JP3139460U - Mass production equipment for gas-dissolved liquid by continuous pressurized flow system - Google Patents

Abstract

An apparatus for producing a liquid in which hydrogen gas containing a supersaturated state is dissolved is provided.
A liquid passage through which a liquid flows, a liquid circulation passage through which a raw material liquid 22 circulates to a gas-dissolved liquid receiver 31, and a pressurizing means provided in the middle of the liquid circulation conduit. A pressurizing means for pressurizing the liquid to flow through the flow pipe, and at least one gas-liquid mixing section provided in the middle of the liquid flow pipe, which is connected to the gas container via the gas supply pipe. A gas-liquid mixing unit for mixing hydrogen gas from the gas container with the liquid, and at least one static mixer 60B provided downstream of the gas-liquid mixing unit in the middle of the liquid circulation pipe, the gas-liquid mixing unit The liquid containing a static mixer that maintains the pressure of the gas mixed liquid mixed in step 1 and promotes the dissolution of the gas in the liquid is circulated through the liquid distribution pipe at a flow rate of 10 to 40 L / min. Producing hydrogen gas-dissolved liquid Open system continuous pressurized flow type hydrogen gas dissolved liquid production equipment.
[Selection] Figure 1C

Description

  The present invention relates to an apparatus for producing a gas-dissolved liquid containing a large amount of gas such as hydrogen suitable for mass production.

  It is said that water containing oxygen and hydrogen is effective for promoting the health of the human body, and a method for producing a liquid in which a large amount of oxygen or hydrogen is dissolved in the liquid and an apparatus therefor have been reported (Patent Documents 1 to 3). See).

  As a method for dissolving a gas in a liquid such as water, there is a method in which a gas is dissolved in a liquid by bringing a fine bubble gas into contact with the liquid under atmospheric pressure (bubble type dissolution method). When the gas is brought into contact with the liquid, the gas dissolves in the liquid. At this time, if the contact area is increased, the dissolution rate is increased. However, the amount of gas to be dissolved is limited to a certain amount in a saturated state and cannot be dissolved further. In addition, when the gas and the liquid in which the gas is already dissolved are brought into contact with each other at atmospheric pressure, only the partial pressure of the gas in contact with the gas is obtained. The gas cannot be dissolved.

  On the other hand, there is a method in which a gas is brought into contact with a solution under high pressure (closed system high-pressure holding manufacturing method). In this method, the gas dissolves in the solution according to Henry's law. Further, at this time, the time required for dissolution can be shortened by making the liquid mist or reducing the gas bubbles. When the gas is brought into contact with the liquid in a closed system, the plurality of gases can be dissolved simultaneously by keeping the partial pressures of the plurality of gases at a certain level or higher. However, in order to maintain a high pressure, it is necessary to bring the gas and the solution into contact in an airtight container. In order to produce a gas-containing liquid by bringing gas into contact with each other in such a sealed container, the steps of dissolution and recovery must be repeated, so that the sealed container is enlarged for mass production. The apparatus is also expensive because a pressure vessel must be used. Therefore, it is not suitable for mass production. Further, in the case of abrupt transition from high pressure to atmospheric pressure, in most cases, supersaturated gas is released instantaneously due to bumping.

  On the other hand, there is also a production of a gas-containing liquid by a continuous flow system in which a liquid is continuously injected from one end into a pressure-resistant thin tube, and the gas and the liquid are brought into contact with each other in the tube (an open flow-type manufacturing method). However, since at least one end of the continuous flow system comes into contact with air under atmospheric pressure, the continuous flow system is an open system, and the inside of the continuous flow system cannot be maintained at a high pressure. Therefore, the gas cannot be dissolved in a larger amount than when the atmospheric pressure gas is brought into contact with the liquid.

  As described above, both the above-described open system flow manufacturing method for mass production and the closed system high pressure holding production method for keeping the gas pressure at a high pressure in the closed system have drawbacks, and dissolved a large amount of gas. It is difficult to produce a large amount of liquid. In addition, in the closed system high pressure holding manufacturing method, it is necessary to manufacture the gas-dissolved liquid completely in the closed system, whereas in the open system flow manufacturing method, the liquid must be in contact with air at atmospheric pressure. It is difficult to maintain a high pressure, and it has been difficult to establish a method for producing a gas-dissolved liquid having the advantages of both methods.

  Furthermore, there is a method of dissolving hydrogen or oxygen in a liquid by electrolysis. However, in this method, the liquid must contain an electrolyte, which is also unsuitable for mass production.

JP-A-8-56632 JP 2002-172317 A JP 2005-296794 A

  An object of this invention is to provide the apparatus which manufactures the liquid which melt | dissolved gas, such as hydrogen containing a supersaturated state.

  The inventors of the present invention have intensively studied an apparatus for producing a gas-dissolved liquid, which has the advantages of the above-described open-type flow-through production method and the closed-system high-pressure holding production method that keeps the gas pressure high in a closed system. It was.

  The inventors of the present application, when dissolving a gas in a liquid under high pressure by a closed system high-pressure holding manufacturing method, must place the manufacturing apparatus in a closed system so that it does not come into contact with the atmosphere. When the gas was dissolved in the liquid by the manufacturing method, the solution to the contradiction that it was not possible to keep the high pressure because of the open system was investigated.

  As a result, it has been found that by bringing a gas such as oxygen or hydrogen in a pressurized state directly into contact with a pressurized liquid flowing in a pipe, the gas is efficiently and rapidly dissolved in the liquid. That is, when a gas is mixed with a liquid and coexists with the liquid in the form of bubbles, pressure is applied and the pressure is maintained so that the liquid can flow even in an unclosed flow-type device. It has been found that a large amount of gas can be continuously dissolved in a liquid.

  The inventors of the present invention have further studied, and when the gas is mixed with the liquid and flows through the apparatus as a gas-liquid mixed phase flow, the action of the reactor unit is obtained by using a means called a reactor unit that inhibits the flow of the liquid. As a result, it was found that the pressure was maintained and the gas was efficiently dissolved in the liquid, and a device for dissolving the gas in the liquid was produced to complete the present invention.

That is, the present invention is as follows.
[1] A liquid flow line through which a liquid flows, the raw material liquid flowing to a gas-dissolved liquid receiver,
Pressurizing means provided in the middle of the liquid circulation pipe, pressurizing means for pressurizing the raw material liquid to circulate through the circulation pipe;
At least one gas-liquid mixing section provided in the middle of the liquid circulation pipe, which is connected to a gas container via a gas supply pipe, and gas-liquid mixing for mixing hydrogen gas from the gas container with the liquid Part,
At least one static mixer provided downstream of the gas-liquid mixing part in the middle of the liquid circulation pipe, maintaining the pressure of the gas mixed liquid mixed in the gas-liquid mixing part, and dissolving the gas in the liquid Promote static mixer,
An open-type continuous pressurized flow type hydrogen gas dissolving liquid production apparatus for producing a hydrogen gas dissolving liquid continuously while pressurizing and flowing the liquid through the liquid circulation pipe at a flow rate of 10 to 40 L / min.

[2] The open-system continuous pressurized flow type hydrogen gas dissolving liquid production apparatus according to [1], wherein the pressure applied to the liquid flowing in the static mixer is gradually reduced in the static mixer.
[3] The open-system continuous pressurized flow type hydrogen gas dissolving liquid production apparatus according to [1] or [2], wherein the gas-liquid mixing unit is an ejector.
[4] The open-system continuous pressurized flow type hydrogen gas dissolving liquid production apparatus according to any one of [1] to [3], wherein the pressurizing means is a pressurizing pump.

[5] The open system continuous pressurized flow type hydrogen gas dissolving liquid production apparatus according to [4], wherein the pressurizing pump is a vortex pump, and is provided downstream of the gas-liquid mixing unit and upstream of the static mixer.
[6] The open system continuous pressurized flow type hydrogen gas dissolving liquid production apparatus according to any one of [1] to [5], wherein the gas-liquid mixing unit and the static mixer are directly connected.
[7] The open-system continuous pressurized flow type hydrogen gas dissolving liquid production apparatus according to any one of [1] to [6], wherein the ratio of the length of the static mixer to the inner diameter of the tube is 10 or more.

[8] The open-system continuous pressurized flow hydrogen gas-dissolved liquid according to any one of [1] to [7], wherein the pressure applied to at least one of the raw material liquid and the gas-dissolved liquid is equal to the atmospheric pressure and is an open system. Manufacturing equipment.
[9] Open system continuous pressurized flow type hydrogen according to any one of [1] to [8], having a plurality of gas-liquid mixing sections and static mixers, and capable of dissolving a plurality of gases including hydrogen gas Gas dissolved liquid production equipment.
[10] The opening according to any one of [1] to [9], wherein the liquid is selected from the group consisting of water, mineral water, tea, coffee, soft drink, juice, gel drink, cosmetics, shampoo and physiological saline Continuous pressurized flow type hydrogen gas dissolved liquid production equipment.

  When the continuous pressure flow type gas dissolving apparatus of the present invention is used, a liquid in which a large amount of gas is dissolved can be continuously produced in a large amount in a short time.

  Moreover, the gas melt | dissolution liquid which melt | dissolved several gas can be manufactured by mixing several gas simultaneously, or by connecting this apparatus partially.

  In the method for producing a gas-dissolved liquid using the apparatus of the present invention, a gas maintained at a high pressure is mixed with the liquid flowing through the pipe of the narrow tube, and the gas mixed liquid mixed with the gas flows in the pipe. By maintaining the pressure, the gas and the liquid are brought into sufficient contact under pressure, and a large amount of gas is dissolved and contained in the liquid. Here, the gas-dissolved liquid means a state in which the gas is dispersed in the liquid to form a uniform phase, and the gas mixed liquid means a state in which the liquid and the gas are mixed. Say. When the gas mixture liquid flows through the narrow tube, a gas-liquid mixed phase flow in which gas bubbles exist in the liquid is obtained. However, a gas-dissolved liquid and a gas-mixed liquid are not strictly distinguished. When a gas-dissolved liquid is produced using the device of the present invention, the gas is mixed with the liquid to form a gas-mixed liquid. A gas-dissolved liquid is made through the reactor, but a part of the gas is dissolved in the liquid even in the state of the gas mixed liquid, and even in the state of the gas-dissolved liquid, a part of the gas is degassed from the liquid, It can be present in the liquid. In the present invention, when the gas is mixed with the liquid, the gas dissolved liquid or the gas mixed liquid may be distinguished depending on which is superior as the gas state. In the present invention, the gas-dissolved liquid is sometimes referred to as a gas-dissolved liquid.

  A narrow pipe line through which liquid flows has a gas-liquid mixing part and a reactor part in the middle of the pipe line. The gas-liquid mixing unit, the thin tube, and the reactor unit are connected in a state where the gas-liquid mixing unit is located upstream of the reactor unit so that the liquid flows through each other. It flows through the reactor section. In the present invention, upstream and downstream are referred to as upstream or downstream on the basis of the direction of the flow of liquid flowing through the conduit of the flow-type device.

  The liquid flows from the raw material liquid container through the narrow tube to the gas dissolved liquid receiver. Here, the raw material liquid is a liquid that is intended to dissolve a gas and is a liquid before the gas is dissolved. While the liquid flows from the raw material liquid container to the gas-dissolved liquid receiver, the gas is mixed in a state where pressure is applied to the liquid flowing through the narrow tube by the gas-liquid mixing unit. However, at this time, the gas is not sufficiently dissolved in the liquid, and the gas and the liquid are mixed in a state where the gas bubbles are present in the liquid, that is, in the state of the gas mixed liquid. The gas mixture liquid flows toward the reactor section in the narrow tube, and the pressure of the gas mixture liquid is maintained in the pipe line upstream of the reactor section or in the reactor section by the action of the reactor section. As a result, a large amount of gas is dissolved in the liquid by the action of pressure. In addition, due to the action of the reactor unit, the bubble size of the gas mixed in the bubble state in the liquid is reduced, the contact area between the gas and the liquid is increased, and the gas is more easily dissolved in the liquid. The gas-containing liquid in which the gas has been dissolved is gradually depressurized in the reactor, and then exits the reactor and enters the receiver through the narrow tube.

  The thin tube is made of a tube that can withstand high pressure, and the thin tube that can withstand high pressure is preferably a thin tube made of a pressure resistant material such as iron, stainless steel, or resin.

  The gas-liquid mixing unit is configured such that a thin pipe line through which a liquid flows and a pipe through which a gas is supplied merge. Gas is pressurized and supplied continuously to the liquid flowing through the narrow tube. The gas may be supplied from a high-pressure cylinder containing gas. The gas-liquid mixing unit may have any form as long as the gas is mixed with the liquid. For example, a pipe that feeds pressurized gas is connected to the side of a thin tube through which liquid flows, and an air supply port is provided at the connecting portion, and gas is injected and mixed from the air supply port into the liquid flowing through the thin tube. What should I do? In this case, the pipe for supplying the gas branches into a T shape or a substantially T shape with respect to the thin tube through which the liquid flows. The air supply port may be provided on the side wall of the thin tube, or may be inserted and opened in the liquid flowing in the pipe line of the thin tube. As such a gas-liquid mixing unit, for example, an apparatus having an ejector structure can be used. An ejector is a device for drawing a gas in a reduced pressure state by providing a bottleneck in a part of the liquid flow path and increasing the flow velocity of that part. In the ejector, a branch pipe is connected to the main pipe in a T-shape, the liquid flowing through the main pipe is decompressed in the bottleneck, and the gas in the non-pressure branch pipe is drawn into the liquid. If fine bubbles are generated by the ejector, the contact surface between the liquid and the gas becomes large and the gas can be easily dissolved.

  What is important here is that the liquid is maintained at a high pressure before flowing into the reactor section downstream of the gas-liquid mixing section. For this purpose, for example, pressure may be applied to the liquid and the fluid may flow in the narrow pipe. At this time, pressure may be applied to the inside of the container for supplying the raw material liquid, and the liquid may flow through the thin tube by the pressure, or a pump, a compressor, a booster, etc. may be provided in the middle of the thin tube. By applying pressure to the liquid, the liquid may flow in the narrow tube. When applying pressure to the liquid, for example, the raw material liquid may be placed in a pressurized container and the liquid may be flowed by pressure. Alternatively, tap water may be used as the raw material liquid and the supply pressure of tap water may be used. When a pump is used, a pressure pump, for example, a vortex pump (cascade pump) is used. A vortex pump is a pump that discharges by increasing the pressure while rotating a disk with a groove in a narrow casing to cause a strong vortex in the liquid and making the inner circumference of the casing approximately one round. A thin tube can be flowed in a state. If a liquid is flowed under pressure, the flow rate becomes a certain speed or higher.

  The pump is located upstream of the reactor and may be located either downstream or upstream of the gas-liquid mixing unit. When a vortex pump is used as the pump, it is preferably installed downstream of the gas-liquid mixing unit.

  For example, by combining a liquid flow capillary that is a liquid supply pipe through which liquid flows upstream of the pump and a gas supply pipe to which gas is supplied, the gas that is supplied at high pressure is supplied to the liquid that flows through the narrow pipe by the action of the pump. Mixed.

The liquid in which the gas is mixed by the gas-liquid mixing part flows through the narrow tube and travels toward the reactor part.
By the action of the reactor section, the pressure of the liquid mixed with the gas is maintained without being rapidly reduced. That is, the reactor part functions as a pressure maintaining part. By maintaining the pressure of the liquid mixed with the gas high, the gas can be dissolved in a large amount in the liquid. Depending on the specific structure or material, the reactor section increases friction between the liquid flowing inside and the reactor section, or acts as a resistance to the flow of the liquid in which the gas is mixed, thereby inhibiting the rapid flow of the liquid. As a result, the pressure upstream of the reactor unit and / or inside the reactor unit can be maintained. The reactor unit is, for example, a thin tube having a plurality of fin (fin) structures inside. Moreover, the thin tube which has a bottleneck may be sufficient.

  Further, the liquid in which the gas is mixed is stirred by the reactor, the contact area between the gas and the liquid is increased, and the gas dissolution efficiency is increased. Furthermore, by applying pressure and stirring, the gas bubbles become smaller, the contact area between the gas and the liquid becomes larger, and the gas dissolution efficiency becomes higher. In this respect, the reactor part of the present invention also functions as a part for increasing the contact area between the gas and the liquid.

  In the reactor section, friction is generated by the contact of molecules and gas molecules constituting the liquid, so that the pressure becomes higher when the liquid is flowed at a high speed.

  An example of the reactor unit is a static mixer. When the static mixer is used, the contact time between the liquid and the gas can be increased, so that the dissolution efficiency of the gas into the liquid can be further improved. As shown in FIG. 5, the static mixer has a plurality of elements (for example, 8, 16, or 32) arranged in an elongated tubular housing, and this element is a rectangular metal flat plate. It consists of a 180 ° right twist (see FIGS. 5B and 5C) or a left twist (see FIGS. 5D and 5E). 5B and 5D are front views of the right twist element and the left twist element, respectively, and FIGS. 5C and 5E are views in which the elements shown in FIGS. 5B and 5C are rotated by 90 °, respectively. The static mixer is formed by appropriately combining these elements in the required number. The size of each element of the static mixer is, for example, about 1.5 cm in length and about 1 cm in width, and the same number of right and left twists are used in combination. In this case, the 8-element type static mixer has a length of about 18 cm, and the 32-element type has a length of about 54 cm.

  The elements of the static mixer may be provided with protrusions and fins as shown in FIG. 5F. By providing such protrusions, fins, and depressions, the flow of liquid flowing in the static mixer is hindered, pressure is applied to the liquid, and the amount of gas dissolved increases. The protrusion may be a small protrusion or a wholesaler-like protrusion. Further, turbulence is generated by the protrusions and fins, the bubble size of the gas mixed in the liquid is reduced, the contact area between the gas and the liquid is increased, and the gas dissolution efficiency is improved. Further, the surface of the element of the static mixer may be processed so as to increase the friction with the liquid. For example, the surface of the element is roughened by a blasting process, and a groove is formed on the element surface.

  In the apparatus of the present invention, the gas is continuously dissolved in the liquid while the liquid flows from the raw material liquid container to the gas dissolution liquid receiver. In the device of the present invention, at least the gas-dissolved liquid receiver may be in contact with the atmosphere. Further, even if the gas-dissolved liquid receiver is not in contact with the atmosphere, it is not necessary to apply pressure to the gas-dissolved liquid receiver, and the gas-dissolved liquid is almost at the same pressure as atmospheric pressure. In this respect, it can be said that the device of the present invention is not completely closed from the atmosphere and is open to the atmosphere. Therefore, it can be said that the device of the present invention is an open device.

  Since the liquid lead-out path portion of the reactor section is connected to a gas-dissolved liquid receiver that is not under pressure, the pressure gradually decreases from the liquid introduction path to the liquid lead-out path inside the reactor section. By gradually lowering the pressure in this way, it is possible to prevent a sudden loss of supersaturated gas due to bumping. Therefore, the gas-dissolved liquid recovered through the reactor via the narrow tube is kept in a supersaturated state.

  In particular, the device of the present invention can keep a gas composed of a single atom such as hydrogen, which is difficult to be bubbled and dissolved in a liquid, in a saturated state for a long time. Suitable for At this time, the gas can be dissolved at a higher concentration by contacting at a low temperature.

  The gas-liquid mixing part and the reactor part may be connected via a thin tube, or the reactor part may be directly connected downstream of the gas-liquid mixing part.

  A valve is installed in the middle of the narrow pipe as necessary to prevent the flowing liquid from flowing backward.

  The inner diameter of the thin tube is 0.2 to 5 cm, preferably 0.5 to 2 cm, depending on the amount of the gas-dissolved liquid to be produced. Similarly, the inner diameter of the reactor part is 0.2 to 5 cm, preferably 0.5 to 2 cm, depending on the amount of the gas-dissolved liquid to be produced. Furthermore, the ratio of the tube inner diameter to the length of the reactor section is 1:10 to 200, preferably 1:20 to 100.

  The pressure applied to the gas mixed with the liquid flowing in the narrow tube is 1 to 20 atmospheres, preferably 2 to 10 atmospheres, and more preferably 3 to 5 atmospheres. The gas is supplied in a high pressure cylinder, and the high pressure cylinder is usually under a pressure of several tens to several hundreds of atmospheres. Therefore, when supplying gas from a high-pressure cylinder, a pressure reducing valve is provided between the high-pressure cylinder and the gas-liquid mixing unit, and the pressure of the gas supplied to the gas-liquid mixing unit is reduced to the above pressure.

  Further, the pressure applied to the liquid flowing in the narrow tube is 3 to 5 atm in the reactor part introduction path, and the pressure is maintained upstream of the reactor part and / or in the vicinity of the reactor part introduction path. Further, as described above, the pressure applied to the liquid gradually decreases when the liquid flows in the reactor section. In the reactor part lead-out path, the pressure applied to the gas is about 1 to less than 2 atmospheres, preferably about 1 atmosphere, which is almost the same as the atmospheric pressure.

  The flow rate of the liquid flowing in the thin tube of this apparatus depends on the passage of the thin tube and the amount of the gas-dissolved liquid to be produced, but when using a reactor having an inner diameter of 1.1 cm, it is 5 to 80 L / min, preferably 10 ~ 40L / min. The flow rate of the gas supplied to the gas-liquid mixing unit is 0.2 to 5 L / min, preferably 0.5 to 2 L / min. When the gas is dissolved in the liquid at normal pressure, the amount of dissolution increases as the time during which the gas and the liquid are in contact with each other is longer. Therefore, when dissolving at normal pressure, a smaller liquid flow rate is preferable. On the other hand, in the apparatus of the present invention, since pressure is applied when the gas and the liquid are in contact with each other, the gas dissolves in a short time, so that the liquid flow rate can be increased. Since the flow rate of the liquid can be increased, the flow rate of the gas can be adjusted to a size corresponding to the flow rate. For example, when a liquid is flowed at a flow rate of 40 L / min to produce a gas-dissolved liquid, about 2.5 tons of a gas-dissolved liquid can be produced per hour. When this manufacturing efficiency is achieved and used in a closed system high pressure holding manufacturing method using a closed pressurized tank, a huge tank or a large number of tanks are required. The continuous pressurized flow type gas-dissolved liquid production apparatus of the present invention can produce a gas-dissolved liquid much more efficiently and inexpensively than the conventional method.

  The continuous pressurized flow type gas-dissolved liquid production apparatus of the present invention may include only one set of the gas-liquid mixing unit and the reactor unit or a plurality of sets. When only one set is provided, one kind of gas can be dissolved and contained in the liquid, and when a plurality of sets are provided, a plurality of gases can be dissolved and contained in the liquid. In an apparatus having a plurality of gas-liquid mixing sections and reactor sections and dissolving a plurality of gases in a liquid, the conditions such as the pressure of each gas and liquid are the same as those in the apparatus for dissolving one kind of gas in a liquid. It is.

  Liquids that dissolve gas using the apparatus of the present invention include general aqueous beverages such as mineral water, fruit juice and fruit beverages, coffee beverages, oolong tea beverages, green tea beverages, tea beverages, barley tea beverages, and the like. , Vegetable drinks, sports drinks, soft drinks, gel drinks, cosmetics, shampoos, physiological saline and the like.

  Examples of the gas dissolved in the liquid include hydrogen gas, oxygen gas, ozone gas, and the like, and hydrogen gas is preferable.

  For example, when hydrogen is used, about 17.5 mL of hydrogen can be dissolved per 1 L of water (about 1.6 ppm, about 0.8 mM) at 1 atm of hydrogen and room temperature. The gas-containing liquid of the present invention contains 10 mL or more, preferably 15 mL or more, particularly preferably 17.5 mL or more of hydrogen molecules per liter of water. Further, the gas-dissolved liquid of the present invention contains 0.1 ppm or more, 0.5 ppm or more, preferably 1 ppm or more, more preferably 1.5 ppm or more. The gas-dissolved liquid of the present invention contains 0.1 mM or more, preferably 0.4 mM or more, more preferably 0.6 mM or more, and particularly preferably 0.8 mM or more. Furthermore, by using the apparatus of the present invention, a large amount of hydrogen-dissolved water in which hydrogen is dissolved in a supersaturated state can be obtained. When dissolved hydrogen concentration is 1.52ppm or more, or 1.5mg / L or more, it is said that hydrogen is dissolved in supersaturation.

  When oxygen is dissolved alone, the gas-containing liquid of the present invention contains 0.2 mg or more, preferably 10 mg or more, more preferably 40 mg or more, per liter of water. When coexisting with hydrogen, 0.2 mg or more, preferably 2 mg or more, more preferably 10 mg or more is contained per liter of water.

  When hydrogen or hydrogen and oxygen are dissolved, the pH of the gas-dissolved liquid is 3 to 11, and the redox potential is -50 mV or less.

  The gas-dissolved liquid obtained by using the apparatus of the present invention is preferably stored in a container made of a material that is not permeable to gas such as aluminum. Examples of such containers include aluminum pouches and aluminum cans.

  The gas-dissolved liquid produced using the device of the present invention is used as drinking water or soft drinks. For example, drinking water and soft drinks in which hydrogen is dissolved, drinking water and soft drinks in which oxygen is dissolved, and drinking water and soft drinks in which hydrogen and oxygen are dissolved are functional drinks that promote health and It becomes a soft drink.

  In addition, the gas-dissolved liquid produced using the apparatus of the present invention is a cosmetic in which gas is dissolved, a pharmaceutical in which gas is dissolved, for example, a cosmetic and pharmaceutical in which hydrogen is dissolved, a cosmetic and pharmaceutical in which oxygen is dissolved. , And cosmetics and pharmaceuticals in which hydrogen and oxygen are dissolved. Specific examples include pharmaceuticals such as infusion containing hydrogen and oxygen simultaneously.

  Furthermore, the gas-dissolved liquid produced using the apparatus of the present invention is used as a cleaning liquid in which a gas is dissolved. For example, when hydrogen is dissolved in pure water, a liquid having a large reducing power is formed. Can be used for washing.

  Furthermore, the gas-dissolved liquid produced using the apparatus of the present invention can also be used for storing gas.

  Furthermore, when tap water is used as the raw material liquid, gas-dissolved tap water can be easily produced at home by connecting the device of the present invention to a tap water faucet. In this case, the raw material liquid is pressurized by the supply pressure of tap water.

  An example of the continuous pressurized flow type gas dissolved liquid production apparatus of the present invention will be described with reference to FIGS. As shown in FIG. 1A, the continuous pressurized flow type gas-containing liquid production apparatus 100 includes a gas-liquid mixing unit 35 and a reactor unit 70.

  As the gas-liquid mixing unit 35, in addition to the ejector 50 shown in FIG. 2, a gas inlet 41 is provided in the pipe line 40 shown in FIG. 3, and a gas permeable membrane is provided in a part of the pipe line 40 shown in FIG. Or what provided the porous gas permeable board 42 is mentioned.

  The reactor unit 70 is located downstream of the gas-liquid mixing unit 35, and the gas-liquid mixing unit and the reactor unit may be directly connected or may be connected via a thin tube as shown in FIG. 1A.

  The structure of the ejector 50 is shown in FIG. The ejector 50 includes a liquid introduction passage 51, a nozzle portion 52 that extends from the liquid introduction passage 51 with a tapered inner diameter, a diffusion chamber 53, a diffuser portion 54 that has a tapered inner diameter and extends, and the diffuser portion 54. An outlet channel having a uniform inner diameter that communicates and a gas introduction channel 56 that communicates with the diffusion chamber 53 are provided. In the ejector 50, when liquid is introduced from the liquid introduction path 51 and injected from the nozzle 52 to the diffuser portion 54, the inside of the diffusion chamber 53 becomes negative pressure, so that the gas is sucked from the gas introduction path 56, and the diffuser Since it is sufficiently mixed in the part 54, the sucked gas can be efficiently absorbed into the liquid. In addition, since the liquid flow rate can be increased, a large amount of gas can be absorbed in a large amount of liquid while being small in size.

  As the reactor unit, a static mixer may be provided downstream of the gas-liquid mixing unit. For example, in FIG. 1C, an ejector 50 is used as a gas-liquid mixing unit, and a static mixer 60 that is a reactor unit is directly connected.

  When the static mixer is used, the contact time between the liquid and the gas can be extended, so that the gas absorption efficiency can be further improved. In addition, when a static mixer is used, the speed of the liquid flowing through the pipe is temporarily reduced. As a result, the pressure of the liquid in the gas-liquid mixing section is increased, and the gas is more efficiently dissolved in the liquid. As shown in FIG. 5A, the static mixer 60 has a plurality of elements 62 (for example, 8, 16, or 32) disposed in an elongated tubular housing 61. The elements 62 are rectangular. It consists of a metal flat plate twisted 180 ° right (see FIGS. 5B and 5C) or left twisted (see FIGS. 5D and 5E). 5B and 5D are front views of the right twist element and the left twist element, respectively, and FIGS. 5C and 5E are views in which the elements shown in FIGS. 5B and 5C are rotated by 90 °, respectively. The static mixer 60 is manufactured by appropriately combining these elements 62 as many as required. Each element of the static mixer has a length of about 1.5 cm and a width of about 1 cm, for example, and the same number of right and left twists are used in combination. The 8-element static mixer is about 18 cm long, and the 32-element type is about 54 cm long.

  1A is a device for dissolving one type of gas in a liquid, and includes only one set of a gas-liquid mixing unit and a reactor unit.

  A liquid circulation thin tube (liquid supply pipe) 24 is connected to the container 21 in which the raw material liquid 22 is placed and the liquid introduction path 36 </ b> B of the gas-liquid mixing unit 35 through the pressurizing pump 23. In addition, a gas supply pipe 28 is connected to the gas cylinder 25 which is a pressurized gas supply source and the gas introduction path 37B of the gas-liquid mixing unit 35 via a pressure reducing valve 26, a pressure gauge 27 and a flow meter (not shown). Has been. Further, the liquid outlet path 38B of the gas-liquid mixing unit 35 is connected to a receiver 31 for the gas-dissolved liquid maintained at normal pressure via the liquid circulation thin tube (gas-dissolved liquid recovery pipe) 29, the reactor unit 70, and the stop valve 30. It communicates with the upper part.

  The pressurizing pump 23 may be located downstream of the gas-liquid mixing unit and upstream of the reactor unit as shown in FIG. 1B.

  The gas-dissolved liquid production apparatus 100 is operated as follows to produce a predetermined gas-dissolved liquid 32. That is, the raw material liquid 22 in the container 21 is pressurized to a predetermined pressure, for example, 1 to 10 atm by the pressurizing pump 23, and supplied to the liquid introduction path 36 </ b> B of the gas-liquid mixing unit 35. The gas is adjusted to a predetermined pressure, for example, 3 to 5 atm by the pressure reducing valve 26, and is supplied to the gas introduction path 37 </ b> B of the gas-liquid mixing unit 35 by the gas supply pipe 28.

  The gas mixed liquid that has exited from the liquid lead-out path 38 </ b> B of the gas-liquid mixing unit 35 travels to the reactor unit 70. The gas mixed liquid is already pressurized, and the pressure is maintained by the action of the reactor unit, and enters the reactor unit introduction path 71B in a pressurized state. For this reason, gas melt | dissolves in a liquid in a reactor part. The liquid is gradually depressurized in the reactor section, and a gas-dissolved liquid having a pressure close to normal pressure comes out from the outlet of the reactor section, passes through a liquid circulation thin tube (gas-dissolved liquid recovery pipe) 29 and a stop valve 30, and is almost constantly discharged. It is led to the upper part of the receiver 31 maintained at a pressure. In the receiver 31, a part of the gas dissolved in the obtained gas-dissolved liquid 32 is vaporized, but a large amount of gas remains in the gas-dissolved liquid 32 in a supersaturated state. Released into the atmosphere. The receiver 31 may be sealed in order to prevent entry of dust or the like in the atmosphere, but is not pressurized and is maintained at almost normal pressure.

  FIG. 1B shows an apparatus in which a pressure pump 23 is located downstream of the gas-liquid mixing unit. In this case, the gas mixed liquid mixed in the gas-liquid mixing unit 35 is directed to the reactor unit 70 in a pressurized state by the action of the pressure pump. As the pressure pump, for example, a vortex pump may be used.

  FIG. 1C shows an apparatus having an ejector 50 as a gas-liquid mixing section and a static mixer 60 directly connected to the ejector 50.

  Furthermore, FIG.6 and FIG.7 shows the apparatus which manufactures the gas melt | dissolution liquid which melt | dissolved two types of gas. The apparatus shown in FIG. 6 has two gas-liquid mixing units and two reactor units, and the gas in the first gas cylinder 15 is liquidized by the first gas-liquid mixing unit 35A and the first reactor unit 70A. 11 and is stored in the liquid receiver 21 in which the gas in the first gas cylinder is once dissolved. Next, the gas in the second gas cylinder 25 is further dissolved into the liquid in which the gas in the first gas cylinder is dissolved by the second gas-liquid mixing unit 35B and the second reactor unit 70B, and the two kinds of gases. A liquid 32 is obtained that dissolves.

  The gas-dissolved liquid manufacturing apparatus 101 shown in FIG. 6 obtains a pressurized gas-dissolved liquid once in the first gas-liquid mixing unit 35A, and then returns to normal pressure to obtain a normal-pressure gas-dissolved liquid. The normal-pressure gas-dissolved liquid is again pressurized to a predetermined pressure, for example, 1 to 10 atm by the pressurizing pump 23, and is supplied to the second gas-liquid mixing unit 35B via the second gas-dissolved liquid supply pipe 24. However, the steps of depressurization and pressurization in this part can be omitted. An example in which the steps of decompression and pressurization are omitted is shown in FIG. In the apparatus shown in FIG. 7, a set of two gas-liquid mixing units and a reactor unit are connected in series, and the gas in the first gas cylinder 15 is the first gas-liquid mixing unit 35A and the first gas cylinder 15A. The gas dissolved liquid obtained by being dissolved in the liquid 11 by the reactor unit 70A is directly sent to the second gas-liquid mixing unit 35B, and the second gas-liquid mixing unit 35B and the second reactor unit 70B The gas in the second gas cylinder is further dissolved in the liquid in which the gas in one gas cylinder is dissolved, and a liquid 32 in which two kinds of gases are dissolved is obtained. The gas-dissolved liquid manufacturing apparatus 102 shown in FIG. 7 is different from the gas-containing liquid manufacturing apparatus 101 shown in FIG. 6 in that the liquid outlet path 72A of the first reactor section 70A and the second The liquid introduction path 36B of the gas-liquid mixing unit 35B is connected by the flow rate adjusting valve 33 and the first gas-dissolved liquid supply pipe 34, and is obtained by the first gas-liquid mixing unit 35A and the first reactor unit 70A. Only the point where the pressurized first gas-dissolved liquid is directly supplied to the liquid introduction path 36B of the second gas-liquid mixing portion 35B through the flow rate adjusting valve 33 by the first gas-dissolved liquid supply pipe 34. The other configurations are substantially the same.

  In this case, the flow rate adjustment valve 33 may not be provided, but the first gas-dissolved liquid in a pressurized state is supplied to the liquid introduction path 36B of the second gas-liquid mixing unit 35B by giving a slight pressure loss at this portion. This is preferable because the flow rate is stabilized and control is facilitated.

  6 and 7, for example, oxygen gas may be used as the first gas and hydrogen gas may be used as the second gas.

  Hereinafter, specific examples of the present invention will be described in detail with reference to examples. However, the following examples are not intended to limit the present invention, and the present invention is shown in the claims of the utility model registration. The present invention can be equally applied to various modifications without departing from the technical idea.

Example 1 Production of Hydrogen Dissolved Water In the apparatus shown in FIG. 1A, tap water was used as the raw material liquid, and water from the tap was passed through the raw water supply pipe 24. The supply pressure of tap water was about 1.5 to 2 atmospheres. A stainless steel pipe (inner diameter: 11 mm) was used as the thin tube, a stainless steel T-shaped joint was used as the gas-liquid mixing part, and hydrogen gas was supplied to the joint from a hydrogen cylinder. The pressure of the hydrogen gas supplied to the gas-liquid mixing part was 0.4 MPa (megapascal) (about 4 atm). A static mixer (32-fin static mixer having 32 elements) was connected to the gas-liquid mixing section. As a static mixer, a static mixer having 32 elements (fins) (Noritake, T8-32R-4PT, size: pipe inner diameter 11 mm × length 540 mm) and a static mixer having 8 elements (fins) (Noritake, CSM-12-1, size: tube inner diameter 11 mm × length 162 mm) was used. FIG. 8 shows each part configuration of the apparatus used. In the figure, 1 to 6 are joints (fine tubes) or parts for connecting thin tubes, and 4 corresponds to a gas-liquid mixing part. 7 is an electromagnetic valve, 8 is a flow switch, 9 is a valve, and 10 is a static mixer. 11 and 12 are electrical components.

  The flow rate of water flowing through the pipe of the apparatus was 4, 6, 8 or 10 L / min, and the flow rate of hydrogen gas supplied to the gas-liquid mixing unit was 0.1, 0.4, 0.6, 0.8 and 1.0 L / min. The hydrogen-dissolved water that came out of the narrow tube through the static mixer was collected, and the hydrogen concentration was measured.

  The results are shown in Table 1. In Table 1, the unit of hydrogen concentration is ppm. As shown in Table 1, the amount of dissolved hydrogen increases as the water flow rate increases and the hydrogen flow rate increases. Also, the amount of dissolved hydrogen increases when a static mixer with 32 elements is used than when a static mixer with 8 elements is used. In particular, when a static mixer with 32 elements was used and the water flow rate was 8 L / min and the hydrogen flow rate was 0.8 L / min, hydrogen-dissolved water in which hydrogen was dissolved by supersaturation was obtained. The greater the water flow rate, the greater the water pressure at the reactor section. Furthermore, the larger the number of elements in the static mixer, the more disturbed the water flow in the reactor section, and the water pressure in the reactor section increases. This result shows that the pressure of the liquid in the reactor part can be kept high enough for a period sufficient to dissolve the gas to a supersaturated state. Moreover, since the contact time of water and hydrogen should become short, so that a water flow speed is quick, it shows that the amount of gas dissolution increases by maintaining a pressure higher than a contact time.

Example 2 Hydrogen Water Production Manufacture by Changing the Reactor Portion Hydrogen dissolved water was produced in the same manner as in Example 1. At this time, a static mixer having 8 elements (fins) was used.

  At this time, in addition to a static mixer that does not process the element, a static mixer in which the surface of the element is blasted (blasting is roughened with sandpaper), a static mixer in which the surface of the element is processed into a wholesale shape (metal The surface was made into a wholesale shape with a file), and a static mixer in which the surface of the element was indented (the surface of the element was drilled) was used.

  The results are shown in Table 2. As shown in Table 2, the amount of dissolved hydrogen is larger when the processed static mixer is used than when the unprocessed static mixer is used. By blasting the elements of the static mixer, the friction between water and the inside of the reactor part increases, and the pressure in the reactor part increases. Further, when the element is processed into a wholesale shape or a recess is formed, water flow failure in the reactor portion occurs, and the water pressure in the reactor portion increases. This result shows that the gas dissolution efficiency is increased by keeping the pressure of the liquid high in the vicinity of the reactor section and / or the upstream reactor section entrance.

Example 3 Production of Hydrogen and Oxygen Dissolved Water As Example 3, tap water (redox potential +420 mV, pH = 7.2) in Chuo-ku, Tokyo is used as raw water, and the production apparatus 101 shown in FIG. 6 is used. Then, oxygen and hydrogen-dissolved water was produced as follows. First, a case where only the ejectors 50A and 50B were used and a static mixer was not used was taken as a comparative example, and an example in which an 8-element type static mixer was used as a reactor portion in the comparative example was taken as Example 3-1. A comparative example in which a 32-element static mixer was used in combination as a reactor section was designated as Example 3-2.

  The raw water flow rate, raw water pressure, oxygen dissolved water flow rate, oxygen pressure, oxygen dissolved water pressure, and hydrogen pressure in Comparative Example, Example 3-1 and Example 3-2 were all made the same to produce oxygen and hydrogen dissolved water. did. Table 3 summarizes the manufacturing conditions and measurement results. The measurement of oxidation-reduction potential, oxygen dissolution amount, hydrogen dissolution amount and pH was carried out at room temperature using the OPR measuring device, oxygen amount measuring device, hydrogen amount measuring device and pH meter manufactured by Toa DKK. Is the same).

The following can be seen from the results shown in Table 3.
(1) As shown in Example 3-2, when a reactor unit using 32 elements is used, a supersaturated or nearly saturated solution can be produced regardless of the type of gas, whether oxygen or hydrogen. Therefore, it was shown that a sufficient pressure was maintained for a sufficient period of time in the reactor to dissolve to a supersaturated state. The saturated concentrations of oxygen and hydrogen are about 42 mg / L and 1.5 mg / L, respectively.

(2) The comparative example using the ejectors 50A and 50B and not using the static mixer has a small amount of dissolved oxygen and a small amount of dissolved hydrogen, indicating that the presence of the reactor part is important for the amount of dissolved gas. . Also, 32 elements dissolve more oxygen and hydrogen than 8 elements. This indicates that the larger the number of elements, the higher the pressure and the more advantageous for gas dissolution. The results obtained when a 64-element static mixer was used were the same as when a 32-element static mixer was used, indicating that 32 elements are sufficient.

(3) As shown in Examples 3-1 and 3-2, when hydrogen was continuously dissolved in oxygen-dissolved water, it was shown that oxygen could remain.
(4) Neutral hydrogen and oxygen dissolution with excellent reducibility, such as ORP (redox potential) of -485 mV or -566 mV, even if the amount of dissolved oxygen is 2.2 mg / L or 3.2 mg / L It was shown that water was obtained.

  In both Examples 3-1 and 3-2, the redox potential of the oxygen-dissolved water obtained by dissolving oxygen in the raw water was lowered, but this phenomenon was caused by the chlorine contained in the raw water. It is presumed that this was caused by volatilization.

Example 4 Production of Hydrogen-Dissolved Water Production Plant A hydrogen-dissolved water production plant for mass treatment was designed and produced for the purpose of obtaining a large amount of hydrogen-dissolved water. FIG. 9 shows a flowchart of the manufacturing apparatus. The manufacturing apparatus of FIG. 9 is an embodiment of the apparatus shown in FIG. 1B. Nitrogen gas is used when discharging the liquid in the tank, not the gas dissolved in the liquid.

The description of each part is as follows.
(01) Hydrogen supply valve (HHV11)
This is a part for opening the valve before the start of operation and preparing for the start of production.
(02) Hydrogen gas regulator (HHV12)
This is a part for finely adjusting the pressure of the hydrogen gas supplied from the hydrogen cylinder, and the gas normally supplied at 0.25 MPa is reduced to an arbitrary pressure.
(03) Hydrogen gas flow meter (HHV13, HF01)
This is a part for finely adjusting the flow rate of the hydrogen gas supplied from the hydrogen gas cylinder.

(04) Gas vent valve (HHV14)
This is a part for manually releasing the gas in the tank, and is normally set to OFF.
(05) Nitrogen supply valve (HHV15)
This valve is used to supply nitrogen gas used during forced drainage.
(06) Hydrogen gas solenoid valve (HAV11)
This valve is used to supply hydrogen gas at the time of replacement of the addition route and at the time of production, and it opens and closes automatically.
(07) Hydrogen gas solenoid valve (HAV12)
This valve is used to supply hydrogen gas at the time of tank hydrogen replacement and filling path hydrogen replacement, and automatically opens and closes.

(08) Tank adjustment solenoid valve (HAV13)
This valve is used for hydrogen replacement in HTA2 tank and HTA3 tank, pressure adjustment, etc., and automatically opens and closes.
(09) Gas vent solenoid valve (HAV14)
Valve for releasing gas when replacing the addition route or draining, and opens and closes automatically.
(10) Nitrogen gas solenoid valve (HAV15)
This valve is used to supply nitrogen gas for forced drainage and opens and closes automatically.
(11) Raw water supply valve (HHV51)
This is a valve for supplying raw water and is normally ON.

(12) Flow meter (HHV52, HF02)
This is the part for adjusting the amount of water supplied from the HPU01 pump to the HTA3 tank.
(13) Raw water supply electromagnetic valve (HAV51)
This is a valve for supplying raw water, and it opens and closes automatically during production.
(14) Hydrogen dissolved water supply solenoid valve (HAV52)
This valve is used to send hydrogen-dissolved water to the filling machine and automatically opens and closes. It also opens and closes automatically during filling route hydrogen replacement and CIP cleaning.

(15) Drainage solenoid valve (HAV53)
This valve opens and closes automatically when the production is finished or forced drainage, and drains. During CIP cleaning, it operates simultaneously with the set temperature check.
(16) Drainage solenoid valve (HAV54)
This valve automatically opens and closes when draining the HTA2 tank.
(17) Drainage solenoid valve (HAV55)
It is a valve that opens and closes automatically when draining water inside the HTA1 tank and HPU01 pump.
(18) Drainage solenoid valve (HAV56)
It is a valve that opens and closes automatically when draining in piping and filters.

(19) Vortex pump (HPU01)
It is a part that feeds raw water, mixes and stirs hydrogen gas supplied from the inlet side and raw water, and mixes hydrogen gas. In the case of this apparatus, the liquid inlet of this vortex pump is a gas-liquid mixing part, and gas is mixed with the liquid.
(20) Raw water storage tank (HTA1)
This is the part that temporarily stores the raw water supplied.
(21) Buffer tank (HTA2)
This tank is mainly used for adjusting the hydrogen gas pressure.

(22) Product storage tank (HTA3)
This tank mainly stores products sent from HPU01. The pressure in the tank is equivalent to atmospheric pressure.
(23) Liquid level switch (HTA1, HTA3)
This switch is used to control tank water supply and drainage, and is controlled by three switches, H, M, and L.
(24) Temperature sensor (HT01)
This is a part for measuring the temperature of hot water supplied to the HTA3 tank during CIP.

(25) Safety valve (HSAV01)
This valve is used to adjust the pressure inside the HTA2 tank and opens when the pressure inside the HTA2 tank exceeds the set value.
(26) Reactor part Liquid and hydrogen gas are brought into gas-liquid contact under pressure to dissolve hydrogen gas in the gas.
(27) Filter 20μ, 4.5μ
It is a part for removing impurities in raw water and hydrogen water.

(28) Vent filter
This is a part for removing dust from the air flowing into the HTA1 and HTA2 tanks.
(29) Sight glass This is a part for confirming the flow of liquid in the tube.
(30) Explosion-proof ventilation fan This is a part for discharging the air in the hydrogen dissolved water production equipment box.

(31) Hydrogen detector This part is for detecting hydrogen gas leaked from the hydrogen-dissolved water production system. When 2,000ppm is reached, the equipment stops.
(32) Air pressure regulator This is the part for adjusting the pressure of the air pressure for the electromagnetic valve to 0.4 MPa.

  In the apparatus shown in FIG. 9, the gas cylinder 25 of FIG. 1B is connected to the portion indicated by hydrogen on the left side of the drawing, and the raw material liquid container 21 of FIG. 1B is connected to the portion indicated by water. Moreover, the vortex pump shown by HPU01 corresponds to the pressurizing pump 23 of FIG. 1B, the gas-liquid mixing part 35 of FIG. 1B exists immediately upstream of the vortex pump, and hydrogen gas is mixed with water. Furthermore, the part shown by the reactor of the apparatus shown in FIG. 8 corresponds to the reactor unit 70 of FIG. 1B. The hydrogen-dissolved water exiting from the reactor section passes through a thin tube and is stored in an HTA3 tank corresponding to the gas-dissolved liquid receiver 31 in FIG. 1B.

  The apparatus shown in FIG. 9 can produce hydrogen-dissolved water in which hydrogen is dissolved in a supersaturated state even when water is flowed at a flow rate of 20 L / min using a reactor having an inner diameter of 1.1 cm. The production speed of dissolved water was 1.2 tons / hour.

It is a figure which shows an example of the continuous pressurization flow type gas dissolution liquid manufacturing apparatus of this invention. It is a figure which shows an example of the continuous pressurization flow type gas dissolution liquid manufacturing apparatus of this invention. It is a figure which shows an example of the continuous pressurization flow type gas dissolution liquid manufacturing apparatus of this invention. It is a cross-sectional view of the ejector used as a gas-liquid mixing part of the continuous pressurization flow type gas dissolution liquid manufacturing device of the present invention. It is a figure which shows an example of the gas-liquid mixing part of the continuous pressurization flow type gas dissolution liquid manufacturing apparatus of this invention. It is a figure which shows an example of the gas-liquid mixing part of the continuous pressurization flow type gas dissolution liquid manufacturing apparatus of this invention. FIG. 5A is a diagram showing a static mixer used as a reactor part of the continuous pressurized flow type gas dissolved liquid production apparatus of the present invention, FIG. 5A is a cross-sectional view of the static mixer, and FIG. 5B is a front view of a right twist element; 5C is a view obtained by rotating FIG. 5B by 90 °, FIG. 5D is a front view of the left twist element, FIG. 5E is a view obtained by rotating FIG. 5D by 90 °, and FIG. 5F is provided with a protruding structure. It is a figure which shows an element. It is a figure which shows an example of the continuous pressurization flow type gas dissolution liquid manufacturing apparatus of this invention which can melt | dissolve a some gas in a liquid. It is a figure which shows an example of the continuous pressurization flow type gas dissolution liquid manufacturing apparatus of this invention which can melt | dissolve a some gas in a liquid. It is a figure which shows the continuous pressurization flow type gas dissolution liquid manufacturing apparatus of this invention used in Example 1. FIG. It is a flowchart figure which shows the continuous pressurization flow type gas dissolution liquid manufacturing apparatus of this invention used in Example 4. FIG.

Explanation of symbols

11 Raw material liquid 12 Raw material liquid container 13 Pressurizing pump 14 Liquid distribution thin tube (liquid supply piping)
15 Gas cylinder 16 Valve 17 Pressure gauge 18 Gas supply pipe 19 Liquid distribution thin pipe (liquid recovery pipe)
20 Valve 21 Raw material liquid container (gas dissolved liquid receiver)
22 Raw material liquid (gas dissolved liquid)
23 Pressurizing pump 24 Liquid distribution thin tube (liquid supply piping)
25 Gas cylinder 26 Valve 27 Pressure gauge 28 Gas supply pipe 29 Liquid distribution thin pipe (gas dissolved liquid recovery pipe)
30 Valve 31 Gas dissolved liquid receiver 32 Gas dissolved liquid 35A, 35B Gas-liquid mixing part 36A, 36B Gas introduction path 37A, 37B of gas-liquid mixing part Gas introduction path 38A, 38B of gas-liquid mixing part Gas of gas-liquid mixing part Mixed liquid outlet 50, 50A, 50B Ejector 51B Ejector liquid inlet 55B Ejector liquid outlet 56B Ejector gas inlet 60B Static mixer 70A, 70B Reactor 71A, 71B Reactor inlet 72A, 72B Reactor outlet 100, 100 ′, 100 ″, 101, 102 Continuous pressurization flow type gas dissolution liquid production equipment

Claims (10)

A liquid flow line through which the liquid flows, and the raw material liquid is circulated to the gas-dissolved liquid receiver;
Pressurizing means provided in the middle of the liquid circulation pipe, pressurizing means for pressurizing the raw material liquid to circulate through the circulation pipe;
At least one gas-liquid mixing section provided in the middle of the liquid circulation pipe, which is connected to a gas container via a gas supply pipe, and gas-liquid mixing for mixing hydrogen gas from the gas container with the liquid Part,
At least one static mixer provided downstream of the gas-liquid mixing part in the middle of the liquid circulation pipe, maintaining the pressure of the gas mixed liquid mixed in the gas-liquid mixing part, and dissolving the gas in the liquid Promote static mixer,
An open-type continuous pressurized flow type hydrogen gas dissolving liquid production apparatus for producing a hydrogen gas dissolving liquid continuously while pressurizing and flowing the liquid through the liquid circulation pipe at a flow rate of 10 to 40 L / min.   The open-system continuous pressurized flow type hydrogen gas dissolving liquid production apparatus according to claim 1, wherein in the static mixer, the pressure applied to the liquid flowing through the static mixer is gradually reduced.   The open system continuous pressurization flow type hydrogen gas dissolution liquid manufacturing device according to claim 1 or 2 whose gas-liquid mixing part is an ejector.   The open system continuous pressurization flow-type hydrogen gas dissolving liquid manufacturing apparatus of any one of Claims 1-3 whose pressurization means is a pressurization pump.   The open-system continuous pressurized flow type hydrogen gas dissolving liquid manufacturing apparatus according to claim 4, wherein the pressurizing pump is a vortex pump, and is provided downstream of the gas-liquid mixing unit and upstream of the static mixer.   The open system continuous pressurization flow type hydrogen gas dissolution liquid manufacturing device according to any one of claims 1 to 5, wherein the gas-liquid mixing unit and the static mixer are directly connected.   The open system continuous pressurization flow type hydrogen gas dissolution liquid manufacturing device according to any one of claims 1 to 6 whose ratio of the length to the pipe inner diameter of a static mixer is 10 or more.   The open-system continuous pressurized flow hydrogen gas-dissolved liquid production according to any one of claims 1 to 7, wherein the pressure applied to at least one of the raw material liquid and the gas-dissolved liquid is equivalent to atmospheric pressure and is an open system. apparatus.   Open system continuous pressurization flow type hydrogen gas given in any 1 paragraph of Claims 1-8 which have two or more sets of a gas-liquid mixing part and a static mixer, and can dissolve a plurality of gas containing hydrogen gas. Dissolved liquid production equipment.   The open system according to any one of claims 1 to 9, wherein the liquid is selected from the group consisting of water, mineral water, tea, coffee, soft drinks, juices, gel drinks, cosmetics, shampoos and physiological saline. Continuous pressurized flow type hydrogen gas dissolved liquid production equipment.

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