JP2008093597A - Method of manufacturing dispersion and module for manufacture of dispersion - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a method and an apparatus for simple manufacture of a dispersion with small particle sizes of the dispersed phase and a narrow distribution of particle sizes and an inexpensive and small dispersion manufacturing apparatus with an energy consumption reduced. <P>SOLUTION: The fluid passage 10 is divided into the upstream and downstream sides with one or more sheets 2, and the division sheets 2 have at least one slit element 3. The slit element 3 consists of a slit 31 and a sheet portion 32 surrounding the slit 31, and the sheet portion is movable with a passing fluid. Two or more substances to form a dispersion are made to pass through the slit element(s) to form the dispersion. The invention provides a stable dispersion with no surfactant or only a small amount of a surfactant. <P>COPYRIGHT: (C)2008,JPO&INPIT

Description

  The present invention relates to a dispersion production method and a dispersion production module. The dispersion liquid in the present invention refers to a liquid in which other finely divided substances are scattered in the liquid, in which the fine liquid is dispersed in the liquid (emulsion), in the liquid. It includes those in which finely divided solids are dispersed (suspension) and those in which finely divided gas is dispersed in a liquid.

  The present invention also provides an O / W dispersion in which the dispersion medium (that is, the continuous phase) is an aqueous phase, a W / O dispersion in which oils and fats are a dispersion medium, and W obtained by redispersing a W / O dispersion in an aqueous phase. The present invention relates to a method capable of producing a dispersion in the form of a / O / W dispersion or an O / W / O dispersion obtained by redispersing an O / W dispersion in an oil phase.

  The present invention relates to resin dispersions used for adhesives, paints, electronic parts, cement additives, etc .; cosmetic dispersions such as creams; medical dispersions used for injections, poultices, transdermal drugs, etc .; milk O / W edible dispersion in which the continuous phase of dairy products such as yogurt, cream, cheese, etc., soy milk, mayonnaise, dressing, etc. is an aqueous phase; / O edible dispersion; W / O / W edible dispersion or O / W / O edible dispersion; for various uses such as W / O dispersion fuel in which water is dispersed in light oil, gasoline, heavy oil, etc. The present invention relates to a method for producing an applicable dispersion.

  Conventionally, to produce a dispersion, a high-speed rotary stirring homomixer, a high-speed shearing homogenizer, an in-line mixer that provides shearing while supplying a lot of twisted blades in the liquid supply pipeline, and ultrasonic waves Many emulsifiers are used.

  However, conventional stirring and shearing devices, ultrasonic emulsifiers, and the like are large and consume a large amount of energy.

  It is known that the properties of the dispersion greatly vary depending on the particle size of the dispersed phase. For example, in the case of a resin dispersion such as paint, the density of the paint film can be improved by a dispersion having a composite particle size distribution consisting of two types of particle size distributions whose average particle sizes differ by an order of magnitude. It is known that the adhesive force varies depending on the particle size of the adhesive. In the dispersion, the particle size distribution is also an important factor. For example, liquid crystal spacers used in liquid crystal display devices are resin particles separated from a dispersion, but liquid crystal spacers are required to have a uniform particle size. Even in dispersions for uses such as pharmaceuticals, agricultural chemicals, and cosmetics, the drug efficacy may change depending on the particle size distribution of the dispersed phase.

  In general, the smaller the particle size of the dispersed phase, the higher the stability for separating the dispersed phase. And there are many technical fields in which the particle size of the dispersed phase is required to be distributed at 1 μm or less. When producing a dispersion using a conventionally used turbo mixer, colloid mill, homogenizer, etc., the particle size distribution of the dispersed phase can be adjusted to some extent by adjusting the shearing force if the particle size of the dispersed phase is 1 μm or more. . However, when the particle size is 1 μm or less, it is quite difficult to obtain a narrow particle size distribution.

  In order to make the particle size of the dispersed phase uniform (to reduce the particle size distribution), it is known to filter the dispersed phase with a porous glass or a porous pipe. In some cases or when the liquid is a precipitate or is a contaminated liquid, there is a problem that the pores are clogged.

  In general, the dispersibility of the dispersion is better as the amount of the surfactant added is larger, and the stronger the shearing force applied to the dispersion, the better. However, if the content of the surfactant in the dispersion increases, the properties of the dispersion may change (for example, the surfactant may cause hygroscopicity in the performance of the resin). It is required to reduce the amount of addition of as much as possible.

  The background art in various technical fields is illustrated below.

(1) Background Art Related to Resin Dispersion Resin dispersions have various uses depending on the composition of the dispersed phase. Further, regarding the production of the dispersion, when the polymerization reaction is carried out in the dispersion, it may be produced without any problem from an economic or technical viewpoint, but there may be a problem.

  For example, a dispersion containing an ethylene-vinyl acetate copolymer has various uses such as an adhesive, a paint, and a cement admixture. When one monomer (monomer) constituting the copolymer is a gas like an ethylene-vinyl acetate copolymer, it is copolymerized with the vinyl acetate monomer via an aqueous phase forming a continuous phase. For this reason, the rate of dissolution of ethylene in water is rate-limiting. On the other hand, in order to increase the adhesion of the resin film when the resin dispersion is applied, it is necessary to increase the copolymerization ratio of ethylene. As described above, since the rate of dissolution of ethylene in water is rate-limiting in the polymerization reaction, in order to increase the copolymerization ratio in the dispersion, the pressure of ethylene in contact with the continuous phase is increased, or the ethylene dissolution rate is adjusted. It was necessary to lengthen the reaction time.

  There is a problem that such a product cannot be economically produced because an increase in the reaction pressure results in an increase in polymerization equipment costs, and a longer reaction time results in a decrease in operating rate.

  Furthermore, since these copolymers cannot remove heat of reaction due to an increase in viscosity, it is necessary to control the viscosity and reduce the particle size distribution of the resin in the dispersed phase. However, when a large amount of surfactant is used for this purpose, there is an adverse effect that the water resistance of the resin film is lowered, and a solution is required.

(2) Background art related to dairy products In order to prevent separation of fats in dairy products, particularly milk and creams with a fat content of 50% or more, the particle size of the dispersed fats, etc. should be reduced. It is known that it is necessary to homogenize at 1 μm or less.

Various techniques have been proposed for homogenization. For example, in Japanese Patent Application Laid-Open No. 10-201386 (Patent Document 1), a dairy product made of a fatty liquid is a multi-stage nozzle at a pressure of 10 to 100 bar (about 10 to 100 kgf / cm ² ), preferably 20 to 80 bar. A method of homogenizing a volume-related particle size of up to 90% to a fat particle size of 0.1 to 1 μm by passing through a dispersing device at a speed of 10 to 200 m / sec without particles exceeding 4 μm. It is disclosed.

  However, the method of Patent Document 1 uses a nozzle dispersion device provided with a large number of pores having a hydraulic diameter of 0.1 to 1 mm. However, these many pores are clogged because of their small diameter. There is a problem that clogging is likely to occur, particularly when the pressure is lower than 20 bar. In order to increase the intake of calcium, calcium carbonate is often added to dairy products. However, since the liquid passes through pores having a hydraulic diameter of 0.1 to 1 mm at high speed, If there is an abrasive material such as calcium, there is a problem that the pores of the nozzle are heavily worn. Furthermore, in the method of Patent Document 1, it can be seen that at least 10% or more of particles having 1 to 4 μm are present, and that the particle size distribution is considerably wide from the average particle size of the examples.

Japanese Patent Laid-Open No. 2003-180243 (Patent Document 2) discloses a method of homogenizing a mixture containing milk and an emulsifier to 1 μm or less at a pressure of 25 MPa (about 250 kgf / cm ² ) or more. In the method of Patent Document 2, an increase in the temperature of milk due to high energy is inevitable, and there is a problem that the flavor of milk is impaired. Moreover, since milk with a high working pressure and a small amount of processing needs to use a multistage reciprocating pump, there is a problem that the equipment cost is high and the maintenance is complicated with a complicated structure.

Japanese Patent Application Laid-Open No. 2004-249289 (Patent Document 3) disperses oil, calcium, and the like together with milk, water, and the like through a small hole and a long hole with a pressure of 200 MPa (about 2000 kgf / cm ² ). An atomization device is disclosed. However, in the apparatus of Patent Document 3, the opening area of the nozzle (small hole) is constant, and therefore the pressure (differential pressure) applied to the nozzle is proportional to the square of the flow rate through the nozzle, so that the fluid can pass through the nozzle at high speed. Requires extremely high pressure. For this reason, since the nozzle itself needs a pressure resistance of 2000 kgf / cm ² , it has a large and firm structure. Furthermore, when the pressure is made constant by the high-pressure pump, the flow rate is limited by the number of nozzles, so the operating conditions are limited to a very narrow range of “high pressure and constant flow rate”.

  Furthermore, both methods of Patent Document 1 and Patent Document 2 have a drawback that the fluctuation range of the operating pressure and the flow rate is remarkably limited.

  On the other hand, consumers are also demanded to prevent aroma and taste changes due to oxidation in edible dispersions such as milk. Japanese Agricultural Chemistry Journal Vol. 77, no. 9, 2003. According to P46 (Non-Patent Document 1), for example, in the case of milk, flavor and taste are inhibited by an oxidation reaction caused by a temperature increase during sterilization or a temperature increase in a homogenization facility by dissolved oxygen of about 10 PPM in raw milk. . In order to prevent this, it is described that it is necessary to reduce dissolved oxygen, which is usually present in about 10 PPM in raw milk, to about 2.5 PPM. Furthermore, as a countermeasure, a method is described in which nitrogen gas is mixed with raw milk with a static mixer, dissolved oxygen in milk is transferred into nitrogen gas, and then nitrogen gas is separated in a defoaming tank.

  However, in general, static mixers require a large amount of nitrogen gas due to a decrease in gas mixing efficiency. As a result, a large amount of bubbles are generated due to excess nitrogen gas, resulting in a large defoaming tank and high construction costs. Economic deoxygenation is difficult to achieve with the above method.

  When the gas is absorbed into the liquid, the method using the static mixer or the disper mixer described above has a poor absorption efficiency and a lot of gas is wasted. In addition, the method of ejecting gas from fine pores such as porous glass is excellent in absorption efficiency, but because the pores of porous glass are likely to be clogged, it cannot be used for suspensions or contaminated liquids. There are drawbacks.

  In Japanese Patent No. 3091552 (Patent Document 4), in a method of reducing dissolved oxygen in milk by replacing with nitrogen gas, means for directly mixing and dispersing nitrogen gas, and milk not mixed with nitrogen gas are disclosed. A method is disclosed in which means for spraying with a nozzle from above a tank stored in a nitrogen gas atmosphere is used in combination. According to Patent Document 4, when 40-50% nitrogen gas is mixed with milk using a static mixer, foaming occurs, and about 1/3 of the total is foamed. However, it is described that the tank can be made small by using milk spray together with a nozzle from above the tank to eliminate bubbles.

(3) Background Art Related to W / O / W or O / W / O In the W / O / W dispersion form in which the W / O dispersion is redispersed in an aqueous phase, an aqueous dispersion in the W / O dispersion Needs to have a particle size that is an order of magnitude smaller than the particle size of the W / O dispersion to be dispersed in the W / O / W dispersion. The same applies to an O / W / O dispersion obtained by redispersing the O / W dispersion in an oil phase. For this reason, the particle size distribution structure of the entire dispersion is extremely important.

  The dispersion of W / O / W or O / W / O has an advantage that a food containing a substance beneficial to health such as a plant sterol, a bad-tasting drug, or the like can be added regardless of the taste of the food. However, since phase transition is likely to occur, there are many restrictions on the selection of the surface-active substance and the raw material composition, and the degree of freedom has been greatly limited. For this reason, a dispersion method in which phase transition hardly occurs is desired.

(4) Background Art Related to Fuel Oil Fuel when fuel such as gasoline, light oil, heavy oil, etc. used in engines and boilers for automobiles, ships, and power generation is injected into the engine or burned by a boiler burner. In addition, it is known that when about 20% of water is added as fine particles of 1 μm or less, NOx in the exhaust gas is reduced and the fuel efficiency is improved by about 20%. In this case, if there are particles of 1 μm or more, the evaporation rate of water particles slows down, and the combustion efficiency is greatly reduced. Therefore, the particle size of the dispersed phase is an important factor. However, an apparatus that disperses water with a narrow particle size distribution of 1 μm or less is expensive, heavy, and severely constrained in operating conditions. It is necessary to use a surfactant for the stability of the water suspension fuel.

For this reason, it is necessary to select a surfactant suitable for the crude oil or fuel oil refining method used as the fuel oil raw material. Also, there are problems such as emulsion fuel stability in cold regions, problems with the engine due to the flammability of the surfactant, and economic problems due to the cost of the surfactant. In practice, a dispersion fuel in which water is dispersed is hardly used.
Japanese Patent Laid-Open No. 10-201386 JP 2003-180243 A JP 2004-249289 A Japanese Patent No. 3091752 Japanese Agricultural Chemistry Journal Vol. 77, no. 9, 2003. P46

  An object of the present invention is to solve the conventional problems described above and to provide a method and an apparatus for easily producing a dispersion having a small dispersed phase particle size and a narrow particle size distribution. Another object of the present invention is to provide a dispersion manufacturing apparatus that is inexpensive and small in size and consumes little energy.

  It is an object of the present invention to provide a dispersion production method and apparatus that can produce a stable dispersion even if no surfactant is used or only a small amount is used. It is another object of the present invention to provide a dispersion production method and apparatus that can uniformly disperse any of gas, liquid, and solid as a dispersed phase in a liquid in the form of fine particles and can be applied to a wide technical field.

  In the present invention, the fluid passage is partitioned into one or more sheets by one or a plurality of sheets, and one or more slit elements are formed on the partition sheet. The surrounding sheet portion is movable by a fluid passing therethrough, and two or more kinds of substances constituting a dispersion are caused to flow through the passage so that the two or more kinds of substances are combined together. The object is achieved by a method for producing a dispersion characterized in that the dispersion is obtained by passing through a slit element.

  In this case, the pressure difference between the upstream side and the downstream side of the partition sheet is preferably 3 MPa or less, and more preferably 1 MPa or less.

  When flowing two or more substances constituting the dispersion into the passage, each substance may be poured simultaneously without being mixed in advance, but after mixing two or more substances constituting the dispersion in advance, It is preferable that the slit element is passed through the passage.

  Substances constituting the dispersion liquid may be a liquid and a gas, the liquid may be a dispersion medium, and the gas may be a dispersion phase. In this case, the liquid serving as a dispersion medium may be a liquid in which one or more types of gas are dissolved, and the gas serving as a dispersed phase may be a gas inert to at least one type of gas dissolved in the liquid. .

  In the method of the present invention, two or more kinds of substances constituting the dispersion liquid are dairy products or soy milk, and other substances are one or more kinds of substances whose components are different from those of the main substance. Applicable to some. Other substances include dairy products, soy milk, vegetable oil, calcium compounds, fruit juice, cocoa, emulsifiers, and the like, which are components different from the main dairy products or soy milk.

  The method of the present invention can also be applied to a material in which the dispersion medium in the dispersion is fuel oil and the main component of the dispersion phase is water.

  In the method of the present invention, the substance constituting the dispersion is at least water and a polymerizable monomer, and the substance is passed through a slit element to form a dispersion, and the polymerizable monomer is polymerized in the dispersion. It can be applied to the case where a polymerized synthetic resin is used as a dispersed phase.

  Further, in the method of the present invention, the substance constituting the dispersion is a gas mixture of a polymerizable monomer and a liquid containing a polymerizable monomer, and the both substances are passed through a slit element to form a dispersion, The present invention can also be applied to the case where the polymerizable monomer and the polymerizable gas mixture are polymerized in a dispersion and the polymerized synthetic resin is used as a dispersed phase. In this case, when the monomer as a gas mixture is a mixture containing ethylene and the monomer as a liquid is a mixture containing vinyl acetate, a dispersion containing an ethylene-vinyl acetate copolymer can be produced.

  The present invention is a module that is arranged in a passage through which two or more substances constituting the dispersion flow together and divides the passage into an upstream side and a downstream side, and the module is formed with one or more slit elements. Each of the slit elements comprises a slit and a sheet portion around the slit, and the peripheral sheet portion is movable by a fluid passing therethrough, and the object is achieved by the module for manufacturing a dispersion liquid. To achieve.

  It is preferable that the slits of the slit element extend radially from the center in a plurality of directions.

  Moreover, it is preferable that a plurality of slit elements are formed on one sheet.

  One sheet having the slit element may be arranged flat so as to partition the passage through which the fluid flows. However, the one sheet having the slit element is cylindrical or conical, and the cylindrical or The fluid may be configured to flow between the inside and the outside of the cone.

  A plurality of sheets having slit elements are preferably arranged in a flat state or in a cylindrical shape or a conical shape and spaced apart.

  Further, a single sheet having slit elements may be wound spirally, and the layers of the spiral may be spaced apart.

  The sheet having the slit element of the present invention is made of metal, plastic or rubber.

  According to the present invention, by simply passing two or more substances constituting the dispersion together through a slit element provided on a metal or plastic sheet, the dispersion phase has a small particle size and a narrow particle size distribution. The liquid can be easily manufactured.

  The slit element of the present invention comprises a slit formed in a plastic, rubber or metal sheet and a sheet portion around the slit. The sheet portion around the slit is a small-area sheet portion having the slit as one or two sides thereof, and has such rigidity that the side formed by the slit can be moved by the fluid passing therethrough as a free end portion. Therefore, the slit element of the present invention can be formed only by providing an appropriately shaped slit suitable for the thickness and material of the sheet.

  According to the present invention, the slit element has substantially no gap in a state where no fluid passes, and the slit is in a closed state. When the fluid passes, the sheet portion around the slit is bent by the pressure of the fluid. A slight gap is generated, and the slit is opened. By preparing a plurality of sheets in which the rigidity of the sheet portion around the slit is different, a dispersion liquid having a desired particle diameter can be easily produced. In this case, the higher the rigidity, the finer the dispersed phase.

  The conventional nozzle has a constant opening area, and the pressure (differential pressure) applied to the nozzle is proportional to the square of the flow rate through the nozzle. Therefore, a very large pressure is required to pass the fluid through the nozzle at a high speed. On the other hand, according to the present invention, the operating slit element is deformed according to the flow velocity and the sheet portion around the slit vibrates, so that the pressure (differential pressure) applied to the surface is 1 to 0.6th power. It only increases in proportion to And if it is the same slit, a particle size distribution will hardly change with flow volume fluctuations. That is, since the ranges of pressure and flow rate are not limited, the present invention can automatically cope with fluctuations in operating conditions such as the treatment flow rate, and is economical. Moreover, a high-pressure pump is not necessary, and a small pump with a small capacity and a low head can be used. The energy cost and the construction cost are remarkably superior to the conventional method.

  According to the present invention, the sheet portion around the slit does not close because the slit vibrates despite a minute interval, and has a self-cleaning function even if it is closed.

  The dispersion liquid production module of the present invention is composed of a sheet having such a slit element, and the sheet merely partitions the passage through which two or more substances constituting the dispersion flow together into an upstream side and a downstream side. Therefore, it has an extremely simple structure, is inexpensive and is small. Moreover, the pressure difference between the upstream side and the downstream side of the partition sheet is a low pressure of 3 MPa or less, and the energy consumption is small.

  According to the present invention, since the dispersed phase can be made into fine particles of 1 μm or less, a stable dispersion can be obtained even if no surfactant is used or only a small amount is used. In addition, any of gas, liquid and solid as a dispersed phase in the liquid can be uniformly dispersed in the form of fine particles, and can be applied to a wide technical field.

  According to the present invention, when a gas is used as a dispersed phase, the dispersed phase can be in the form of fine particles of 1 μm or less, the gas can be dispersed in the liquid, and the gas can be absorbed by the liquid. Therefore, even when one monomer constituting the copolymer is a gas, such as an ethylene-vinyl acetate copolymer, it is easy to increase the copolymerization ratio of the monomer that is a gas. It is possible to economically produce a resin dispersion with an increased gas copolymerization ratio.

  Further, the inert gas can be dispersed in the liquid by passing the liquid in which the gas is dissolved and the inert gas through the slit element of the present invention. Then, after the dissolved gas in the liquid is transferred into the inert gas in a dispersed state, the dissolved gas can be removed from the liquid by defoaming. When the present invention is applied to milk, the amount of nitrogen gas (inert gas) necessary for dispersion with fine bubbles is as small as about 13% on a volume basis, and foaming is about 1/20 of the whole. Therefore, the equipment is small and the amount of nitrogen gas is small, so that dissolved oxygen in milk can be easily and economically separated. Thus, according to the present invention, dissolved oxygen in milk can be easily removed, and the flavor and taste of milk can be improved.

  Furthermore, the particle size distribution of the dispersed phase of the raw material can be changed by passing the raw material as the dispersion through the slit element of the present invention. For example, it is possible to homogenize the particle size of the fat and the like dispersed in order to prevent separation of fats such as milk and cream having a fat content of 50% or more at 1 μm or less.

  By passing a mixture of dairy product or soy milk and a component other than the above components (for example, at least one kind of dairy product, soy milk, butter, vegetable oil, calcium compound, emulsifier) through the slit element of the present invention, the dairy product or soy milk It can be set as the dairy product or soymilk containing ingredients other than.

  In order to use a fuel oil (gasoline, light oil, heavy oil, kerosene, etc.) as a dispersion medium and a water-based liquid as a dispersed phase, it has been necessary to use a considerable amount of surfactant in the past. However, according to the present invention, a liquid containing water as a main component can be dispersed as fine particles in the fuel oil even when almost no surfactant is used, and thus a dispersion fuel containing water can be produced. In addition, since the dispersion device can be made extremely small, the dispersion fuel can be manufactured on-vehicle or on-site.

  A polymerizable monomer mixture is passed through the slit element of the present invention to form a polymerizable monomer dispersion, and then the dispersion is polymerized to produce a synthetic resin dispersion composed of solid fine particles. Can do. In this case, according to the present invention, the particle diameter of the synthetic resin can be easily reduced to 1 μm or less.

  Hereinafter, the present invention will be described in detail based on the embodiments shown in the drawings. FIG. 1 is a cross-sectional view along a flow direction showing a fluid passage provided with an embodiment of a module for producing a dispersion of the present invention. FIG. 2 is a sectional view taken along line II-II in FIG.

  In FIG. 1, two or more substances constituting the dispersion are caused to flow together in the direction of arrow A through the passage 10 in the pipe 1. The dispersion manufacturing module M is disposed in the passage 10, and the passage 10 is partitioned by the module M into an upstream side and a downstream side. In this embodiment, the module M is a sheet 2 made of metal, plastic or rubber, and one slit element 3 is formed at the center of the sheet 2 as shown in FIG. In the embodiment of FIG. 1, the sheet 2 is disposed between the pipe 11 and the pipe 12 so as to block the flow passage 10, and no liquid leaks directly or through the ring-shaped seal 14 to the flange portion 13 of the pipe 11 and the pipe 12. As shown, the bolt 15 and the nut 16 are attached.

  The sheet 2 is not particularly limited with respect to the material, but for example, the following is suitable.

  The metal sheet is preferably made of an iron alloy such as stainless steel or spring steel, a copper alloy such as phosphor bronze or brass, an aluminum alloy, a nickel alloy, a titanium alloy, or the like and having moderate elasticity.

  Plastic sheets include general-purpose resins such as polyethylene and polypropylene, vinyl chloride resins such as polyvinyl chloride, fluorine resins such as polytetrafluoroethylene (registered trademark is Teflon), ABS resins, polyamides, polycarbonates, polyacetals, Engineering resins such as PET and polysulfone, thermosetting resins such as phenolic resins, epoxy resins and unsaturated polyester resins, and mixing or pasting these resins, or carbon fibers, glass fibers, nano A sheet made of a composite material filled with a filler such as a substance, a composite material of metal and plastic, or the like, and preferably has elasticity, wear resistance, and chemical resistance.

  The rubber sheet is preferably a rubber such as polybutadiene rubber, isoprene rubber or styrene butadiene rubber, which has elasticity, wear resistance and chemical resistance.

  Further, the surface state of these metals and plastics may be subjected to a surface treatment such as plating to adjust the interfacial tension with the liquid as a dispersion.

  The slit element 3 in the present invention comprises a slit 31 formed in a plastic sheet, a metal sheet or a rubber sheet and a sheet portion 32 around the slit. The sheet portion 32 around the slit is a small-area sheet portion having the slit 31 as one or two sides thereof, and has such rigidity that the side formed by the slit 31 can be moved by the fluid passing therethrough as a free end.

  The slit element 3 of the present invention has substantially no gap in a state where no fluid passes, and the slit 31 is in a closed state. When the fluid pressure is applied to the surface when the fluid passes, the sheet around the slit is formed. The portion 32 is bent to form a slight gap, the slit 31 is opened, and the fluid can pass therethrough.

  The slit element 3 in the embodiment shown in FIG. 2 includes three slits 31 and three sheet portions 32 extending in three directions from the center. Each sheet portion 32 is a portion surrounded by two slits 31, and a portion between the two outer ends 31 a of the two slits 31 is continuous with the main body of the sheet 2. Accordingly, in this embodiment, the sheet portion 32 that is movable by the fluid passing therethrough is substantially triangular or substantially fan-shaped.

  FIG. 3 is a front view showing various embodiments of the slits 31 formed in the sheet 2. The slit 31 may be a straight line or a curved line. The slits 31 preferably extend from the center in a plurality of directions as shown in (b), (c), (d), (g), (h) and (i) of FIG. Moreover, it is good also as a shape which provided the short slit 31a extended in another direction in the edge part of each slit 31 like (f), (g), (h), (i), and (j) of FIG. The slit 31 of the present invention is not limited to the embodiment shown in FIG. Further, the number of sheet portions 32 varies depending on the number of slits 31. For example, the number of sheet portions 32 in FIG. 3B is three, and the number of sheet portions 32 in FIG. 3C is four.

  FIG. 4 is a front view showing another embodiment of the seat 2. In this embodiment, three slit elements 3 are formed on one sheet 2. Moreover, the attachment hole 21 is provided in the sheet | seat 2, and the location corresponding to the channel | path 10 when it attached to the pipe 1 was shown with the virtual line (two-dot chain line). When the sheet 2 is arranged so as to partition the passage 10 as shown in FIG. 1, the fluid flowing through the passage 10 flows from the upstream side to the downstream side through the three slit elements 3.

  FIG. 5 is a sectional view in the flow direction showing another embodiment of the module M of the present invention. In FIG. 5, two or more substances constituting the dispersion flow in the direction of arrow A in the passage 10 in the pipes 11 and 12 together. The dispersion liquid producing module M is disposed in the passage 10, and the passage 10 is partitioned by the module M into an upstream side and a downstream side. In the module M of this embodiment, three sets of combinations of the sheet 2 and the support body 41 that carries the sheet 2 are provided. Each sheet 2 is formed with one or a plurality of slit elements 3, and a corresponding support body 41 is formed with a hole 42 larger than the slit element 3 at a position corresponding to each slit element 3. .

  As shown in FIG. 5, the support 41 that supports the seat 2 has an outer peripheral portion sandwiched between two end ring bodies 43 and 45 and two intermediate ring bodies 44 and 44. The end ring body 43 or 45 and the intermediate ring body 44 and the intermediate ring body 44 and the intermediate ring body 44 are screwed together and integrated so as not to leak. The end ring bodies 43 or 45 have flange portions 43a and 45a, respectively, and are attached to the flange portion 13 of the pipe 11 or the pipe 12 so as not to leak liquid directly or via the ring-shaped seal 14, respectively. When a fluid flows through the passage 10 in the direction of arrow A, the fluid sequentially passes through the hole 42 of each support 41 and the slit element 3 of the sheet 2.

  In this embodiment, since the sheet 2 is supported by the support body 41, the sheet 2 is not loosened even when the sheet 2 has a large area and a small thickness. Further, in this embodiment, the support body 41 is provided only on one side of the sheet 2, but the thickness of the support body 41 is reduced and the hole 42 is made sufficiently large to adversely affect the movement of the sheet portion 32 of the slit element 3. In other words, the support body 41 may be provided on both sides of the sheet 2 so that the sheet 2 is sandwiched between the two support bodies 41.

  Furthermore, in the module M of the embodiment of FIG. 5, the number of sheets 2 is three, but the number is not limited to this number, and may be two or may be easily increased to four or more by increasing the number of intermediate ring bodies 44. it can.

  6A is a sectional view in the flow direction showing still another embodiment of the module M of the present invention, and FIG. 6B is a perspective view of the module M shown in FIG. In this embodiment, as shown in FIG. 6B, the sheet 2 has a cylindrical shape, and a plurality of slit elements 3 are formed on the peripheral surface thereof. One end of the cylindrical shape is attached to the ring body 51, and the other end of the cylindrical shape is closed by a disc 52. As shown in FIG. 6A, the ring body 51 is attached so as not to leak into the pipe 11 and the pipe 12.

  In this embodiment, when the fluid is flowed in the direction of arrow A, the fluid enters the inside of the cylindrical sheet 2 from the pipe 11 and passes through the slit element 3 provided on the peripheral surface of the cylindrical sheet 2 so that the pipe 12 It flows to. Thus, also in this embodiment, the passage 10 is partitioned by the sheet 2.

  In the embodiment of FIG. 6, the fluid flows from the inside of the cylindrical sheet 2 to the outside, but conversely, it flows from the outside of the cylindrical sheet 2 to the inside through the slit element 3 provided on the peripheral surface. It may be.

FIG. 7 is a sectional view in the flow direction showing another embodiment of the module M of the present invention.
In this embodiment, the sheet 2 has a conical shape, and a plurality of slit elements 3 (not shown) are formed on its peripheral surface. One end of the conical shape is attached to the ring body 51, and the ring body 51 is attached so as not to leak into the pipe 11. In this embodiment, when the fluid is flowed in the direction of arrow A, the fluid enters the inside of the conical sheet 2 from the pipe 11 and passes through the slit element provided on the peripheral surface of the conical sheet 2 to the pipe 12. And flow. The fluid flow direction may be reversed.

  FIG. 8 is a perspective view of another embodiment of the module M of the present invention. In this embodiment, a plurality of cylindrical sheets 2 are arranged concentrically at intervals. Each sheet 2 is provided with a plurality of slit elements 3. As in the embodiment shown in FIG. 6, this module M has one end supported by a ring body, the other end closed by a disk, and placed in the flow path, so that the fluid flows on each cylindrical peripheral surface. It suffices to pass through the formed slit element 3 from the inside of the cylindrical shape to the outside, or vice versa.

  FIG. 9 is a front view of still another embodiment of the module M of the present invention. In this embodiment, a rectangular sheet 2 having a plurality of slit elements is spirally wound, and spacers 55 are provided between the spiral layers so that the spiral layers are spaced apart. ing. This module M is arranged in the passage 10 through which the fluid flows in the same manner as in the embodiment of FIG. 6, and the fluid passes through a slit element formed in the peripheral surface of the spiral, from the inside of the spiral to the outside, or vice versa. Circulate from outside to inside.

  As shown in the above embodiments, in the present invention, the sheet 2 is not limited to the circular shape as shown in FIGS. 2 and 4, and may be a shape that matches the shape of the passage 10 and the shape of the attachment portion. Further, as long as the seat 2 has a function of partitioning the passage 10 into the upstream side and the downstream side, the shape is not limited to a flat shape, and may be a cylindrical shape shown in FIG. 6 or a conical shape shown in FIG. Also good. Further, as shown in FIGS. 5 and 8, a plurality of sheets 2 having the slit elements 3 may be arranged at intervals, or as shown in FIG. 9, a single sheet 2 wound spirally. May be arranged at intervals.

  In the present invention, the slit element 3 formed on one sheet 2 may be one or plural (the number is not particularly limited), and in the case of plural, all the slit elements 3 may have the same shape. Alternatively, a combination of slit elements 3 having different shapes may be used.

  As described above, in the slit element 3 of the present invention, when the fluid pressure is applied to the surface when the fluid passes, the sheet portion 32 around the slit is bent to form a slight gap, and the slit 31 is opened. The structure allows fluid to pass through, but the gap is not constant. That is, when the pressure applied to the surface increases, the sheet portion 32 bends in the direction in which the slit 31 opens, and when the pressure decreases, the sheet portion 32 moves in the direction in which the slit 31 closes. The pressure applied to the surface of the slit element 3 is the difference between the pressure on the upstream side and the pressure on the downstream side (differential pressure), but when the fluid flows between the deflected sheet portions 32, the turbulence generated on the downstream side When the pressure difference fluctuates due to flow, cavitation, etc., and the sheet portion 32 once bent in the opening direction returns to the closing direction, it is repeated that the sheet portion 32 is bent again in the opening direction due to the pressure of the flowing fluid. The portion 32 vibrates.

  The higher the rigidity of the sheet portion 32 of the slit element 3, the higher the pressure (differential pressure) applied to the surface, and the higher the frequency, and conversely, the lower the rigidity of the sheet portion 32, the pressure applied to the surface ( The differential pressure) and the frequency are low.

  The rigidity of the sheet portion 32 of the slit element 3 varies depending on the material and thickness of the sheet 2 and the size and shape of the slit 31. The rigidity of the sheet portion 32 of the slit element 3 increases as the rigidity of the material of the sheet 2 increases, and increases as the thickness of the same material increases. Further, in the sheet 2 having the same material and thickness, the smaller the size of the slit 31, the higher the rigidity. Regarding the shape of the slit 31, for example, the sheet portion 32 of FIG. ), The rigidity is higher than that of the sheet portion 32. Therefore, the slit element 3 of the present invention can be formed only by providing a slit having an appropriate shape suitable for the thickness and material of the sheet.

  In the present invention, the thickness of the sheet varies depending on the material, but is preferably about 0.1 mm to 10 mm. Moreover, it is preferable that the size of each slit element (a width that includes all the slits) is about 4 mm to 50 mm in diameter.

  Although the mechanism by which fine particles are generated by the present invention is not clear, it is thought that the vibration of the sheet portion 32 also contributes. From the experimental results, a dispersion having a smaller dispersed phase particle size and a smaller particle size distribution is obtained when the rigidity of the sheet portion 32 is higher, and a dispersed particle having a larger particle size of the dispersed phase is obtained when the rigidity is lower. A large dispersion is obtained. By preparing a plurality of sheets 2 having different rigidity of the sheet portion 32 and exchanging the sheets 2, a dispersion liquid having a desired particle diameter can be easily obtained.

  Further, if the amount of fluid passing through the slit element 3 increases, the slit 31 opens, but if the amount of fluid passing excessively increases, the metal, plastic, or rubber constituting the sheet portion 32 is plastically deformed, The slit 31 cannot be closed. Accordingly, in the present invention, it is necessary to flow the fluid within a range where the sheet portion 32 does not undergo plastic deformation, that is, within a range within the elastic limit of the sheet portion 32, thereby determining the maximum flow rate. Further, the minimum flow rate that passes through the slit element 3 is determined by the setting of the gap of the slit, and is the minimum amount that can bend the sheet portion 32 of the slit element 3 to widen the gap of the slit 31.

  In the present invention, the module M (sheet 2) is divided into an upstream side and a downstream side, but the sheet portion 32 of the slit element 3 is bent and the gap of the slit 31 is widened to allow fluid to pass therethrough. And the pressure difference between the upstream side and the downstream side can be reduced. In the present invention, the module M (sheet 2) is preferably used in a state where the pressure difference between the upstream side and the downstream side is 3 MPa or less, and more preferably 1 MPa or less.

  In the present invention, when the passage flow rate is changed using the same slit, the differential pressure of the slit increases only in proportion to the 1st to 0.6th power of the flow rate, even if the flow rate passing through the slit changes. The particle size distribution is almost unchanged. This is because the sheet portion 32 of the slit element 3 is movable in accordance with the flow rate and flow velocity. On the other hand, in the conventional nozzle type device, the opening area of the nozzle is constant, and therefore the pressure (differential pressure) applied to the nozzle is proportional to the square of the flow rate through the nozzle, so that the fluid passes through the nozzle at a high speed. Required extremely high pressure.

  In addition, as shown in FIG. 5, even if a plurality of sheets 2 having the slit elements 3 are passed in the flow direction, the particle size distribution may not change or the particle size may rather increase due to re-collision. However, when a large number of slit elements 3 are provided on one sheet 2 as in the embodiment of FIG. 4, a part of these slit elements 3 is damaged or deformed for some reason. In consideration of the above, arranging the sheets 2 in the flow direction has an effect of increasing the reliability of the entire module M.

  The method and apparatus of the present invention can be applied to various technical fields. As an example, the present invention is applied to the case where gas is absorbed in a liquid, and the gas itself can be finely divided, so that stable gas absorption can be achieved with a minimum <gas / liquid> ratio. Since the sheet portion 32 of the slit element 3 of the present invention has a function of self-cleaning the blockage by vibration, it can be used industrially even if the liquid is a deposit, a turbid liquid, or a dispersion. . Furthermore, since supersaturated oxygen water can be produced with a simple apparatus as exemplified in Example 8, it is most suitable for oxidation of sewage in water and has extremely excellent economic characteristics from an industrial viewpoint.

  The present invention can be applied when other components are mixed with dairy products or soy milk. That is, a modified edible dispersion containing other components can be produced by mixing components other than the above components with dairy products or soy milk and passing them through the slit element of the module M of the present invention.

  Other ingredients to be mixed with dairy products or soy milk here are dairy products, soy milk, butter, olive oil, corn oil, safflower oil, peanut oil, sunflower oil, grape seed oil, canola oil, cottonseed oil, soybean oil, wheat Germ oil, rapeseed oil, oat oil, calcium carbonate, calcium phosphates, calcium citrate, hydroxyapatite, coffee, cocoa, green tea, fruit juice, lanolinic acid, sucrose fatty acid ester, polyglycerin fatty acid ester, pectin, agar, starch, Sucrose, a salt, and a mixture containing at least one of these.

  The present invention can also be applied to fuel oil reforming. By passing fuel oil such as gasoline, light oil, heavy oil and water used for engines, boilers for automobiles, ships, power generation and water through the slit element of the module M of the present invention, water as a dispersed phase is 1 μm or less and A dispersion fuel with a narrow particle size distribution can be produced. Since the module M of the present invention is small, the dispersion fuel can be easily produced on-vehicle or on-site.

  In general, when the particle size of the dispersed phase is dispersed to 1 μm or less, it is difficult to separate. Therefore, according to the present invention, the dispersion can be kept stable for several minutes without adding a surfactant. Since the module M of the present invention can be used even when the differential pressure is low, it can be applied even when using a small pump with a small capacity and a low head such as an injection fuel pump of an engine, and the fuel consumption fluctuates greatly. Even in this case, it is possible to stably produce a dispersion fuel in which water is dispersed with a particle diameter of 1 μm or less.

  For this reason, when producing dispersion fuel on-board or on-site and using it for an engine, etc., the instability of the dispersion can be ignored, and the cost of the surfactant can also be ignored. Down can be expected and NOx can be significantly reduced.

  Further, since the sheet portion 32 of the slit element 3 of the present invention vibrates when the fluid passes therethrough, it has a self-cleaning function and is stable even if an adhering substance such as heavy oil is present in the fuel. Driving can be expected.

  When using the dispersion fuel produced in a loaded state according to the present invention as a fuel for a diesel engine or a gasoline engine, it is preferable to add alcohols or glycols to water in order to prevent freezing of water. The dispersion also increases stability due to the active effect.

  If a combustible surfactant is added to the continuous phase, or a combustible surfactant other than water is added to the dispersed phase, the particle size may become smaller or the particle size distribution may become narrower. Therefore, there is an advantage that the stabilization time of the dispersion becomes long. However, since this increases the cost, it is preferable to add as little as possible.

  In addition, when manufacturing the dispersion fuel in a loaded state according to the present invention, the engine is started with the normal fuel without using the dispersion fuel at the start-up, the engine is stable after the start-up, and the temperature of the water to be used becomes an appropriate temperature. The cycle operation in which the fuel is switched to the dispersion fuel at the time of stopping and the normal fuel is used again at the time of stoppage can be easily performed by turning on and off the water pump as the dispersion phase, for example. An apparatus for producing dispersion fuel in a loaded state is composed of a pump that is compact enough to be loaded on a vehicle, has a low lift, and a small capacity, and uses the dispersion production module M of the present invention as part of the system. The equipment to be loaded is not limited to automobiles, but is loaded or used on-site, for example, on ships such as fishing boats and cargo ships, engine generators, heaters, small boilers, construction machinery, engine pumps, and farm equipment. Also included.

  The module M of the present invention can also be applied to the production of W / O / W dispersions and O / W / O dispersions. In the W / O / W dispersion form in which the W / O dispersion is re-dispersed in the aqueous phase, the aqueous dispersion in the W / O dispersion is the W / O dispersion to be dispersed in the W / O / W dispersion. The particle size must be smaller than the particle size. For this reason, a W / O dispersion liquid having a small particle diameter is prepared using the sheet 2 having a high rigidity and a lipophilic surface of the sheet portion 32 of the slit element 3. When the sheet 2 having a small rigidity and a hydrophilic surface is used for the sheet portion 32 of the slit element 3 so that the particle size of the water that forms a continuous phase with the W / O dispersion is increased, W / An O / W dispersion can be produced under less restrictions.

  Further, in the O / W / O dispersion form in which the O / W dispersion liquid is redispersed in the oil phase, the O / W dispersion liquid is prepared by using the sheet 2 having a large rigidity of the sheet portion 32 and a hydrophilic surface. The O / W dispersion liquid and the oil are passed through the slit element 3 having the sheet portion 32 with low rigidity formed on the lipophilic sheet 2 on the surface, so that the O / W / O dispersion can be performed under less restrictions. A liquid can be produced.

  The present invention can be applied to the case of producing a dispersion of a synthetic resin having a constant particle size distribution. Polymerizability having a certain particle size distribution by passing a polymerizable monomer mixture comprising a monomer, a polymerization initiator, a surfactant and the like before polymerization reaction through a slit element 3 provided on the sheet 2 of the present invention After the monomer dispersion is produced in advance, the polymerizable monomer dispersion is polymerized to obtain a synthetic resin dispersion having a certain particle size distribution. Furthermore, if the synthetic resin is separated from the dispersion, a synthetic resin powder having a particle size in a certain particle size range can be obtained.

  In the above method, two or more kinds of slit elements 3 having different rigidity are prepared, and a polymerizable monomer mixture is passed through each of the slit elements 3 so that two or more kinds of polymerizability having different dispersed phase particle size distributions are obtained. Create a monomer dispersion. Then, by mixing these polymerizable monomer dispersions at a desired ratio, a polymerizable monomer dispersion having two or more kinds of particle size distributions in the dispersed phase can be obtained. By polymerizing this, a synthetic resin dispersion in which the dispersed phase has two or more kinds of particle size distributions can be obtained.

  In the above method, the polymerization was carried out in a state where two or more kinds of polymerizable monomer dispersions were mixed. However, each polymerization monomer dispersion was polymerized without mixing before polymerization, and the particle size distribution was reduced. A plurality of different synthetic resin dispersions may be manufactured, and then these synthetic resin dispersions may be mixed at a desired ratio to obtain a synthetic resin dispersion in which the dispersed phase has two or more particle size distributions.

  The present invention can be applied to the production of a resin dispersion in which one monomer constituting the copolymer is a gas, such as an ethylene-vinyl acetate copolymer. When the composition of the dispersed phase is a copolymer such as an ethylene-vinyl acetate copolymer, for example, a monomer that is one gas constituting the copolymer and the other monomer that undergoes a copolymerization reaction, A polymerizable monomer mixture composed of a polymerization initiator, a surfactant and the like is passed through the slit element 3 provided on the sheet 2 of the present invention to absorb the monomer as one gas in a suspended state. Both are polymerizable monomer dispersions having a certain particle size distribution capable of controlling the viscosity after polymerization. This polymerizable monomer dispersion is polymerized to obtain a synthetic resin dispersion having a certain particle size distribution. The other monomer that undergoes the copolymerization reaction, a polymerization initiator, a surfactant, and the like are passed through the slit element 3 of the present invention in advance to form a polymerizable monomer mixture (dispersion). The monomer that is a gas constituting the copolymer and the monomer mixture may be passed through the slit element 3 of the present invention to obtain a desired polymerizable monomer dispersion.

  If the particle size distribution of the polymerizable monomer dispersion is kept small, an increase in viscosity during the polymerization reaction can be suppressed and the heat balance can be maintained, so that economical production is possible.

  In order to increase the proportion of one component of the copolymer, when the monomer that is one gas is absorbed into the other polymerizable monomer dispersion, the monomer that is one gas is It is preferable that the polymerizable monomer dispersion is at least in a saturated dissolved state, and particularly preferably maintained in a supersaturated dissolved state.

A slit element having a sheet of Teflon (registered trademark) and a thickness of 0.5 mm and having the shape shown in FIG. 3 (b), each slit having a side length of 2.5 mm and each side having an angle of 120 degrees. One was provided. One sheet was disposed so as to partition the passage. Then, 80 parts of water, 20 parts of soybean oil, and 0.8 parts of a surfactant (sodium dodecyl sulfate) were stirred with a stirrer at 1000 rpm for 1 minute, and a premixed solution was obtained in the passage at 8 cm ³ / min. And passed through the slit element of the sheet. The differential pressure at this time was 2 kgf / cm ² (about 0.2 MPa). The results of measuring the particle size distribution before and after passage were as follows. It was found that the particle size distribution was 1 μm or less.

Average particle size (μm) Before standard deviation (preliminary mixture) 23.106 0.238
After passing 0.804 0.212

One slit element having the same shape as in Example 1 was formed on a sheet made of Teflon (registered trademark) and having a thickness of 0.9 mm, and this sheet was disposed in the same manner as in Example 1. Then, the same premixed solution as in Example 1 was passed through the slit element at 8 cm ³ / min. The differential pressure at this time was 2.2 kgf / cm ² . The results of measuring the particle size distribution before and after passage were as follows. As compared with Example 1, it was found that when the thickness of the sheet was increased and the rigidity of the slit element was increased, a fine particle size distribution was obtained.

Average particle size (μm) Before standard deviation (preliminary mixture) 23.106 0.238
After passing 0.636 0.194
Example 1 0.804 0.212

A slit having the same shape as that of Example 1 was formed in a sheet made of Teflon (registered trademark) having a thickness of 0.9 mm, and one sheet of the sheet was disposed in the passage in the same manner as in Example 1. Then, the same premixed solution as in Example 1 was passed through the slit element at 48 cm ³ / min. The differential pressure at this time was 6 kgf / cm ² . The results of measuring the particle size distribution before and after passage were as follows.

Average particle size (μm) Before standard deviation (preliminary mixture) 23.106 0.238
After passing 0.820 0.217
Example 2 0.636 0.194
Although the flow rate of Example 3 is 6 times that of Example 2, the particle size distribution tends to increase slightly even when the flow rate is 6 times, but hardly changes. For this reason, it has been found that the slit element of the present invention has a structure capable of following a change in flow rate.

Further, even when the flow rate was increased 6 times, the differential pressure increased only 2.7 times. This is compared to the pressure difference of 79 kgf / cm ² expected in the case of the conventional fixed slit (assuming that the pressure difference is proportional to the square of the flow velocity as in a normal orifice, 2.2 × 6 ² = 79). About 8%. It could be judged that the slit element of the present invention can be handled by a pump having a low head and a small capacity.

One slit element having the same shape as in Example 1 was formed on a sheet made of Teflon (registered trademark) and having a thickness of 0.9 mm. Three such sheets were arranged at intervals such that each sheet was partitioned into passages. The same premixed solution as in Example 1 was passed through slit elements provided on each sheet under the same conditions as in Example 2. The results were as follows. The differential pressure at this time was 6.5 kgf / cm ² .

  When Example 4 was compared with Example 2, the particle size distribution was slightly increased. This may be because the particles re-collised due to re-collision.

Average particle size (μm) Before standard deviation (preliminary mixture) 23.106 0.238
After passing 0.857 0.208
Example 2 0.636 0.194

One slit element having the same shape as in Example 1 was formed on a sheet made of Teflon (registered trademark) and having a thickness of 0.9 mm. One sheet was disposed so as to partition the passage. And the differential pressure | voltage becomes ² kg / cm <2> with the preliminary | backup liquid mixture obtained by stirring 20 parts of water, 80 parts of light oil, and 3 parts of surfactant [sorbitan monooleate (span80)] with a stirrer at 500 rpm for 1 minute. The sheet was passed through the passage as such a flow rate and passed through the slit element of the sheet. The results of measuring the particle size distribution before and after passage were as follows.

Average particle size (μm) Before standard deviation (preliminary mixture) 11.503 0.307
After passing 0.793 0.224
From this result, it was found that a fuel oil dispersion having a dispersed phase of water and a fuel oil dispersion having a water particle size of 1 μm or less can be easily produced.

One slit element having the same shape as in Example 1 was formed on a sheet made of Teflon (registered trademark) and having a thickness of 0.9 mm. One sheet was disposed so as to partition the passage. Then, a premixed solution obtained by stirring 20 parts of water and 80 parts of light oil with a stirrer at 500 rpm for 1 minute is passed through the passage as a flow rate such that the differential pressure becomes 2 kg / cm ² and passes through the slit element of the sheet. To give a dispersion. Since the surfactant is not used and the particle size is unstable, the measurement result is unreliable, so when photographed and observed without measuring the particle size distribution, immediately after emulsification (immediately after making the dispersion) Swimming of water particles in the vicinity of 1 μm was observed. Then, after standing still and observing again after 2 hours, the suspended state was maintained on the external appearance, and the clarified layer of light oil and water could not be observed at all. From this, it is considered that the stability can be maintained for a considerable time in a dispersion in which water particles of about 1 μm are dispersed in light oil without using a surfactant.

FIG. 10 is a system diagram for removing dissolved oxygen from milk. In the system diagram shown in FIG. 10, M <b> 1 and M <b> 2 are sheets (module M) having the same slit elements as in the third embodiment. Milk (raw milk) containing 8.6 mg / L of dissolved oxygen is controlled to 50 cm ³ / min by the flow meter F 1 and nitrogen gas is controlled to 3.5 cm ³ / min by the flow meter F 2 and sent to the module M 1. . Milk containing fine bubbles that has passed through the module M1 is separated from nitrogen gas by the gas-liquid separator V1. The milk after separation passes through the check valve C1 and then passes through the module M2 together with nitrogen gas controlled to 3.0 cm ³ / min by the flow meter F3, and the milk containing fine bubbles that has passed through the module M2 is gas-liquid separated. Nitrogen gas is separated by the vessel V2 and stored in the container V3.

  The ratio of bubbles in the gas-liquid separators V1 and V2 was about 5 to 6%, and gas-liquid separation was easy. The dissolved oxygen at the outlet of the gas-liquid separator V1 was 2.5 mg / L. The dissolved oxygen in the milk stored in the container V3 was 0.8 mg / L. Regarding the nitrogen gas used, the volume ratio (nitrogen gas / milk) was 0.13.

  With the slit element of the present invention, milk can be deoxygenated economically with less nitrogen gas, and the foaming rate is greatly reduced as compared with existing deoxygenation methods. For this reason, it is considered that the apparatus is small and can be practically used economically.

  FIG. 11 is a system diagram for dissolving a gas in a liquid. In the system diagram shown in FIG. 11, reference numerals F1 and F2 denote water and oxygen flow meters, respectively, and P denotes a liquid feed pump. M1 is a module according to the present invention, and a sheet made of Teflon (registered trademark) and having a thickness of 0.9 mm is rolled into a cylindrical body having an outer diameter of 35 mm and a length of 250 mm. On the circumferential surface of this cylindrical body, 420 slit elements having 14 rows in the length direction and 30 rows each and having the shape shown in FIG. 3B were provided. M2 is a module similar to M1 made of a Teflon (registered trademark) sheet, and is a cylindrical body having an outer diameter of 25 mm and a length of 250 mm. On the circumferential surface of the cylindrical body, 300 slit elements each having 10 rows in the length direction and 30 rows each having the shape shown in FIG. 3B were provided.

  Distilled water with a dissolved oxygen amount of 17.8 mg / L is 4000 cc / min, oxygen gas is 100 cc / min, controlled by the flow meters F1 and F2, respectively, and sucked into the feed pump P, and discharged from the pump P. When the module M1 and the module M2 provided in series on the side were passed, the dissolved oxygen at the outlet of the module M2 was 53 mg / L and flowed out in a stable state.

  From the viewpoint of the dissolved oxygen amount, the mixed oxygen is absorbed in approximately 100% water. Since the amount of saturated dissolved oxygen at a water temperature of 11 ° C. during mixing was about 10 mg / L, supersaturated dissolved oxygen water could be produced easily and easily.

  From this, it is considered that the gas can be dissolved in the liquid in a supersaturated state easily with a simple facility such as this apparatus.

From 450 parts of distilled water (parts by weight, the same shall apply hereinafter), polyoxyethylene alkylaryl sulfate ester <Lebenol WZ: Kao Corporation product> 8 parts, 100 parts of methyl methacrylate, 0.5 parts of lauroyl peroxide, 3 parts of lauryl alcohol The preliminarily mixed liquid obtained by stirring the polymerizable monomer composition consisting of 1 minute at 1000 rpm with a stirrer was passed through the same slit element of the present invention as in Example 1 with a differential pressure of 1.5 kg / cm ^2. I let you. As a result, a polymerizable monomer dispersion having an average particle size of 0.718 μm and a standard deviation of 0.210 μm was obtained.

  Into a reactor equipped with a stirrer, a reflux condenser, a thermometer, and a dropping funnel, 560 parts of the polymerizable monomer dispersion is put, and the temperature in the vessel is kept at 70 ± 2 ° C. while blowing nitrogen gas, over 8 hours. A polymerization reaction was performed to obtain a synthetic resin dispersion. The synthetic resin particle size of the obtained synthetic resin dispersion was 0.872 μm in average particle size and 0.217 μm in standard deviation.

It was found that a synthetic resin dispersion having a small particle size variation (that is, a small particle size distribution width) can be obtained by the slit element of the present invention.
[Comparative Example 1]
The polymerizable monomer composition prepared by the same method as in Example 9 was stirred with a homogenizer at 5000 rpm for 10 minutes to obtain a polymerizable monomer dispersion. This polymerizable monomer dispersion was subjected to a polymerization reaction under the same conditions in the same apparatus as in Example 9 to obtain a synthetic resin suspension. The synthetic resin particle size of the resulting synthetic resin dispersion was 7.2 μm in average particle size and 14.21 μm in standard deviation.

  From this, it is considered that a synthetic resin dispersion having a small particle size distribution cannot be obtained with a normal homogenizer.

In a dissolution tank equipped with a 60 L internal volume stirrer, 7361 g of water, 28 g of 50% acetic acid, 54 g of partially saponified polyvinyl alcohol (polymerization degree 1750, saponification degree 88 mol%), partially saponified polyvinyl alcohol (polymerization degree 350, saponification degree) 88 mol%) 214 g and polyoxyethylene nonylphenyl ether (HLB16.2) 321 g were charged and stirred at 30 ° C. to obtain a uniform solution. To this aqueous solution, 0.300 g of ferrous sulfate, 140 g of a 14% by weight sodium formaldehyde sulfoxylate aqueous solution, and 7981 g of vinyl acetate were added and stirred. The mixture was passed at a pressure of 2 kg / cm ² to obtain a monomer mixed dispersion. This dispersion had an average particle size of 0.645 μm and a standard deviation of 0.196 μm.

The monomer mixture dispersion is put into a 300 L autoclave equipped with an irrigation type stirrer, and after nitrogen substitution and ethylene substitution, the monomer mixture dispersion is heated to 60 ° C. and the ethylene pressure is 45 kg / cm ^2. While maintaining the above, 1040 g of 0.5 wt% aqueous hydrogen peroxide was uniformly added over 6 hours. Subsequently, 494 g of a 3.2% by weight aqueous hydrogen peroxide solution was uniformly added over 2 hours, and a 7% by weight aqueous sodium formaldehydesulfoxylate solution was uniformly added over 7 hours. During this time, while vinyl acetate was passed through the same slit element as in Example 2 with ethylene gas at a slit differential pressure of 2 kg / cm ² , 7891 g of vinyl acetate was uniformly fed over 6 hours to polymerize the ethylene vinyl acetate. A dispersion in polymer was obtained. As a result, ethylene weight% in the obtained ethylene vinyl acetate copolymer was 21%, and the viscosity of the dispersion in the ethylene vinyl acetate copolymer was 1430 CPS.

Thus, according to the present invention, a dispersion in an ethylene vinyl acetate copolymer having a low viscosity and a high ethylene ratio was obtained.
[Comparative Example 2]
The monomer mixture having the same composition as in Example 10 was further stirred to obtain a monomer mixture dispersion. This mixture had an average particle size of 2.63 μm and a standard deviation of 0.283 μm.

The monomer mixture dispersion is put into a 300 L autoclave equipped with an irrigation type stirrer, and after nitrogen substitution and ethylene substitution, the monomer mixture dispersion is heated to 60 ° C. and the ethylene pressure is 45 kg / cm ^2. While maintaining the above, 1040 g of 0.5 wt% aqueous hydrogen peroxide was uniformly added over 6 hours. Subsequently, 494 g of a 3.2% by weight aqueous hydrogen peroxide solution was uniformly added over 2 hours, and a 7% by weight aqueous sodium formaldehydesulfoxylate solution was uniformly added over 7 hours. During this time, 7891 g of vinyl acetate was uniformly fed over 6 hours to polymerize to obtain a dispersion in ethylene vinyl acetate copolymer. As a result, ethylene weight% in the obtained ethylene vinyl acetate copolymer was 14.3%, and the viscosity of the dispersion in the ethylene vinyl acetate copolymer was 10,000 CPS or more.

  Therefore, it was considered that the copolymerization ratio of ethylene was low and the viscosity was high, so that it was not suitable for industrial production.

It is sectional drawing along the flow direction which shows the channel | path of the fluid which provided one Example of the module for dispersion liquid manufacture of this invention. It is sectional drawing along II-II of FIG. It is a front view which shows the various Example of the slit formed in a sheet | seat. It is a front view which shows another Example of a sheet | seat. It is a flow direction sectional view showing another example of module M of the present invention. (A) is sectional drawing of the flow direction which shows another Example of the module M of this invention, (b) is a perspective view of the module M shown to (a). It is sectional drawing of the flow direction which shows another Example of the module M of this invention. It is a perspective view of another Example of the module M of this invention. It is a front view of another Example of the module M of this invention. It is a systematic diagram for removing dissolved oxygen from milk. It is a systematic diagram for dissolving gas in a liquid.

Explanation of symbols

1 Pipe 2 Sheet 3 Slit Element 31 Slit 32 Sheet Part 10 Passage A Flow Direction M Module

Claims (17)

The fluid passage is divided into an upstream side and a downstream side by one or a plurality of sheets, and one or more slit elements are formed in the partition sheet, and the slit elements include the slits and the surrounding sheets. The surrounding sheet portion is movable by the fluid passing therethrough, and two or more substances constituting the dispersion are caused to flow through the passage, and the two or more substances are passed through the slit element together. A method for producing a dispersion, wherein the dispersion is made into a dispersion. The method for producing a dispersion according to claim 1, wherein the pressure difference between the upstream side and the downstream side of the partition sheet is 3 MPa or less. The method for producing a dispersion according to claim 1, wherein two or more kinds of substances constituting the dispersion are mixed and then passed through the slit element. The dispersion liquid according to any one of claims 1 to 3, wherein the two or more substances constituting the dispersion liquid are a liquid and a gas, the liquid is a dispersion medium, and the gas is a dispersion phase. Manufacturing method. The liquid as the dispersion medium is a liquid in which one or more kinds of gas is dissolved, and the gas as the dispersion phase is a gas inert to at least one kind of gas dissolved in the liquid. The method for producing a dispersion according to claim 4. The two or more kinds of substances constituting the dispersion are characterized in that the main substance is dairy product or soy milk, and the other substances are one or more kinds of substances having different components from the main substance. The method for producing a dispersion according to any one of claims 1 to 3. The substance constituting the dispersion is a substance that becomes a dispersion medium and a dispersion phase, the dispersion medium is fuel oil, and the main component of the dispersion phase is water. 4. The method for producing a dispersion according to any one of 3 above. The substance constituting the dispersion is at least water and a polymerizable monomer, and the substance is passed through the slit element to form a dispersion, and the polymerizable monomer is polymerized in the dispersion and synthesized. Resin is used as a dispersed phase, The manufacturing method of the dispersion liquid in any one of Claims 1-3 characterized by the above-mentioned. The substance constituting the dispersion is a gas mixture of a polymerizable monomer-containing liquid and a polymerizable monomer, and the both substances are passed through the slit element to form a dispersion, and the polymerizable in the dispersion The method for producing a dispersion according to any one of claims 1 to 4, wherein a monomer and the polymerizable gas mixture are polymerized and the polymerized synthetic resin is used as a dispersed phase. The method for producing a dispersion according to claim 9, wherein the monomer as the gas mixture is a mixture containing ethylene, and the monomer as the liquid is a mixture containing vinyl acetate. A module that is arranged in a passage through which two or more substances constituting the dispersion flow together and divides the passage into an upstream side and a downstream side, and the module includes a sheet on which one or more slit elements are formed. Each of the slit elements comprises a slit and a sheet portion around the slit, and the surrounding sheet portion is movable by the fluid passing therethrough. 12. The dispersion manufacturing module according to claim 11, wherein the slit of the slit element extends in a plurality of directions from the center. The module for manufacturing a dispersion according to claim 11 or 12, wherein a plurality of slit elements are formed on one sheet. 11. A sheet having a slit element is cylindrical or conical, and is configured to allow fluid to flow between the inside and the outside of the cylindrical or conical shape. The module for manufacturing a dispersion according to claim 13. The module for manufacturing a dispersion liquid according to any one of claims 11 to 14, wherein a plurality of sheets having slit elements are arranged at intervals. 14. The dispersion according to claim 11, wherein one sheet having slit elements is spirally wound, and a space is formed between the layers of the spiral. Manufacturing module. The module for manufacturing a dispersion according to any one of claims 11 to 13, wherein the sheet having the slit elements is made of metal, plastic, or rubber.

Images