioxide gas is used as gas and hot water for washing hair in which the carbon dioxide gas is dissolved is supplied from the shower 401 is taken as an example.
  • the hot and cold water mixing tap 408 of the water heater and the liquid supply pipe connecting portion 202B of the gas dissolving apparatus 200 are connected by water faucet fittings 406 and 407 via an inflow side hose 405 forming a liquid supply pipe.
  • the shower head 401 and the liquid discharge pipe connecting portion 202A of the gas dissolving apparatus 200 are connected to each other by faucet fittings 403 and 404 through an outflow side hose 402 as a discharge pipe.
  • the pressure reducing valve 411 of the carbon dioxide cylinder 410 serving as a gas supply source and the gas supply port joint 211 of the gas dissolving apparatus 200 are connected by a gas supply tube 412.
  • the gas dissolving apparatus 200 of FIG. 28 operates as follows. When the power switch 214 is turned on and the valve of the carbon dioxide gas cylinder 411 is open, if the hot-water mixing tap 408 is opened in this state, hot water is supplied to the gas melting apparatus 200 and sprayed from the shower head 401. . At this time, the flow sensor 204 in FIG.
  • the pressure sensor 209 detects the carbon dioxide pressure supplied through the gas supply pipe 210.
  • SF and gas supply pressure detection signal SP are input. Therefore, in this state, if the gas flow control operation unit 216 enters an operation state in which the gas supply is permitted, the control board 212 outputs the drive signal SVP to the electromagnetic valve 208, and the electromagnetic valve 208 is opened in response to this, and the hot water is supplied.
  • Carbon dioxide gas is supplied to the flowing liquid processing nozzle 71, and becomes hot water containing dissolved carbon dioxide gas and fine bubbles and is jetted from the shower head 401.
  • the control substrate 212 stops the output of the drive signal SVP, the electromagnetic valve 208 is closed, and the carbon dioxide gas is supplied to the liquid processing nozzle 71. Stops.
  • hot water containing only fine bubbles due to dissolved air is jetted from the shower head 401.
  • the flow rate of water flowing out from the liquid outlet is defined as Q, and the total flow of the processing core section
  • the water flux Q / St normalized by the cross-sectional area St is 0.5 L ⁇ mm.
  • the dynamic water pressure on the coal liquid inlet side is 0.015 MPa or more and 0.3 MPa or less
  • the carbon dioxide / water flow ratio Q1 / Q2 is 0.1 or more and 1. If water and carbon dioxide gas are supplied to the liquid treatment nozzle in one pass with a gas flow rate of 0 or less (however, the gas flow rate is a volumetric flow rate converted to a pressure of 0.1 MPa), the carbon dioxide gas dissolves in water with a dissolution efficiency of 40% or more be able to.
  • the gas flow control operation unit 216 is configured as a foot switch, and the state in which the foot switch 216 is urged by the foot is defined as an operation state that permits gas supply (of course, the reverse is also possible). Good).
  • fine bubbles are mainly used for cleaning effects such as removal of sebum, scalp dirt, and horny plugs that fill pores, as well as to improve the moisture retention of the hair and to prevent rough hands by maintaining the skin's moisture retention. It can be enjoyed in any mode of carbonated fine bubble water and non-carbonated fine bubble water.
  • the check valve 207 should also act to prevent the backflow of water, but many of the check valve type commercially available gas check valves cannot often stop the backflow of low-pressure liquid. It is effective to reliably prevent backflow using (Embodiment 4)
  • the multiphase flow supply means (specifically, the liquid supply unit) includes circulation pipes 422 and 425 that return from the liquid storage unit 430 that stores the liquid to the liquid storage unit 430 via the liquid processing nozzle 71 (FIG. 30), The liquid in the liquid storage unit 430 is mixed with the gas from the gas supply unit 410 through the circulation pipes 422 and 425, and then circulated through the liquid processing nozzle 71 (FIG. 30) and then returned to the liquid storage unit 430.
  • the liquid feed pump 218 is configured to be liquid. Returning to FIG.
  • the configuration of the gas dissolving apparatus 260 will be further described. Since the gas dissolving device 260 has the same configuration as the gas dissolving device 200 of FIG. 28 except that the liquid feed pump 218 is incorporated in the middle of the internal liquid pipe 205, only the differences will be mainly described below. Explanation will be given, and the same components as those in FIG. That is, in this configuration, the internal liquid pipe 205 is divided into a first pipe 205A on the pump inlet side and a second pipe 205B on the pump outlet side, which are connected to the suction side and the discharge side of the liquid feed pump 218, respectively.
  • the liquid feed pump 218 receives a drive voltage from the power supply circuit 213. 28 is omitted, and the control board 212 performs the following control operation.
  • the application destination of the gas dissolving device 260 is a bath, and it is used as a so-called carbonated bath in which carbon dioxide gas is dissolved as a gas while circulating the hot water in the bathtub 430 as a liquid storage unit by the gas dissolving device 260.
  • a return side pipe 425 Connected to the liquid supply pipe connecting portion 202B of the gas dissolving apparatus 260 is a return side pipe 425 that forms part of the above-described circulation pipe that returns the hot water in the bathtub 430 to the gas dissolving apparatus 260.
  • the liquid discharge pipe connection 202A of the gas dissolving device 260 is connected to a discharge side pipe 422 that forms part of a circulation pipe that discharges hot water in which gas has been dissolved by the gas dissolving device 260 into the bathtub 430. ing.
  • the pressure reducing valve 411 of the carbon dioxide cylinder 410 serving as a gas supply source and the gas supply port joint 211 of the gas dissolving device 260 are connected by a gas supply tube 412.
  • FIG. 31 first, hot water is filled in a bathtub 430 from a water heater (not shown). Then, the valve of the carbon dioxide cylinder 411 is opened, and the power switch 214 (FIG. 30) is turned on.
  • the pump 218 starts to operate, sucks hot water in the bathtub 430 through the return side pipe 425, and circulates and flows so as to return to the bathtub 430 through the discharge side pipe 422 while passing through the liquid processing nozzle 71.
  • the flow sensor 204 detects the flow of hot water
  • the pressure sensor 209 detects the carbon dioxide pressure supplied through the gas supply pipe 210.
  • a detection signal SF and a gas supply pressure detection signal Sp are input. Therefore, the control board 212 outputs the drive signal SVP to the solenoid valve 208, the solenoid valve 208 is opened, the carbon dioxide gas is supplied to the liquid processing nozzle 71, and circulates as hot water containing dissolved carbon dioxide gas and fine bubbles. Will continue.
  • FIG. 32 shows an example of an apparatus in which nitrogen or oxygen is dissolved in a liquid while circulating using the liquid processing nozzle of the present invention.
  • raw water (including an aqueous solution and a colloidal solution) 502 is stored in a tank 501, and a gas introduced by an ejector or the like is provided in the raw water supply pipe 51 extending from the tank 501.
  • the unit 219, the liquid feed pump 505, and the liquid processing nozzle 1 of FIG. 1 (the liquid processing nozzle 151 of FIG. 13 and the liquid processing nozzle 51 of FIG. 18 may be provided) in this order.
  • Nitrogen gas is supplied to the gas introduction unit 219 from a nitrogen cylinder 430 as a gas supply source via a pressure reducing valve 411 and a gas supply tube 412.
  • a pipe 507 extending from the tank 501 is formed as a circulation pipe that returns from the tank-side outlet 506 to the tank-side inlet 508 via the gas introduction unit 219, the liquid feed pump 505, and the liquid processing nozzle 1.
  • the liquid feed pump 505 When the liquid feed pump 505 is operated, the raw material water from the tank 501 is supplied with nitrogen gas from the nitrogen cylinder 430 at the gas introduction unit 219 and becomes a mixed phase flow of water / nitrogen gas, and the liquid feed pump 505 generates the nitrogen gas phase.
  • the liquid processing nozzle 1 dissolves the nitrogen gas and pulverizes it into fine bubbles, and returns to the tank 502. Thereafter, while the water 502 in the tank is circulated, the nitrogen gas is continuously dissolved and pulverized into fine bubbles, so that the dissolved concentration of nitrogen gas or the formation concentration of fine bubbles is increased.
  • the circulating water thus obtained is recovered from an outlet 503 having a valve 504 provided in the tank.
  • the raw material water 502 can be dissolved in nitrogen, and thus deoxygenated.
  • the oxygen concentration of the raw water 502 can be reduced with a smaller nitrogen gas flow rate and circulation time.
  • the circulation is continued while supplying nitrogen gas even after the nitrogen concentration reaches the saturation value, the dissolved nitrogen concentration reaches a peak, but the formation concentration of fine bubbles continues to increase.
  • the duration of the dissolved nitrogen concentration is considerably longer than that of water in which nitrogen gas is merely dissolved due to the large amount of fine bubble nitrogen (nitrogen nanobubbles or colloidal nitrogen). As a result, a low dissolved oxygen concentration state can be maintained for a long time.
  • the pump water pressure on the inlet side of the liquid processing nozzle 1 is, for example, 0.015 MPa or more and 0.3 MPa or less, and the nitrogen / water flow rate ratio Q1 / Q2 is set to 0.00.
  • the concentration of dissolved oxygen in water can be 1 ppm or less, for example, from 1 to 0.3, for example, up to about 3 cycles.
  • the raw water 502 can be an alcoholic beverage such as liquor or wine.
  • oxygen dissolved before circulation is discharged by nitrogen substitution, and the alcohol beverage can be prevented from being oxidized.
  • antioxidants such as nitrite that have been added to the antioxidant of beverages.
  • hydrogen can be used instead of nitrogen.
  • the raw water 502 can be dissolved in oxygen.
  • the dissolved oxygen concentration can be significantly increased with a small oxygen gas flow rate and circulation time.
  • the tank 501 it can be used as a fish breeding tank or a ginger for curing live fish (including shellfish), and even if oxygen consumers such as fish and shellfish are present, the oxygen gas flow rate can be reduced. Highly dissolved oxygen concentration can be maintained, which in turn contributes greatly to maintaining the freshness of fish and shellfish, or improving rearing density.
  • the gas pure oxygen may be used, or when using raw water deficient in oxygen from the beginning, a mixed gas of nitrogen and oxygen such as air may be used.
  • the pump water supply pressure on the inlet side of the liquid processing nozzle 1 is set to 0.
  • the oxygen gas source or the nitrogen gas source may be a PSA (Pressure Swing Adsorption) type oxygen concentrator or a nitrogen concentrator, or a liquid for large-scale gas dissolution.
  • the apparatus 560 of FIG. 33 is a modification of the apparatus of FIG. 32 so as to be able to circulate and dissolve ozone (the same reference numerals are given to parts common to the apparatus 550 of FIG. 32, and description thereof is omitted). ).
  • a source of oxygen gas as a raw material here, an oxygen cylinder 440 and an ozone generator (ozonizer) 563 that ozonizes oxygen from the oxygen cylinder are provided, and a gas supply tube 412 is provided.
  • an ozone-containing gas having a concentration of 10 ppm to 100 ppm oxygen that has not been ozonized except for ozone.
  • the raw water can be made into ozone water containing fine bubbles of ozone / oxygen mixture.
  • the pump water supply pressure on the inlet side of the liquid processing nozzle 1 is 0.
  • the dissolved ozone concentration of water is, for example, 1 ppm or more (although there is no limit on the upper limit). For example, 20 ppm or less). Since most of the gas phase in the gas-liquid mixed phase flow to be circulated is oxygen, the waste oxygen / ozone mixture (hereinafter referred to as waste ozone gas) that has not dissolved floats in the tank 501. Therefore, in this embodiment, a waste ozone gas return path 413 is provided to return the recycled waste ozone gas to the ozone generator and reuse it, thereby effectively utilizing oxygen and ozone.
  • dissolved ozone water generally disappears in about several minutes, for example, about 5 ppm due to decomposition of ozone when exposed to the atmosphere (particularly under ultraviolet irradiation).
  • the method of the present invention is used, even when ozone is dissolved, the resulting ozone water contains a large amount of fine bubbles containing ozone. Thereby, the duration of the dissolved ozone concentration when exposed to the atmosphere can be dramatically increased. (Embodiment 5)
  • an aqueous sodium hypochlorite solution can be used as water.
  • the sodium hypochlorite aqueous solution has a hypochlorite ion concentration of 10 ppm or more and 1000 ppm or less (particularly preferably 30 ppm to 200 ppm or less), and a dissolved concentration of carbon dioxide gas is 200 ppm or more and 1500 ppm or less.
  • a sodium hypochlorite aqueous solution having a target concentration is prepared in advance, stored in a tank or the like (not shown), and sent from the liquid inflow pipe connecting portion 202B side of the gas dissolving device 200 of FIG. 28 using an external pump or the like.
  • the solution is dissolved to dissolve carbon dioxide gas, and the pH of the sodium hypochlorite aqueous solution is adjusted to 4.3 to 6, and then taken out from the liquid discharge pipe connecting portion 202A side and used for disinfection.
  • the carbon dioxide gas may be dissolved in normal water using the gas dissolving apparatus 200 of FIG. 28, and the sodium hypochlorite aqueous solution may be added later.
  • a sodium hypochlorite aqueous solution whose pH has been adjusted by adding a sodium hypochlorite aqueous solution having a concentration higher than the target concentration to the water in which the carbon dioxide gas is dissolved, taken out from the liquid discharge pipe connecting portion 202A side.
  • An apparatus 270 in FIG. 34 shows an example, and a sodium hypochlorite aqueous solution supply unit 310 includes an aqueous solution tank 311 for holding a sodium hypochlorite aqueous solution and an aqueous solution incorporated downstream of the liquid processing nozzle 71.
  • a supply nozzle 317 and a liquid feed pump 312 for quantitatively feeding the sodium hypochlorite aqueous solution in the aqueous solution tank 311 to the aqueous solution supply nozzle 317 are provided.
  • the aqueous solution supply nozzle 317 is configured by using a tee joint (which may be a venturi-type ejector), a liquid introduction joint 330 is attached to the branch opening, and the liquid supply pipe 314 from the aqueous solution tank 311 is fed. It is attached to a liquid introduction joint 330 via a liquid pump 312.
  • the rest of the configuration and basic operation are the same as in FIG. 28, and the same reference numerals as in FIG. 26 are assigned to the common components.
  • the pump 218 When the power switch 214 is turned on, the pump 218 operates, and the carbon dioxide gas is dissolved by the liquid processing nozzle 71 in the same operation as in FIG. 29 while taking the raw water from the liquid inflow pipe connecting portion 202B side.
  • the liquid feed pump 312 operates, and a sodium hypochlorite aqueous solution is quantitatively injected from the aqueous solution supply nozzle 317 downstream of the liquid processing nozzle 71.
  • the flow rate of the liquid feed pump 312 depends on the concentration of the sodium hypochlorite aqueous solution to be added and the flow rate of the raw material water fed by the pump 218, and the hypochlorite ion concentration obtained on the liquid discharge pipe connecting portion 202A side is It is set to be 10 ppm or more and 1000 ppm or less. It is also possible to configure so that the supply / stop of carbon dioxide gas can be switched manually or automatically during the injection of the sodium hypochlorite aqueous solution. In FIG.
  • a changeover switch 331 is added, and the control board 201 receiving the changeover signal Sc opens and closes the electromagnetic valve 208 in the same manner as the operation of the foot switch 216 in the apparatus 200 of FIG. Switch between carbon dioxide supply and stop.
  • weakly acidic hypochlorous acid water having a high sterilization property is obtained from the liquid discharge pipe connecting portion 202A in the carbon dioxide gas supply mode, and alkaline hypochlorous acid having a high detergency in the carbon dioxide gas stop mode.
  • a sodium aqueous solution that is, a solution obtained by simply diluting the sodium hypochlorite water in the tank 311 with the raw water supplied by the pump 218) is obtained.
  • the mode is switched to the carbon dioxide gas supply mode to weakly acidic hypochlorous acid. It can contribute to the maintenance of a higher level of hygiene, such as sterilization with water.
  • Example 1 As the nozzle configuration, the nozzle 1 shown in FIG. 1 was used for the test in which gas was not dissolved, and the nozzle 171 (FIG. 26) shown in FIG. 1 was used for the test in which gas was dissolved.
  • the gas introduction hole 28 has an inner diameter of ⁇ 2 mm.
  • the material of the nozzle body 2 is ABS resin, the inner diameter of the liquid inlet 4 and the liquid outlet 5 is ⁇ 14 mm, and the lengths of the inflow chamber 6 and the outflow chamber 7 in the flow direction are 30 mm.
  • the length of the throttle hole 9 was set to 5.3 mm, and the inner diameter D of the throttle hole 9 was set to various values of ⁇ 2.1 to ⁇ 8.0 mm.
  • the screw members were arranged in the form shown in FIG. 2 (Tables 3 to 6) and in the form shown in FIG. 6 (Tables 1 and 2: However, no liquid flow gap was formed). All of the screw members were of various dimensions having a screw outer diameter of M1.0 to M2.0 and a thread valley depth of 0.25 to 0.4 mm.
  • the total flow cross-sectional area St was set to various values of 1.23 to 40.27 mm 2 in combination with the throttle hole inner diameter D. Then, a photograph image of the screw layout in the aperture hole as shown in FIG. 3 and FIG.
  • the total distribution cross section St is calculated based on the number of pixels in the distribution region, and the valley point is referenced on the image. Counted separately inside and outside the circle.
  • the total valley score is Nt
  • the 70% valley score inside the reference circle is N 70 .
  • the laser diffraction particle size distribution measuring device makes a laser light beam incident on a measurement cell at a certain angle, and a three-dimensional scattering distribution of light scattering generated at the gas-liquid interface according to the refractive index difference between the bubble and water and the bubble diameter.
  • a three-dimensional scattering distribution of light scattering generated at the gas-liquid interface according to the refractive index difference between the bubble and water and the bubble diameter.
  • scattered light intensity for each angle is detected by an individual photodetector, and information related to the bubble diameter distribution is obtained from the detected intensity distribution of each sensor.
  • the obtained distribution is a volume bubble size distribution, but the software attached to the apparatus converts the bubble into a spherical shape by converting it into a spherical shape, and the number average bubble size calculated based on this is displayed.
  • the measuring device is accompanied by a function for measuring the absorbance of the laser light passing through the cell, and the higher the absorbance, the higher the concentration of bubbles in the cell.
  • the absorbance value is a relative value, and information on the absolute value of the bubble concentration cannot be obtained. However, it is possible to relatively compare the bubble concentrations of a plurality of samples to be measured simultaneously. The absorbance value is also displayed together (note that the maximum absorbance displayed by the device is 0.2).
  • pure oxygen gas was supplied from the gas introduction part 219 while adjusting the supply pressure to 0.3 MPa and the oxygen gas flow rate to be 20% of the circulation flow rate in terms of normal pressure, thereby dissolving oxygen gas.
  • the circulation time was determined to be equal to the time obtained by dividing the volume of purified water in the tank by the pump circulation flow rate. After the circulation was stopped, 5 L of water dissolved with oxygen gas was immediately taken from a outlet 503 into a resin beaker having an opening diameter of 18 cm, and dissolved oxygen was measured with an optical dissolved oxygen meter.
  • the obtained results will be described.
  • the inner diameter D of the liquid flow path is set to approximately 2 mm to 4.5 mm (preferably 2 mm to 3.5 mm), and all While setting the flow sectional area St to 1.2 mm 2 to 10 mm 2 (preferably 1.2 mm 2 to 5 mm 2 ), the outer diameter of the screw member is M1.2 to M1.6, and the valley depth is 0.25 mm.
  • the value is selected to be 0.35 mm or less, the value of the effective valley point density is remarkably increased, and it can be seen that better fine bubble generation efficiency can be achieved.
  • the inner diameter D of the liquid flow path is set to about 2.5 mm to 7 mm (preferably 2.9 mm to 5.5 mm).
  • the outer diameter of the screw member is M1.2 to M1.6
  • the valley depth is 0.25 mm.
  • the value is selected to be 0.35 mm or less, the value of the effective valley point density Ne is remarkably increased, and better microbubble generation efficiency can be achieved. It is clear that the fine bubble generation efficiency at a large flow rate is improved as compared with the nozzle of FIG.
  • FIG. 35 shows a weight loss curve associated with moisture evaporation of the hair sample for (Example: effective valley point density 2.2) and No. 110 (comparative example: effective valley point density 1.2).
  • FIG. 36 to FIG. 38 individually show the weight reduction curves of the respective nozzles. It can be seen that the rate of water evaporation is clearly slower as the water is treated with a nozzle having a higher effective valley point density.
  • the form of the weight reduction curve reflects the binding state between the protein polymer constituting the hair and water.
  • the rate of weight loss associated with the evaporation of the moisture is not constant. It is known to exhibit a behavior following a characteristic cusp-shaped curve in which the rate of weight reduction gradually decreases. If the evaporation behavior of the moisture contained in the hair is governed by the diffusion of water molecules in the radial direction of the hair, the weight reduction curve should have a smooth curve shape according to the compensation function. However, as shown in FIGS. 36 to 38, the weight reduction curve actually obtained by the measurement includes a straight section where the evaporation rate becomes substantially constant with time.
  • the hydrogen atom contained in the water molecule is positively polarized and charged with a force much higher than the intermolecular force against the protein polymer chain. That is, the water molecules constituting the antifreeze water are in a semi-chemically integrated state with respect to the protein polymer chain, and therefore do not evaporate at a temperature below the boiling point of water. Bound water penetrates deep into the protein structure and controls various factors such as appearance and feel that create a good hair condition, such as moisture, gloss, softness, suppleness, and the way of hands and brushes. It is thought that there is.
  • the method for estimating the presence and content of water in the protein as described above from the weight loss curve accompanying water evaporation retained by the protein has been proposed in Non-Patent Document 1 for a long time.
  • the weight content of free water and bound water is zero for each straight section. It can be calculated as the difference of the weight axis intercept extrapolated to. 36 to 38 also show the results of calculating the contents of bound water and free water in the hair from the weight reduction curves at each nozzle. Tables 1 to 6 show the weight content (Wb, Wf) of the bound water and free water calculated for the treated water of each nozzle and the value of the total Wb + Wf. From this result, it can be understood that the weight ratio of the bound water when it is applied to the hair increases as the treated water is produced by the nozzle having a higher effective valley point density.
  • the total weight content of bound water and free water is constant between about 25-30% regardless of the effective valley point density of the nozzle used. It is that you are. This means that the amount of water penetrating into the hair is almost constant, but water treated with the present invention so as to increase the generation efficiency of fine bubbles in particular increases the amount of water converted to bound water. is doing. This also means that the amount of free water that creates the feeling of “wetting” is reduced, which is consistent with the body sensation of the subject who feels that the drying time can be shortened when drying the dryer. Conventionally, it has been considered that the improvement in the moisture retention of the hair is brought about by an increase in the absolute amount of moisture penetrating into the hair.
  • Liquid treatment nozzle 1, 51, 71, 171 Liquid treatment nozzle 2 Nozzle body O Center axis 3 Liquid flow path 4 Liquid inlet 5 Liquid outlet 6 Inflow chamber 7 Outflow chamber 8 Partition portion 9 Restriction hole 10 Colliding portion (screw member) CORE processing core part 11 mountain part 12 valley part 15 liquid distribution gap 16 inflow side connection part (screw part) 17 Outflow side connection (screw) 20 circumscribed circle 28 gas introduction hole 200,260,270,500,550,560 gas dissolving apparatus

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  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Organic Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • Environmental & Geological Engineering (AREA)
  • Engineering & Computer Science (AREA)
  • Hydrology & Water Resources (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Public Health (AREA)
  • Dispersion Chemistry (AREA)
  • General Health & Medical Sciences (AREA)
  • Epidemiology (AREA)
  • Medicinal Chemistry (AREA)
  • Nozzles (AREA)

Abstract

L'invention concerne une buse de traitement liquide qui permet de produire de manière très efficace des bulles microscopiques et qui présente une excellente capacité de dissolution de gaz.　La buse de traitement de liquide (1) est pourvue : d'un corps de buse (2), comprenant un passage de liquide (3) formé à l'intérieur de celui-ci; et une partie centrale de traitement (partie centrale) comprenant des saillies (10) qui font saillie à partir de la surface intérieure du passage de liquide (3) et qui comportent, formées dans la direction circonférentielle et sur la surface périphérique externe de celles-ci, une pluralité de parties crêtes contiguës (11) alternant avec des parties vallées (12), les parties vallées (12) servant de parties à débit d'écoulement élevé. La densité de points de vallées effective (Ne-St) normalisée par toute la zone de section transversale d'écoulement (St) est maintenue à au moins 1,5 parties/mm2. Pour les saillies (10), la densité de points de vallées effective (Ne/St), qui est le nombre (Ne) de points de vallées effectif normalisé par toute la surface de section transversale d'écoulement (St), est maintenue à au moins 1,5 parties/mm2.
PCT/JP2016/067152 2015-06-02 2016-06-01 Buse de traitement de liquide, procédé de traitement de liquide utilisant cette buse, procédé et dispositif de dissolution de gaz WO2016195116A2 (fr)

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JP2018065979A (ja) * 2016-10-19 2018-04-26 株式会社ウォーターデザイン 食用油の製造方法及び製造装置
JP2018178538A (ja) * 2017-04-13 2018-11-15 東芝ライフスタイル株式会社 水洗便器装置、洗浄水タンク装置、及び局部洗浄装置
CN110874513A (zh) * 2018-08-13 2020-03-10 中石化石油工程技术服务有限公司 一种气液混合器注气孔设计方法及装置
JP2020189286A (ja) * 2019-05-22 2020-11-26 啓雄 加藤 液体処理ノズル
JP2020189274A (ja) * 2019-05-22 2020-11-26 株式会社リスニ 液体処理装置
JP2021019509A (ja) * 2019-07-24 2021-02-18 株式会社リスニ 閉鎖型陸上養殖装置及びそれを用いた陸上養殖方法
CN112930121A (zh) * 2018-12-06 2021-06-08 菲利普莫里斯生产公司 包括文丘里元件的气溶胶生成系统
CN113368715A (zh) * 2021-06-23 2021-09-10 重庆新申世纪新材料科技有限公司 一种多孔无机材料制备用的原料溶解装置及方法
JP2022079413A (ja) * 2020-11-16 2022-05-26 株式会社アクアフューチャー研究所 液体処理ノズル

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JP2011240268A (ja) * 2010-05-19 2011-12-01 Maindorei Gijutsu Kagaku Kenkyusho:Kk 微小気泡発生機構
JP5731650B2 (ja) * 2011-07-20 2015-06-10 株式会社 Ｊａｐａｎ Ｓｔａｒ 気泡発生機構及び気泡発生機構付シャワーヘッド
KR20140048940A (ko) * 2011-07-21 2014-04-24 가부시키가이샤 시바타 기포발생기구 및 기포발생기구 부착 샤워헤드
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JP2018065979A (ja) * 2016-10-19 2018-04-26 株式会社ウォーターデザイン 食用油の製造方法及び製造装置
JP2018178538A (ja) * 2017-04-13 2018-11-15 東芝ライフスタイル株式会社 水洗便器装置、洗浄水タンク装置、及び局部洗浄装置
CN110874513A (zh) * 2018-08-13 2020-03-10 中石化石油工程技术服务有限公司 一种气液混合器注气孔设计方法及装置
CN110874513B (zh) * 2018-08-13 2023-11-03 中石化石油工程技术服务有限公司 一种气液混合器注气孔设计方法及装置
CN112930121A (zh) * 2018-12-06 2021-06-08 菲利普莫里斯生产公司 包括文丘里元件的气溶胶生成系统
CN112930121B (zh) * 2018-12-06 2024-03-26 菲利普莫里斯生产公司 包括文丘里元件的气溶胶生成系统
JP2020189274A (ja) * 2019-05-22 2020-11-26 株式会社リスニ 液体処理装置
JP7370534B2 (ja) 2019-05-22 2023-10-30 株式会社リスニ 液体処理装置
JP7376904B2 (ja) 2019-05-22 2023-11-09 株式会社タケシタ 液体処理ノズル
JP2020189286A (ja) * 2019-05-22 2020-11-26 啓雄 加藤 液体処理ノズル
JP2021019509A (ja) * 2019-07-24 2021-02-18 株式会社リスニ 閉鎖型陸上養殖装置及びそれを用いた陸上養殖方法
JP7410490B2 (ja) 2019-07-24 2024-01-10 株式会社リスニ 閉鎖型陸上養殖装置及びそれを用いた陸上養殖方法
JP2022079413A (ja) * 2020-11-16 2022-05-26 株式会社アクアフューチャー研究所 液体処理ノズル
WO2023027136A1 (fr) * 2020-11-16 2023-03-02 株式会社タケシタ Buse de traitement de liquide
CN113368715A (zh) * 2021-06-23 2021-09-10 重庆新申世纪新材料科技有限公司 一种多孔无机材料制备用的原料溶解装置及方法
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