JP4389559B2 - Microchannel structure - Google Patents

Description

  INDUSTRIAL APPLICABILITY The present invention is suitable for performing mixing, solvent extraction, chemical reaction, separation, and the like of fluid introduced into a microchannel in a microchannel structure having a microchannel that performs chemical reaction, droplet generation, analysis, and the like. The present invention relates to a microchannel structure.

  Usually, a reaction using a phase transfer catalyst is performed by dissolving a substrate and a phase transfer catalyst in an organic phase, dissolving an alkali such as potassium hydroxide or sodium hydroxide in a water phase as a reaction initiator, and mixing the organic phase and the water phase. The two-phase system is stirred and suspended to allow the reaction to proceed. In the case of this reaction system, the reaction that the reaction initiator alkali reacts with the product and decomposes to the original substrate also proceeds at the same time, so the reaction usually stops in an equilibrium state. was there.

  As a solution to the above problem, in recent years, only the phase transfer catalyst is dissolved in a solvent that is immiscible with neither the organic phase nor the aqueous phase, and is disposed between the aqueous phase and the organic phase to be present as the third liquid phase. A reaction process has been attempted. In the above example, as shown in FIG. 15, the catalyst phase (28) in which the phase transfer catalyst is dissolved is used as the third phase so that the organic phase (2) and the aqueous phase (1) are not in direct contact with each other. carry out. For the stirring, a Lamond stirrer (29) which is a stirrer having a special structure is used so that the three phases are not completely suspended. By doing so, it becomes possible to react the reactants dissolved in both phases while separating the organic phase and the aqueous phase, so that the product does not come into direct contact with the alkali as a reaction initiator. Periodic operation in which the reverse reaction is suppressed, the reaction yield and selectivity are increased, the reaction rate is increased, the organic phase containing the reaction product is extracted, the organic phase containing the reaction product is newly added, and the reaction is performed again. It has been reported that can be done. (For example, refer nonpatent literature 1).

  However, in general, in a reaction vessel such as a test tube, a beaker, or a reaction kettle, the arrangement of each phase is determined by the specific gravity of each phase, or it is freely mixed with other phases due to the philicity. It is extremely difficult to locate between the organic and aqueous phases. In addition, it is very practical to use by scaling up, such as designing a special stirrer to stir so that each phase does not mix, or stirring so as not to break the interface of each phase due to vibration. There was a problem that it was difficult.

  Recently, a microchannel structure having a microchannel having a length of about several centimeters on a glass substrate of several cm square and a width and depth of sub-μm to several hundreds of μm is used to introduce the fluid into the microchannel. Research that conducts chemical reactions is attracting attention. In such a microchannel, the rapid diffusion of molecules due to the effect of a short intermolecular distance and a large specific interfacial area in a microspace enables efficient chemical reaction without special stirring operation. It has been suggested that the side reaction that occurs subsequently is suppressed by rapidly extracting and separating the target compound produced by the reaction from the reaction phase to the extraction phase (see, for example, Non-Patent Document 2). The microchannel generally means a channel having a channel width of 50 to 300 μm or less and a channel depth of 10 to 100 μm or less. In general, most Reynolds numbers are smaller than 1 in the microscale flow path, and unless the flow velocity is increased, the laminar flow state shown in FIG. 1 is obtained, and the fluid boundary (3) is formed. The For example, in the case of using a micro flow path (12) in which the fluid introduction port (9) as shown in FIG. 1 used in the present invention has a ψ-shape, the arrangement of each phase from the three-phase junction (4). Can easily form a three-phase laminar flow without depending on the specific gravity of each phase and form a stable fluid boundary (3). This is because, in general, the influence of surface tension is far greater than the influence of gravity in a microscale flow path, so the Reynolds number in the fluid flowing in the flow path is less than 10 or less than 1, and the flow velocity is much higher. This is because a laminar flow state is maintained unless the value is increased (see, for example, Non-Patent Document 3). This phenomenon is not limited to organic phases such as toluene and cyclohexane, which are generally difficult to mix, and aqueous phases. In a test tube, organic phases such as methanol and ethanol that are mixed instantaneously by free mixing and aqueous phases. In the case of the above, when the organic phase of toluene or cyclohexane and the organic phase of methanol or ethanol described above are fed at a flow rate of several centimeters / minute to several tens of liters / minute, Is formed. Here, the fluid boundary may be referred to as a laminar flow interface.

  In general, since the diffusion time is proportional to the square of the width (8) of the microchannel shown in FIG. 1, the smaller the microchannel width is, the smaller the microfluidic width, the more the molecular diffusion is achieved without active mixing of the reaction solution. Mixing progresses and reaction and extraction become easy to occur. That is, when such a micro flow path is used, the progress of solvent extraction and chemical reaction proceeds mainly by diffusion resulting from the concentration difference of substances contained between adjacent fluids at the fluid boundary (3), In general, solvent extraction and chemical reaction progress more as the flow rate of fluid supply (hereinafter referred to as the liquid feeding speed) is slower or the flow path length is longer. That is, it is said that the longer the contact time between adjacent fluids, the more the solvent extraction and chemical reaction proceed (for example, see Non-Patent Document 3).

  Furthermore, as shown in FIG. 2, it is generally said that each phase can be separated by keeping the fluid outlet (10) of the microchannel (12) in a Ψ shape. . In this way, completely separating and discharging the fluid introduced at the fluid discharge port means that the solvent extraction and chemical reaction caused by the contact of the fluid in the microchannel are completely performed at the branch portion (5) of the microchannel. This is a very important function even when the fluid is stopped or reused once the fluid is introduced into the microchannel.

  However, in actuality, the position of the fluid boundary (3) fluctuates in an unstable manner due to fluctuations in the liquid feeding pressure of the liquid feeding pump and the difference in affinity between the fluid and the inner wall of the micro flow path. It is very difficult to stably form a fluid boundary (3) as shown in FIG. 2 and discharge each fluid without substantially mixing with other fluids. In particular, as shown in FIG. 2, when two or more fluid boundaries exist in the microchannel, the fluid boundary is not more stable than in the case of the two-phase laminar flow, Fluid mixing has not been substantially prevented. Here, “substantially not mixed” or “substantially not mixed” is defined as that the mixing ratio of each fluid is less than 10% in the channel length of the microchannel.

"Development of next-generation chemical reaction process technology Development of multi-phase catalytic reaction process technology 2001 technical report", Chemical Technology Strategy Organization, May 2001, pages 13-43

H. Hisamoto et. al. (H. Hisamoto et al.) “Fast and high conversion phase-transfer synthesis exploitation the liquid-liquid interface formed in a microchannel chip”, Chem. Commun. , 2001, 2662-2663. Fujii, “Integrated Microreactor Chip”, Nagare 20 Volume, 2001, pp. 99-105

  The object of the present invention has been proposed in view of such a conventional situation. Two or more kinds of fluids are introduced into a microchannel and two adjacent kinds of fluids are maintained while maintaining a multiphase laminar flow state. It is an object of the present invention to provide a microchannel structure that allows solvent extraction and chemical reaction between them to proceed, and that each fluid can be separately discharged from a predetermined outlet without substantially mixing with other fluids.

  In order to solve the above-described problems, the present invention provides three or more inlets for introducing a fluid, an introduction channel communicating with the inlet, and a fluid introduced and communicated with a junction where the introduction channel merges. A microchannel structure having a microchannel for flowing, a discharge channel communicating with the microchannel and discharging a predetermined fluid, and a discharge port communicating with them, A plurality of discontinuous partition walls are formed in the fluid traveling direction along the vicinity of the boundary formed by the fluid, and the partition walls perpendicular to the fluid traveling direction of the discontinuous partition walls along the boundary are adjacent to each other. By using the microchannel structure that is substantially deviated from the position of the fluid in the fluid traveling direction, the above-mentioned problems with the prior art can be solved, and the present invention has finally been completed.

  In the present invention, the expression “boundary formed by two or more kinds of fluids” is used synonymously with the expression “laminar flow interface” or “fluid boundary”.

  Hereinafter, the present invention will be described in more detail.

  In the present invention, usually two or more kinds of fluids in which a target reactant or a substance to be extracted is dissolved in a medium such as water or an organic solvent are introduced into a microchannel formed in a microchannel structure. In addition, the microfluidic structure is capable of feeding the introduced fluid while maintaining a multiphase laminar flow in the microfluidic space.

For this reason, the microchannel structure used in the present invention communicates with and introduces three or more inlets for introducing a fluid, an introduction channel communicating therewith, and a junction where the introduction channel merges. A micro-channel structure having a micro-channel for causing the fluid to flow, a discharge channel communicating with the micro-channel and discharging a predetermined fluid, and a discharge port communicating with them, A plurality of discontinuous partition walls are formed in the fluid traveling direction along the vicinity of the fluid boundary formed by two or more kinds of fluids, and are perpendicular to the fluid traveling direction of the discontinuous partition walls along the vicinity of each fluid boundary. There is a need for a microchannel structure in which the position is substantially deviated from the position of adjacent partition walls in the fluid traveling direction. Here, “substantially deviated” means that the deviation of the position of at least one of the ends of the partition wall in the fluid traveling direction is a difference within the range of machining accuracy, and more specifically, This means a displacement of ± 2.5 μm or more. Conversely, “substantially matching” the position of the partition wall means that the deviation of the position of at least one end of the partition wall in the fluid traveling direction is a difference that is less than the processing accuracy range. Specifically, this means a positional deviation of less than ± 2.5 μm. The above-mentioned micro flow channel is not limited in particular in the width of the flow channel and the depth of the flow channel as long as the feature of the micro space appears. In the present invention, a channel having a width of 500 μm or less and a depth of 300 μm or less, preferably a channel having a channel width of 50 to 300 μm and a channel depth of 10 to 100 μm. To do. The width and depth of the introduction channel and the discharge channel are not particularly limited, but may be the same width and depth as the microchannel. The sizes of the inlet and the outlet are not particularly limited, but may generally be about 0.1 mm to several mm in diameter.

  As described above, by providing the partition wall in the micro flow path, a stable multiphase laminar flow is maintained without the adjacent fluids being substantially mixed in each of the two or more introduced fluids. It flows as it is. Furthermore, each fluid can be discharged into a predetermined discharge flow path without substantially mixing with fluids adjacent to each other.

  If the height of the partition wall is too low with respect to the depth of the flow path, the effect of the present invention cannot be obtained. Further, the height of the partition wall is preferably 20% or more with respect to the depth of the flow path, and in order to prevent adjacent fluids from substantially mixing with each other in the micro flow path. Is preferably such that the height of the partition wall is such that the fluid cannot move beyond the partition wall to the adjacent fluid phase and is substantially equal to the microchannel depth. preferable.

  Hereinafter, the fine channel structure of the present invention will be described in more detail with reference to the drawings.

  As shown in the present invention, a plurality of partition walls that are discontinuous in the direction of fluid flow are formed in the microchannel along the vicinity of a plurality of fluid boundaries, and the fluid flow of the discontinuous partition walls along the vicinity of each boundary is formed. By shifting the position perpendicular to the direction to the position of the adjacent partition wall and the fluid traveling direction, when the introduced fluid is fed while maintaining a multiphase laminar flow in the microchannel space, the partition wall is shifted. Compared with a micro flow channel having no structure, the mixing of fluids can be greatly reduced. The principle will be described below with reference to FIG.

  3 and 4 are views showing a state in which two fluids form a three-phase laminar flow. FIG. 3 shows a case where the partition wall (13) is not displaced, and FIG. 4 shows a case where the partition wall (13) is displaced.

  As shown in FIG. 3, when the partition wall is not displaced, if the position of the fluid interface 1 (6) fluctuates mainly due to the fluid pressure fluctuation caused by the liquid feed pump, the adjacent fluid interface 2 (7) is also affected and fluctuates.

  On the other hand, as shown in FIG. 4, when the partition wall is displaced, the position of the fluid interface 2 (7) is stably maintained by the partition wall even if the position of the fluid interface 1 (6) fluctuates. As a result, fluctuations are suppressed, and as a result, while maintaining a stable multi-phase laminar flow, each fluid is discharged into a predetermined discharge channel without substantially mixing with adjacent fluids. Is possible.

  Some aspects of the microchannel in the present invention are shown in FIGS. It is needless to say that the present invention is not limited to these embodiments and can be arbitrarily changed without departing from the gist of the invention. As shown in FIG. 5, the position of the partition wall perpendicular to the fluid traveling direction is shifted from the position of the adjacent partition wall in the fluid traveling direction, and the positions perpendicular to the fluid traveling direction at both ends of the partition wall are substantially And the length of all the partition walls in the fluid traveling direction is substantially equal to the distance between the partition walls in the fluid traveling direction. However, as shown in FIG. The length in the fluid traveling direction and the interval between the partition walls in the fluid traveling direction may be different between discontinuous partition walls along the vicinity of adjacent boundaries. By doing in this way, it becomes possible to adjust the contact time and specific interface area of the adjacent fluid, and the extraction effect and reaction efficiency can be adjusted.

  Here, the position of the partition wall with respect to the width direction of the microchannel is not particularly limited, and can be changed according to the properties of the solution such as the flow rate, the flow rate, and the viscosity. Naturally, even if the viscosity of the adjacent fluid changes due to chemical reaction or solvent extraction and the position of the fluid boundary gradually changes according to the fluid traveling direction, if the change in viscosity is calculated and predicted in advance by simulation, etc. A partition wall may be provided along the vicinity of the fluid boundary. Conversely, if fluids with different viscosities flow through a microchannel formed near the center of the partition wall in the width direction of the channel, if the fluid is fed at a liquid feeding speed that is inversely proportional to the viscosity of the fluid A fluid boundary can be formed near the partition wall. Moreover, as shown in FIG. 7, the thickness (14) of the partition wall is not particularly limited, but is preferably about 3 to 10% of the flow path width so as not to disturb the liquid feeding itself. Further, the minimum value of the shortest interval (25) between the partition walls in the fluid traveling direction formed along the vicinity of the fluid boundary is not particularly limited as long as the partition wall (13) is discontinuous, About 1 / (number of fluids separated by partition walls) is preferable, for example, in the case of a three-phase laminar flow, the number of fluids partitioned by partition walls is 3, so that the flow width is as small as 150 μm. In the case of a flow path, the shortest distance between the partition wall and the partition wall is preferably about 50 [μm].

  The microchannel substrate having the microchannels constituting the microchannel structure as described above is made of, for example, a substrate material such as glass, quartz, ceramic, silicon, metal, resin, machining, laser processing, It can be manufactured by direct processing by etching or the like. Further, when the substrate material is ceramic or resin, it can also be manufactured by molding using a mold such as a metal having a channel shape. Generally, the microchannel substrate is laminated and integrated with a cover body having a small hole with a diameter of about several millimeters at a position corresponding to the fluid inlet, the fluid outlet, and the outlet of each microchannel. Used as a microchannel structure. As a method for joining the cover body and the micro-channel substrate, when the substrate material is ceramics or metal, soldering or adhesive is used, or when the substrate material is glass, quartz, or resin, it is a hundred to several hundreds of degrees A bonding method suitable for each substrate material is used, such as thermal bonding by applying a load at a high temperature, or when the substrate material is silicon, by activating the surface by washing and bonding at room temperature.

  According to the present invention, the following effects can be obtained.

  The microchannel structure according to the present invention has three or more inlets for introducing a fluid, an introduction channel communicating with the inlet, and a junction where the introduction channel merges and allows the introduced fluid to flow. A microchannel structure having a microchannel, a discharge channel that communicates with the microchannel and discharges a predetermined fluid, and a discharge port that communicates with the channel. A plurality of discontinuous partition walls are formed in the fluid traveling direction along the vicinity of the boundary formed by the step, and the positions of the discontinuous partition walls along the boundary near the fluid traveling direction are adjacent to each other. A microchannel structure that is substantially deviated in position and in the fluid traveling direction. By using such a microchannel structure, two or more kinds of fluids are introduced into the microchannel, and a multiphase layer is formed. While maintaining the flow state, solvent extraction and chemical reaction between two adjacent fluids Allowed to proceed, and can be separately discharged from a predetermined discharge port without each fluid is substantially uncontaminated by other fluids.

  Further, in the microchannel structure according to the present invention, the position perpendicular to the fluid traveling direction of at least one end of the partition wall may substantially coincide with the fluid traveling direction of both ends of the partition wall described above. The vertical direction of the partition wall may substantially coincide with each other, and the length and interval of the partition wall in the fluid traveling direction may be substantially equal. By doing in this way, it becomes possible to adjust the contact time and specific interface area of the adjacent fluid, and the extraction effect and reaction efficiency can be adjusted.

  Hereinafter, embodiments of the present invention will be described in detail. Needless to say, the present invention is not limited to these examples, and can be arbitrarily changed without departing from the scope of the invention.

  7 to 8 show conceptual diagrams of the microchannel structure used in the first embodiment. The shape of the microchannel (12) is such that the fluid inlet port side and the fluid outlet port side are branched into three microchannels in a ψ-shape, and the microchannel is located in the microchannel as shown in FIG. A discontinuous partition wall (13) along the fluid traveling direction having a height equal to the channel depth (11) of the microchannel was formed in approximately three equal parts with respect to the width direction. The positions of the discontinuous partition walls perpendicular to the fluid traveling direction are substantially displaced in the fluid traveling direction, and the positions perpendicular to the fluid traveling directions at both ends of the partition wall are substantially aligned. . The width (8) of the manufactured microchannel is 150 μm, and the channel depth (11) is 20 μm (recognized in FIG. 5 showing the AA ′ section in FIG. 7 and FIG. 10 showing the BB ′ section). The length is 30 mm. The shortest distance (16) between the partition wall and the partition wall with respect to the fluid traveling direction and the longest length (17) of the partition wall in the fluid traveling direction are 50 μm, and the thickness (14) of the partition wall in the channel width direction is about 5 μm. It is. The microchannel is formed on a Pyrex (registered trademark) substrate of 70 mm × 38 mm × 1 mm (thickness) by general photolithography and wet etching, and three fluid inlets A (19) and B (20 ), A small hole having a diameter of 1.0 mm is mechanically formed at a position corresponding to the inlet C (21) and the three fluid outlets D (22), E (23), and F (24). The micro flow path was sealed by joining the Pyrex (registered trademark) substrate of the same size provided by the processing means as a cover body by heat fusion.

  Water and cyclohexane were fed to the microchannel structure at an equal feeding rate between 1 μL / min and 50 μL / min, respectively. The viscosity of water at 20 ° C. is 1.002 [mPa · s], and the viscosity of cyclohexane is 0.979 [mPa · s], which are substantially equal. The amount of water discharged from the inlet D (22) when water was fed from the inlet A (19), cyclohexane from the inlet B (20), and water from the inlet C (21) was sent under the above conditions. The amount of mixed cyclohexane, the amount of cyclohexane discharged from the outlet E (23) and the amount of mixed water, the amount of water discharged from the outlet F (24) and the amount of mixed cyclohexane, respectively. The measurement was made by weighing with a graduated cylinder, and the results are shown in Table 1.

表１は、等速条件下で、各送液速度における混入率を、水相への有機相の混入率（％）、有機相への水相の混入率（％）として示したものであり、流速は３、５、８、１０、２０、５０μＬ／分である。

Table 1 shows the mixing rate at each feeding speed under constant speed conditions as the mixing rate (%) of the organic phase into the aqueous phase and the mixing rate (%) of the aqueous phase into the organic phase. The flow rate is 3, 5, 8, 10, 20, 50 μL / min.

  From this result, a mixing rate of less than 5% was realized when the liquid feeding speed was in the range of at least 8 to 50 μL / min.

  The cyclohexane structure used in Example 1 is fed at a liquid feed rate at which cyclohexane is fixed at 8 μL / min, and water is sent at a liquid feed rate of 3 μL / min to 20 μL / min. Liquid. That is, when the ratio of the feed rate of water to cyclohexane is 0.375 to 2.5, water is introduced from the inlet A (19), cyclohexane is introduced from the inlet B (20), and water is introduced from the inlet C (21). The amount of water discharged from the outlet D (22) and the amount of mixed cyclohexane, the amount of cyclohexane discharged from the outlet E (23) and the amount of mixed water, The amount of water discharged from the discharge port F (24) and the amount of mixed cyclohexane were measured by measuring with a graduated cylinder, and the results are shown in Table 2.

表２は、各送液速度比における混入率を、水相１への有機相の混入率（％）、有機相への水相１および水相２の混入率（％）、水相２への有機相の混入率（％）、として示したものであり送液速度比は０．３７５、０．６２５、１．０００、１．２５０、２．５００である。

Table 2 shows the mixing ratio at each liquid feeding speed ratio, the mixing ratio (%) of the organic phase to the aqueous phase 1, the mixing ratio (%) of the aqueous phase 1 and the aqueous phase 2 to the organic phase, and the aqueous phase 2. The mixing ratio (%) of the organic phase is 0.375, 0.625, 1.000, 1.250, 2.500.

  From this result, a mixing rate of less than 10% was realized when the range of the liquid feeding speed ratio was at least 0.625 to 1.25.

  The conceptual diagram of the microchannel structure used for the Example was shown in FIGS. The shape of the microchannel is such that the fluid introduction port side and the fluid discharge port side are branched into three microchannels in a ψ-shape, and within the microchannel, as shown in FIG. In contrast, a discontinuous partition wall (13) along the fluid traveling direction having a height equal to the flow path depth (11) of the micro flow path was formed in approximately three equal parts. The position of the discontinuous partition wall perpendicular to the fluid traveling direction is not substantially displaced in the fluid traveling direction, and the positions perpendicular to the fluid traveling direction at both ends of the partition wall are substantially aligned. . The width (8) of the manufactured microchannel is 150 μm, and the channel depth (11) is 20 μm (recognized in FIG. 13 showing a CC ′ section in FIG. 11 and FIG. 14 showing a DD ′ section). The length is 30 mm. The shortest distance (16) between the partition wall and the partition wall with respect to the fluid traveling direction and the longest length (17) of the partition wall in the fluid traveling direction are 50 μm, and the thickness (14) of the partition wall in the channel width direction is about 5 μm. It is. The microchannel is formed on a Pyrex (registered trademark) substrate of 70 mm × 38 mm × 1 mm (thickness) by general photolithography and wet etching, and three fluid inlets A (19) and B (20 ), A small hole having a diameter of 1.0 mm is mechanically formed at a position corresponding to the inlet C (21) and the three fluid outlets D (22), E (23), and F (24). The micro flow path was sealed by joining the Pyrex (registered trademark) substrate of the same size provided by the processing means as a cover body by heat fusion.

  In the same manner as in Example 1, water and cyclohexane were fed into the microchannel structure at a rate of 5 μL / min to 20 μL / min at the same rate. The amount of water discharged from the inlet D (22) when water was fed from the inlet A (19), cyclohexane from the inlet B (20), and water from the inlet C (21) was sent under the above conditions. The amount of mixed cyclohexane, the amount of cyclohexane discharged from the outlet E (23) and the amount of mixed water, the amount of water discharged from the outlet F (24) and the amount of mixed cyclohexane, respectively. The measurement was made by weighing with a graduated cylinder, and the results are shown in Table 1.

  As a result, the mixing ratio of cyclohexane into water, the mixing ratio of water into cyclohexane, and the mixing ratio of cyclohexane into water were 15% or more at any liquid feeding speed ratio, which was a very high mixing ratio.

  Further, in the same manner as in Example 2, the microchannel structure was fed at a liquid feed rate at which cyclohexane was fixed at 8 μL / min, and water was fed at a rate of 3 μL / min to 20 μL / min. The liquid was sent at a different liquid speed. That is, when the ratio of the feed rate of water to cyclohexane is 0.375 to 2.5, water is introduced from the inlet A (19), cyclohexane is introduced from the inlet B (20), and water is introduced from the inlet C (21). The amount of water discharged from the outlet D (22) and the amount of mixed cyclohexane, the amount of cyclohexane discharged from the outlet E (23) and the amount of mixed water, The amount of water discharged from the discharge port F (24) and the amount of mixed cyclohexane were measured by measuring with a graduated cylinder, and the results are shown in Table 2. As a result, the mixing rate of cyclohexane into water and the mixing rate of water into cyclohexane were 15% or more at any liquid feeding speed, which was a very high mixing rate.

It is a conceptual diagram which shows the three-phase laminar flow in the microchannel with which the fluid introduction port became ψ-shape. It is a conceptual diagram which shows the three-phase laminar flow in the microchannel in which the fluid inlet and the fluid outlet were ψ-shaped. It is the figure which showed a mode that 2 fluid formed the three-phase laminar flow, and shows the case where the partition wall has not shifted | deviated. It is the figure which showed a mode that 2 fluid formed the three-phase laminar flow, and the case where the partition wall has shifted | deviated is shown. FIG. 4 is a schematic plan view of one aspect of the microchannel according to the present invention, in which the position perpendicular to the fluid traveling direction of the partition wall is shifted from the position of the adjacent partition wall in the fluid traveling direction, and the fluid at both ends of the partition wall The position perpendicular to the traveling direction is substantially the same, and the lengths of all the partition walls in the fluid traveling direction and the intervals between the partition walls in the fluid traveling direction are substantially equal. FIG. 4 is a schematic plan view of one aspect of the microchannel according to the present invention, in which the position perpendicular to the fluid traveling direction of the partition wall is shifted from the position of the adjacent partition wall in the fluid traveling direction; The case where the length and the space | interval of the fluid advancing direction of partition walls differ in the discontinuous partition walls along the boundary vicinity which adjoins is shown. The structure of the microchannel structure used for the Example is shown. It is a conceptual diagram of the internal structure of the microchannel used for the Example. It is sectional drawing (enlarged) of AA 'in FIG. It is sectional drawing (enlarged) of BB 'in FIG. The structure of the microchannel structure used for the comparative example is shown. It is a conceptual diagram of the internal structure of the microchannel used for the comparative example. It is sectional drawing (enlarged) of CC 'in FIG. It is sectional drawing (enlarged) of DD 'in FIG. It is the figure which showed an example which implements reaction by making the catalyst phase which is a 3rd phase exist between an organic phase and an aqueous phase so that an organic phase and an aqueous phase may not be contacted directly.

Explanation of symbols

1: Water phase 2: Organic phase 3: Fluid boundary 4: Merge part 5: Branch part 6: Interface 1
7: Interface 2
8: Width of microchannel 9: Fluid inlet 10: Fluid outlet 11: Channel depth 12: Microchannel 13: Partition wall 14: Partition wall thickness 15: Partition wall height 16: Fluid progression 17: The longest length of the partition wall in the fluid traveling direction 18: The fluid traveling direction 19: Inlet A
20: Inlet B
21: Inlet C
22: Discharge port D
23: Discharge port E
24: Discharge port F
25: Substrate 26: Cover 27: Small hole 28: Catalyst phase 29: Lamond stirrer

Claims (4)

Three or more inlets for introducing a fluid, an introduction channel communicating therewith, a microchannel communicating with a merging portion where the introduction channel joins and flowing the introduced fluid, and the microflow A microchannel structure having a discharge channel that communicates with a channel and discharges a predetermined fluid and a discharge port that communicates with the channel, and is formed by a fluid of two or more types and a three-phase laminar flow or more A plurality of discontinuous partition walls are formed in the fluid traveling direction along the vicinity of the fluid boundary, and the positions perpendicular to the fluid traveling direction of the discontinuous partition walls along the vicinity of each fluid boundary are the positions of the adjacent partition walls. A microchannel structure characterized by being substantially displaced in a fluid traveling direction. 2. The microchannel structure according to claim 1, wherein a position perpendicular to the fluid traveling direction of at least one end of one side of the partition wall substantially coincides. 2. The microchannel structure according to claim 1, wherein positions perpendicular to the fluid traveling direction at both ends of the partition wall substantially coincide with each other. The microchannel structure according to any one of claims 1 to 3, wherein the partition walls have the same length in the fluid traveling direction, and an interval between the partition walls adjacent to each other in the fluid traveling direction is the partition wall. A microchannel structure characterized by being substantially equal to a length of a wall in a fluid direction .

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