JPWO2006030952A1 - Fluid mixer - Google Patents

Abstract

The present invention has a micro-channel composed of a mixing channel and a plurality of inflow channels connected to the mixing channel, and at least two kinds of fluids are introduced into the mixing channel from the plurality of inflow channels, respectively, and the fluid is mixed. A fluid mixer for causing a chemical reaction between reagents mixed in the mixing flow path, for example, a reaction between a reagent and a specimen for a synthetic reaction or a test for the purpose of producing a predetermined substance The present invention relates to a fluid mixer (hereinafter also referred to as a microreactor).

Description

  The present invention has a micro-channel composed of a mixing channel and a plurality of inflow channels connected to the mixing channel, and at least two kinds of fluids are introduced into the mixing channel from the plurality of inflow channels, respectively, and the fluid is mixed. A fluid mixer for causing a chemical reaction between reagents mixed in the mixing flow path, for example, a reaction between a reagent and a specimen for a synthetic reaction or a test for the purpose of producing a predetermined substance The present invention relates to a fluid mixer (hereinafter also referred to as a microreactor).

  The fluid here refers to a liquid or gas, or a mixture of liquid and gas, or a solid containing them. In the case of a liquid, it is also simply referred to as a reagent or a reagent solution.

  In addition, the micro flow path described above refers to a flow path having a cross-sectional dimension of 10 mm or less. The flow path preferably has a cross-sectional dimension of 500 μm to 100 nm under the conditions in light of the current processing technology. In the case where the processing cost is reduced and the processing accuracy is improved by the progress of the processing technology of the micro flow channel, a flow channel having a cross-sectional dimension of 1 μm to 100 nm is further desirable in order to control the reagent at the molecular level.

  2. Description of the Related Art In recent years, attention has been focused on microreactors that cause various microchemical reactions while circulating reagent solutions using channels (microchannels) having a minute channel cross-sectional area. In such a microreactor, for example, since the cross-sectional area of the flow path is very small, a small volume of the reagent solution and the sample is sufficient, and a specific surface area (surface area per unit volume) flowing through the flow path is sufficient. Therefore, the heat exchange efficiency is extremely high and the temperature control is easy to perform quickly, so that high selectivity is obtained for the stereochemistry, geometric isomerism, and positional isomerism of the reaction product, and the reaction can be performed. There is a merit that it can be performed efficiently.

  Here, in general chemical reactions, suitable temperature conditions exist for each reaction. This is because when the temperature is increased in the chemical reaction, the thermal kinetic energy of the particles in the solution increases. In order for a chemical reaction to occur, particles such as atoms, molecules, and ions must collide, and atomic recombination must occur between the particles. The atomic recombination that occurs between particles does not occur in all of the colliding particles. As shown in FIG. 1, an active complex in an unstable state with high energy is once created between particles having a certain energy or more called activation energy, and only particles that have formed an active complex It turns into a product. In addition, the vertical axis | shaft of FIG. 1 shows energy, and a horizontal axis shows the advancing direction of reaction. Here, the case where the energy of the product is lower than that of the reactant is an exothermic reaction, and the opposite case is the endothermic reaction, and FIG. 1 shows the case of the exothermic reaction. Therefore, in a chemical reaction, the reaction rate tends to increase with increasing temperature. This tendency is also clearly shown by the Arrhenius equation shown in Equation 1 below.

Where A is the frequency factor and E _a is the activation energy, which are constants specific to the reaction. R is a gas constant and T is an absolute temperature. Further, k is referred to as a rate constant, and the reaction rate increases as the value increases.

  However, an extremely high temperature reaction causes undesirable phenomena such as chemical decomposition of the reagent before the reaction. Therefore, suitable temperature conditions exist for each chemical reaction, and temperature control in the reaction region is very important. If the temperature control is insufficient, the chemical reaction is not performed as scheduled, and a system with poor productivity such as a decrease in the yield of the target main product is forced. However, in conventional chemical reactions using flasks, beakers, and large reaction tanks, it is very easy to adjust the temperature of the entire reaction area quickly and uniformly because chemical reactions are performed using a certain amount of reagent solution. It was difficult. On the other hand, in the chemical reaction in the microreactor, the mass of the reagent solution in the reaction region is extremely small, so that the temperature can be set quickly and uniformly. Therefore, it is possible to obtain a temperature condition suitable for the chemical reaction.

  As described above, a chemical reaction using a microreactor has many merits and is regarded as a promising next-generation reactor.

  However, one of the greatest concerns during microreactor operation is that mixing of different types of reagent solutions in the microreactor does not sufficiently proceed. In general, in a microreactor, mixing by stirring or the like is not promoted as compared with a reaction vessel (mixer) such as a test tube, a beaker, or a flask. Molecular diffusion and turbulent diffusion act to mix the fluid. Compared with molecular diffusion, turbulent diffusion has a great effect on mixing. For example, when you drop milk into coffee, you can intuitively understand that it is faster and more reliable to mix by turbulent diffusion by stirring with a spoon etc. than waiting for the milk to mix by molecular diffusion while looking still . Theoretically, the Reynolds number Re, which is the term of fluid engineering, is used as an indicator of the above matters. The definition formula of Reynolds number Re is shown in Formula 2.

  Here, V is a flow velocity, and ν is a kinematic viscosity coefficient. D is referred to as a representative dimension, and uses a cross-sectional dimension (width or height) of a flow path through which fluid flows. A flow with a small Re number is called laminar flow, and a flow with a large Re is called turbulent flow.

As an example of laminar flow and turbulent flow, FIGS. 2 and 3 show flow visualization photographs when an obstacle (cylinder) is placed in the flow field. For example, in FIG. 2 where Re≈32, it can be seen that the flow flows in a clean layer on the downstream side of the obstacle, and there is no turbulence. Such a beautiful laminar flow is called a laminar flow. However, in FIG. 3 where Re≈161, a staggered vortex street called Karman vortex street is formed on the downstream side of the obstacle, and it can be seen that mixing is promoted by the effect of the vortex. Although not shown, in the region where the Re number is 10 ³ to 10 ⁵ , vortices discharged from the left and right sides of the obstacle diffuse toward the downstream and the entire flow becomes irregularly turbulent. Such a flow field is called turbulent flow.

  In a pipe flow such as a flow in a microreactor, it is known that the Re number is about 1000, and a transition from a laminar flow to a turbulent flow is obtained. It can be said that the road width is large and the flow velocity is large.

  An example of a typical microreactor shape of the prior art is shown in FIG. The Re number in the mixing channel of the reactor is calculated assuming that the representative dimension D is 100 μm of the channel width, the flow rate is 0.001 m / s in the mixing channel, and the flowing fluid is water. Then

The Re number is a small laminar flow region. For this reason, it is predicted that the mixing channel is a clean laminar flow and mixing is not easily promoted.

FIG. 5 is an example of fluid analysis when two kinds of solutions are mixed in the reactor of FIG. As analysis conditions, an assumed substance (hereinafter simply referred to as substance A) having a molecular weight of 131 g / mol is introduced into inflow path A with a 1.0 mol / l aqueous solution (reagent solution A), and water (reagent solution B) is introduced into inflow path B. Each flows at a flow rate of 0.001 m / s. The diffusion coefficient of substance A to water was 6.9 × 10 ⁻⁸ cm ² / s. The contour map of FIG. 5 shows the volume concentration of the reagent solution A. From the analysis result of FIG. 5, in the microreactor of the prior art, it is gradually diffusing from the joint surface of the reagent solutions A and B in the mixing channel, but it can be seen that it is layered and flows to the downstream. It turns out that it is not promoting. When the flow rate in the mixing flow path is increased so as to promote the promotion of mixing by increasing the Re number, the reactor is increased in size due to an increase in friction loss in the reactor and an increase in the mixing distance. As shown in FIG. 36 (c), it is conceivable that the two fluids are joined to the meandering fluid channel and the two fluids are sufficiently mixed in a space-saving manner, but in this case, the friction loss further increases. Further, when measuring information such as the pressure, flow velocity, temperature, pH and concentration of the fluid in the fine channel, or when inputting energy such as vibration, heating and cooling to the fluid, as shown in FIG. The bent fine flow path has a complicated shape, so that installation of elements is complicated, and there is a difference in physical quantity between the inner periphery and the outer periphery of the bend, so that measurement and control are complicated. Therefore, it is difficult to increase the Re number in a microreactor, and it can be said that mixing depends on molecular diffusion rather than turbulent diffusion. For this reason, a conventional microreactor requires a long mixing channel, and a long time is required to complete sufficient mixing and chemical reaction.

  As described above, mixing of the reagent solution in the microreactor is governed by molecular diffusion. Molecular diffusion is a phenomenon caused by the Brownian motion of particles, and the diffusion distance is a function of temperature only. In other words, if the temperature is constant, the reagent solution to be mixed is formed as a very thin layer in the mixing channel of the microreactor, and if the interfaces of the thin layers are joined together, the mixing distance is reduced, so that rapid mixing can be obtained. .

  On the other hand, it is conceivable to reduce the mixing distance in the flow direction by decelerating the flow by enlarging the cross-sectional area of the flow path while forming an interface between layers of appropriate thinness.

  In order to solve the above problems, various types of fluid mixers have been proposed. For example, with a technique called superfocus, different reagent solutions are made into a multi-layered flow, and then the entire flow is passed through an extremely thin flow path, thereby shortening the mixing distance (width direction of the flow path) and promoting mixing. There is something to plan. However, since the flow rate increases as the flow path becomes thinner, the time for passing through the narrow flow path in the reactor is extremely short, and it is assumed that the mixing effect of the reactor is low.

  Moreover, the arrangement | positioning of the flow path etc. which are suitable for mixing by molecular diffusion are proposed. For example, in Japanese Patent Laid-Open No. 2001-120971, two plates are provided, one plate is provided with a liquid dividing fine groove having a divided flow path, and the other plate is formed with a mixing fine groove. A liquid mixer formed by superimposing and joining a liquid is described, in which a thin layer of liquid introduced from a divided flow path is obtained in a mixing fine groove.

  Further, as a conventional configuration, there is a mixing mechanism disclosed in Japanese Patent Application Laid-Open No. 2003-294596, in which two conveying channels are provided symmetrically with respect to the mixing channel.

  The conventional mixer and mechanism are intended to perform molecular diffusion mixing in the fluid mixing portion. Here, according to the inventor's investigation, effective mixing by molecular diffusion is to form a fluid to be mixed in a thin and uniform multilayer in the mixing portion, or to reduce the flow velocity while keeping the thin layer. Is achieved.

  However, the conventional liquid mixer as described above is not necessarily suitable for forming such a thin and uniform fluid layer.

  For example, the above-mentioned Japanese Patent Application Laid-Open No. 2001-120971 states that “the closer to the tip of the liquid mixing fine groove 5 the faster the liquid flow rate. There is a description that “the narrow groove 5 should be thicker as it gets closer to the tip” (see paragraph “0021”). However, if a multi-layered thin layer is formed and then increased in the height direction (direction perpendicular to the paper surface) in FIG. 5 of the publication, the diffusion distance increases, which is not suitable for good mixing. Further, FIG. 5 of the publication shows a multilayer of A layer and B layer, but has the following problems. That is, in the mixer, since the arrangement of the liquid dividing fine grooves 3 and 4 is not symmetrical with respect to the liquid mixing fine groove 5, the flow drifts at the portion flowing into the liquid mixing fine groove 5. Alternatively, flow separation occurs when the flow velocity is relatively high. In other words, it can be said that this mixer has a shape that tends to generate a flow having a strong three-dimensionality having flow components in the three directions of XYZ. When the flow in which the three-dimensionality is generated flows into the liquid mixing fine groove 5, in reality, it does not become a uniform thin layer as shown in the figure, and the thickness of the layer is different. As a matter of course, in the portion where the layer is thick, the diffusion distance of molecular diffusion is increased, so that mixing is not promoted.

  Furthermore, the above publication does not mention the length and thickness of each of the liquid dividing thin grooves 3 and 4. Since the liquid mixing fine groove 5 has a minute cross-sectional shape, the pressure loss of the fluid is large, and it seems that a large flow path loss occurs upstream and downstream of the liquid mixing fine groove 5. Therefore, it is surmised that some contrivance is required for each of the liquid dividing fine grooves 3 and 4, such as changing the thickness or length with respect to the flow direction of the liquid mixing fine grooves 5. In the shape described in the above publication, there is a high possibility that the flow rate flowing from each narrow groove into the liquid mixing narrow groove 5 is not uniform. The difference in flow rate from each narrow groove is caused by the difference in the thickness of each layer of the liquid A and liquid B in FIG. Naturally, the thickened layer does not promote mixing with the surrounding layers. In this prior art, the importance of making the thickness of each layer in the liquid mixing fine groove uniform by controlling the flow rate flowing into the liquid mixing fine groove from each fine groove is not considered at all.

  Further, in the mixing mechanism described in the above Japanese Patent Application Laid-Open No. 2003-294596, the conveying flow paths a, b1, and b2 are provided symmetrically with respect to the mixing flow path ab. It seems possible to obtain a uniform layer state in the path ab (see [FIG. 7]). However, this publication states that “at least two transport channels for transporting the same liquid are connected to the mixing channel from different sides on the basis of another transport channel for transporting another liquid. There is a description that “they need not be on the same plane as long as they are present” (see paragraph “0031”). Further, “the position where at least two transport channels for transporting the same liquid are connected is a position where the liquid sent to the mixing channel via the transport channel simultaneously joins the mixing channel. It may also be a position where one of these liquids joins first ”(see paragraph“ 0033 ”). Thus, in view of the disclosure that allows any connection form of the flow path without any distinction, this mixing mechanism is unfavorable for forming a uniform thin layer in the flow path for mixing. It cannot be said that the examination from the viewpoint of eliminating the element that causes the general flow has been made.

  Conventionally, in reagent mixing in a microreactor in a low Re number state that only depends on the mixing effect due to molecular diffusion, mixing of each reagent solution in the microreactor is not performed sufficiently, resulting in a decrease in yield and planned There were serious problems such as chemical substances not being synthesized. However, as described above, the prior art does not sufficiently cope with this problem. Therefore, there is room for further study and improvement regarding the promotion of mixing by molecular diffusion.

  The present invention has been made in view of the above-described problems, and can stably and easily form a multi-layered state of uniformly thinned reagent solutions in a mixing channel, and is a molecule that is preferable by ultrathin multilayering. A fluid mixer that can achieve the effect of diffusive mixing, or a state in which uniformly layered reagents are stacked in the mixing flow path, and the flow is decelerated in that state, resulting in a favorable molecular diffusive mixing effect. It is an object to provide a fluid mixer.

  In order to solve the above problems, the present invention has a mixing channel and a plurality of inflow channels connected to the mixing channel, and at least two kinds of fluids are respectively introduced from the plurality of inflow channels into the mixing channel to mix the fluids. In the fluid mixer, a plurality of flow path connection portions are provided in the mixing flow path by connecting the plurality of inflow paths at a predetermined interval in the flow direction. Provided is a fluid mixer characterized in that piping is provided so that different types of fluids are introduced.

  In the fluid mixer according to the present invention, it is preferable that the plurality of inflow channels are arranged symmetrically with respect to the mixing channel.

  In the fluid mixer of the present invention, the plurality of inflow paths are arranged on substantially the same plane as the mixing flow path, and at least two inflow paths for introducing the same kind of fluid in each of the flow path connecting portions. Is preferably connected to both sides of the mixing channel.

  Further, in the fluid mixer of the present invention, from the viewpoint of uniform flow rate of each inflow path, the length of each flow path of the plurality of inflow paths is set to be longer toward the downstream side of the mixing flow path. Good. Moreover, it is good to set it as the structure which made each cross-sectional area of these inflow path small so that it might be located in the downstream of a mixing flow path. Further, it is preferable that a resistor is provided in the plurality of inflow passages so that the fluid loss increases as the inflow passage is located downstream of the mixing flow passage.

  The fluid mixer of the present invention is a fluid mixer having a multilayer structure, wherein a mixing channel and a plurality of inflow passages connected to the mixing channel are provided on at least one layer, and at least the upper layer and / or the lower layer are provided. A supply tank having two kinds of fluids is provided, and a fluid is supplied from a predetermined supply tank to each inflow path by providing a vertical hole that connects the supply tank and the inflow path. it can.

  Moreover, in the fluid mixer of the present invention having the multilayer structure described above, it is preferable that the diameter of the vertical hole is made smaller as it is located downstream of the mixing flow channel from the viewpoint of uniform flow rate of each inflow channel. In addition, the supply tank for supplying the same kind of fluid can be divided into parts that can be fed with different back pressures, and the back pressure can be set to be lower as it is located downstream of the mixing channel. It is good to be.

  Further, in the fluid mixer of the present invention, from the viewpoint of uniforming the flow rate of each inflow path, the temperature in the vicinity of the plurality of inflow paths can be controlled, and the temperature is higher as it is located upstream of the mixing flow path. It is good that it can be set as follows. Further, the depth of the mixing channel may be made deeper as the part located on the downstream side thereof. Further, the cross-sectional area of the mixing flow channel in the downstream portion from the range having the flow channel connecting portion may be smaller than the cross-sectional area in the upstream portion.

  Further, in the fluid mixer of the present invention, from the viewpoint of further promoting the mixing, it is preferable that the mixing channel in the downstream portion meanders from the range having the channel connecting portion.

  Furthermore, the present invention includes the following inventions.

  (1) A processing device that performs a predetermined process on one or a plurality of fluids, a processing chamber that forms a disk-shaped processing space, an introduction channel that introduces the fluid into the processing chamber, and the processing A processing apparatus comprising: a discharge channel for discharging the fluid from a chamber, wherein the predetermined processing is performed while the fluid flows in a radial direction in the processing chamber.

  According to the invention described in (1), when the fluid flows in the radial direction in the disc-shaped processing space, the flow velocity is reduced because the flow path cross-sectional area is large, and therefore sufficient processing time can be obtained. it can. Therefore, for example, even if it is a fine processing space such as a microchip and it is difficult to obtain a stirring action by turbulent flow, the processing is performed by sufficiently performing the mutual diffusion action between the interfaces.

  (2) The processor according to (1), wherein the introduction flow path is provided on a central side of the processing space, and the outlet flow path is provided on an outer peripheral side of the processing space. .

  (3) The processor according to (1), wherein the outlet channel is provided on a central side of the processing space, and the introduction channel is provided on an outer peripheral side of the processing space. .

  (4) The processor according to any one of (1) to (3), wherein a plurality of the introduction flow paths are provided, and different fluids are introduced from these introduction flow paths.

  (5) The processor according to (4), wherein the plurality of introduction channels are provided coaxially.

  (6) In the invention according to any one of (1) to (5), a dividing plate that divides the processing space in the thickness direction is provided, and two processing spaces partitioned by the dividing plate are divided. A processor characterized by merging near an edge of a plate.

  (7) The processor according to any one of (1) to (6), wherein a plurality of the outlet channels are provided.

  (8) The processor according to (7), wherein the plurality of outlet channels are arranged in a circumferential direction.

  (9) The processor according to any one of (1) to (8), wherein the outlet channel is provided along a tangential direction of the processing chamber. Thereby, a swirl flow is formed, the processing space can be efficiently utilized, and the area occupied by the outlet channel can be reduced to reduce the size of the apparatus.

  (10) The processor according to any one of (1) to (9), wherein the processing space has a radial thickness distribution. Thereby, a flow-path cross-sectional area can be changed and a flow velocity can be adjusted.

  (11) The processor according to any one of (1) to (10), wherein a partition member extending in a radial direction is provided inside the processing space. Thereby, the flow of radial direction can be subdivided and adjusted.

  (12) In the invention described in (11), the partition member is provided so as to partition the processing space in a spiral shape. Thereby, a swirl flow is formed, the processing space can be efficiently utilized, and the area occupied by the outlet channel can be reduced to reduce the size of the apparatus.

  (13) The processor according to any one of (1) to (12), wherein a catalyst is provided in the processing space.

  (14) The processor according to any one of (1) to (13), wherein means for irradiating electromagnetic waves to a fluid inside the processing space is provided.

  (15) The processor according to any one of (1) to (14), wherein means for heating or cooling the fluid inside the processing space is provided.

  (16) The processor according to any one of (1) to (15), wherein means for vibrating or ultrasonically vibrating a fluid inside the processing space is provided.

  With these configurations, various desired reactions can be promoted in the processing space.

  (17) In the invention according to any one of (1) to (16), means for measuring a physical or chemical characteristic value of a fluid is provided inside the processing space. Processor. Thereby, various parameters can be adjusted based on the measurement result, and the process can be accurately controlled.

  (18) The processor according to any one of (1) to (17), wherein a plurality of the processing spaces are provided, and the fluid sequentially flows through them. As a result, a longer processing time can be secured and multistage processing can be performed.

  (19) The processor according to the item (18), wherein in the processing spaces adjacent to each other, the fluid alternately flows in the opposite directions in the radial direction.

  (20) The processor according to any one of (1) to (19), wherein a lead-out flow path is provided in a central portion of the second processing space.

  (21) The processor according to any one of (18) to (20), wherein the first and second processing spaces are coaxially connected in multiple stages. Thereby, a multi-stage processing space can be obtained with a compact configuration.

  (22) In the invention according to any one of (1) to (21), the introduction channel has an equivalent diameter of 1 cm or less, the diameter of the processing space is 10 cm or less, and the thickness of the processing space is 1 cm or less. A processor characterized by.

  (23) The processor according to any one of (1) to (22), wherein the processing space has a thickness of 1 mm or less. Even in such a fine processing space, the necessary processing time can be obtained.

  (24) introducing one or more fluids into a processing chamber forming a disc-shaped processing space, and mixing and / or chemistry with the one or more fluids while the fluid flows radially through the processing chamber. The processing method characterized by performing reaction.

  (25) In the invention described in (24), the function of measuring one or more of pressure, flow velocity, temperature, pH, etc. is used to measure the mixing situation and chemical reaction situation in real time, and this situation is negatively affected. A processing method characterized by performing an optimum mixing and / or chemical reaction by changing the pressure, flow rate, temperature, pH, concentration, etc. of the fluid to be returned.

  In the fluid mixer of the present invention, a plurality of flow paths are provided by connecting a plurality of inflow paths at predetermined intervals in the flow direction, and different types of fluids are introduced into adjacent flow path connections. Therefore, different types of fluids in the mixing channel are extremely thinned, and a flow field can be obtained by sequentially laminating with a uniform thickness to obtain a multi-layered flow field between two or more types of fluids. Mixing by molecular diffusion can be favorably promoted.

  In particular, in the minute mixing channel in the microreactor where mixing by molecular diffusion is forced because the flow field has a very low Re number, the reagent solution can be mixed in a short mixing channel and the yield can be reduced. It is possible to improve and shorten the chemical reaction time. If the mixing channel can be shortened, the microreactor can be miniaturized and the pressure loss in the reactor is also reduced. Reduction of the pressure loss in the reactor directly contributes to reducing the running cost of the micro reaction system. Furthermore, parallelization (numbering up) is performed to adjust the production volume of the micro reaction system. When thousands or tens of thousands of reactors are arranged in parallel to expand production volume, downsizing of one reactor greatly contributes to downsizing of the entire apparatus.

  Furthermore, according to the processing device described in the above (1) to (23) and the processing method described in (24) to (25), physical or chemical processing of a fluid can be performed with a simple shape and configuration. It is possible to provide a processing apparatus and a processing method that can be promoted or controlled and are inexpensive and efficient.

FIG. 1 is a diagram for explaining the progress of a chemical reaction handled in a microreactor. FIG. 2 is a diagram showing a laminar flow state for explaining mixing of liquids. FIG. 3 is a diagram illustrating a turbulent state in order to explain the mixing of the liquid. FIG. 4 is a schematic diagram showing an example of a flow path shape of a typical microreactor of the prior art. Reagent A (aqueous solution having a molecular weight of 131 g / mol and a concentration of 1.0 mol / l) flows from the upper inflow pipe at 0.001 m / s, and reagent B (water) flows from the lower inflow pipe at 0.001 m / s. FIG. 5 is a diagram showing the result of fluid analysis when two kinds of solutions are mixed in the reactor of FIG. FIG. 6 is a schematic diagram showing a schematic configuration of an embodiment of the present mixer. The branch pipe end of the upper layer plate and the lower layer plate are communicated with each other through a pothole, and the reagent is supplied to the upper layer plate. FIG. 7 is a schematic diagram showing a multilayer flow of reagent solutions A and B formed in the mixing flow path of the mixer. FIG. 8 is a schematic diagram showing a model of flow analysis in order to confirm the molecular diffusion effect by the mixer. Reagent A (aqueous solution having a molecular weight of 131 g / mol and a concentration of 1.0 mol / l) flows from the upper inflow pipe at 0.001 m / s, and reagent B (water) flows from the lower inflow pipe at 0.001 m / s. FIG. 9 is a diagram showing an analysis result in the model of FIG. FIG. 10 is a schematic diagram showing a model for calculating flow path loss in the mixer. FIG. 11 is a schematic view showing an embodiment of the present mixer in which the flow path length is suitably changed. FIG. 12 is a schematic view showing an embodiment of the present mixer in which the tube diameter is suitably changed. FIG. 13 is a schematic view showing an embodiment of the present mixer in which the diameter of the vertical hole communicating with the supply tank and the inflow passage is suitably changed. FIG. 14 is a schematic view showing an embodiment of the present mixer in which the back pressure of the supply tank is suitably changed. FIG. 15 is a schematic view showing an embodiment of the present mixer in which a resistor is suitably installed in the inflow channel. FIG. 16 is a schematic diagram showing an embodiment of the mixer in which the temperature of each inflow path is suitably changed in the flow direction. FIG. 17 is a schematic view showing an embodiment of the present mixer in which the mixing channel is suitably deepened toward the downstream side. FIG. 18 is a schematic diagram showing an embodiment of the present mixer in which the channel width is suitably reduced on the downstream side of the mixing channel. FIG. 19 is a schematic diagram showing an embodiment of the present mixer in which the width of the mixing channel is suitably increased according to the inflow of the reagent solution. FIG. 20 is a schematic diagram showing an embodiment in which the multistage reaction is performed on one mixer. FIG. 21 is a schematic diagram showing an embodiment in which a multistage reaction is performed on a plurality of mixers. FIG. 22 is a schematic diagram showing an embodiment of the present mixer in which the arrangement of one supply tank is changed. FIG. 23 is a schematic diagram showing an embodiment of the present mixer in which the downstream portion of the mixing flow path is meandering. 24 (a) and 24 (b) are diagrams showing the processor according to the embodiment of the present invention. 25 (a) and 25 (b) are diagrams showing a processor according to another embodiment of the present invention. FIGS. 26A to 26C are diagrams showing a processor according to another embodiment of the present invention. FIGS. 27A and 27B are diagrams showing the processor according to the embodiment of the present invention. FIGS. 28A to 28D are diagrams showing a processor according to the embodiment of the present invention. FIGS. 29A and 29B are diagrams showing a processor according to another embodiment of the present invention. 30 (a) and 30 (b) are diagrams showing a processor according to the embodiment of the present invention. FIG. 31A shows a conventional processor, and FIGS. 31B and C show a processor according to an embodiment of the present invention. FIG. 32A is a diagram showing a processor according to another embodiment of the present invention, and FIG. 32B is a diagram showing a conventional processor. 33A and 33B show a conventional processor, and FIGS. 33C and D show a processor according to another embodiment of the present invention. FIG. 34 is a diagram showing a processor according to another embodiment of the present invention. FIG. 35 is a diagram showing a processor according to another embodiment of the present invention. FIG. 36 (a) is a diagram showing a conventional standard micro-mixing processor, and FIGS. 36 (b) and (c) are diagrams showing a conventional micro-processor having a long mixing channel in order to take a sufficient diffusion distance. (D) is a figure which shows the processing device which is the conventional residence space for mixing. [Explanation of symbols] 10 .... Processing chamber 11, 12 .... Introduction flow path 13, 13A..Delivery flow path 16, 16b..Division member 17 Dividing plate 18 Columnar body 19 Columnar body 20 Heater 21 Transition portion 22 Communication flow Path 23 Dividing plate 25 Connection flow path 28 Pressure sensor 29 Flow rate sensor 30 pH sensor 31 Concentration sensor 32 Temperature sensor 43, 44 Introduction flow path 51 Heater 52 Titanium oxide layer 53 Cooler 54 Sunlight 56 Ultrasonic oscillator P Micro pump S Processing space

BEST MODE FOR CARRYING OUT THE INVENTION

  DESCRIPTION OF EMBODIMENTS Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings.

  FIG. 6 schematically shows a schematic configuration of a fluid mixer according to an embodiment of the present invention. This fluid mixer (hereinafter simply referred to as this mixer) is composed of two plates that are bonded together and joined together, and different types of reagent solutions are mixed on one side of the upper layer plate (or lower layer plate). And a plurality of inflow passages joined to the mixing flow channel at the flow passage connecting portion, and a predetermined reagent solution is supplied to each of the plurality of inflow passages in the upper layer plate (or lower layer plate) A supply tank is formed. The mixing channel and the plurality of inflow channels are formed on one upper layer plate, and all the channels are arranged on substantially the same plane. The supply tank and the inflow path communicate with each other through a vertical hole, and the reagent solution is supplied to the corresponding inflow path. The reagent solution supply tank is disposed below (or above) the layer having the mixing channel, and may be provided in a plurality of layers depending on the type and amount of the reagent to be supplied.

  The mixing flow path is provided with a plurality of flow path connection portions in which two of the plurality of inflow paths are connected at approximately equal intervals. The two inflow passages connected to one flow path connecting portion are connected to the mixing flow path so as to merge from both sides thereof, and are symmetrically arranged with the mixing flow path interposed therebetween. Thus, the same amount of the predetermined reagent solution is supplied from both side surfaces of the mixing channel at each channel connecting portion. Furthermore, each inflow path has a different length between adjacent flow path connecting portions, and is connected to a different supply tank according to the length, so that different types of reagent solutions are supplied.

  In this mixer, an inflow channel with a short channel length corresponding to the reagent solution A and an inflow channel with a long channel length corresponding to the reagent solution B are alternately piped and connected in the flow direction of the mixing channel, Two different reagent solutions flow alternately in the same amount. According to the configuration of the present mixer, the same type of reagent solution is allowed to flow in the same amount from both sides on the same surface at the same flow rate in the respective flow path connection portions, and is different between adjacent flow path connection portions. Since the same amount of each type of reagent solution is allowed to flow in, the flow having strong three-dimensionality does not occur in the flow path connection portion and the mixing flow path. Therefore, in the mixing channel at the position where the flow of all the reagent solutions is completed, the fluid of each reagent solution appears to have an extremely thin layer (see an enlarged view in FIG. 7). In this way, the diffusion distance of each layer of the reagent solution is reduced, so that mixing is promoted.

  The details of the material and handling of the plate used and the method for forming the micro flow path and supply tank to the plate follow the conventional method of photolithography technology commonly used in semiconductor engineering. The present mixer can also be manufactured using materials and methods well known in the art based on the disclosure of the present application. Any known means can be applied to the method of driving the fluid from the supply tank to each inflow path. For example, pressure driving by a pump or the like and / or electric driving by electrophoresis or electroosmotic flow or the like can be used. Can be used.

Flow analysis was performed to confirm the molecular diffusion effect in this mixer. FIG. 8 shows the analysis model. In order to compare with the analysis result of the conventional mixing mechanism in FIG. 5, the assumed solution (hereinafter simply referred to as “substance A”) having a molecular weight of 131 g / mol in the inflow channel of the reagent solution A has a 1.0 mol / l aqueous solution Reagent solution A) and water (reagent solution B) flow into inflow channel B at a flow rate of 0.0001 m / s, respectively. Similarly, the diffusion coefficient of the diffusion substance A with respect to water was set to 6.9 × 10 ⁻⁸ cm ² / s.

  The analysis results are shown in FIG. Compared with the analysis result of FIG. 5, it was found that the present mixer clearly diffuses faster, and the mixing of the reagent solution surely proceeds even in a short mixing channel. This is because the different reagent solutions flow alternately from both sides of the mixing flow path as they go to the downstream part of the mixing flow path, whereby the fluids of the different reagent solutions overlap as a thin layer of uniform thickness, forming a multilayer. This is because mixing by molecular diffusion is promoted. For example, in the case of the mixer shown in FIG. 8, 20 layers of each reagent solution are formed in the width direction of the mixing channel. Theoretically, it is estimated that each reagent solution layer of about 5 μm was formed in the mixing channel having a width of 100 μm, and it is considered that each reagent solution layer became extremely thin and mixing was accelerated rapidly.

  For example, there are cases such as the Friedel-Crafts reaction that has been obtained with high selectivity using a reactor capable of obtaining a multi-channel of 25 μm (S. Suga et al., Chemical Communications, 2003, pages 354-355, "Highly Selective Fridel-Crafts Monoalkylation Using Micromixing"). Under the reaction conditions, the selectivity using a tube having a diameter of 500 μm was not improved. On the other hand, it is considered that by obtaining a multilayer of 25 μm, molecular diffusion occurs efficiently, and the reaction progresses ideally to improve the selectivity.

  Next, the flow rate adjustment of each inflow channel will be described.

  As described above, in this mixer, in order to promote mixing by molecular diffusion in the mixing channel, it is important that the fluid layer of each reagent solution can be formed in a substantially uniform thickness. It is highly preferable to make the flow rate from to the mixing channel uniform. However, the above analysis was carried out by defining the flow rate of each inflow channel with boundary conditions. Actually, the inflow amount from each inflow channel to the mixing channel changes due to the channel loss of the mixing channel. It is predicted that Therefore, the channel loss in the mixed channel portion was estimated.

Here, it is assumed that the cross-sectional shapes of the mixing channel and the inflow channel are rectangular, and the hydraulic loss is obtained for each to examine the channel loss. From the upstream side to the downstream side of the mixing channel, the inflow paths are A ₁ to ₅ and B ₁ to ₅ , and the respective junctions are A ₁ to ₅ junctions and B ₁ to ₅ junctions (see FIG. 10). ), Other parameters are as follows.

  Here, the following equation is used for the loss coefficient λ of each flow path.

Under the above conditions, the loss h _A1B1 up to the merging point of the mixing channels A1 to _B1 is expressed by the following equation.

Similarly, the loss h _XX in the mixing channel between the inflow channel junctions downstream from the B1 junction is expressed by the following equation.

The flow rate of each inflow path can be made uniform by adjusting the flow path loss of each inflow path in consideration of the loss h _XX in the mixing flow path. That is, the flow rate in each inflow path located on the downstream side can be ensured by lengthening the inflow paths on the downstream side in order to balance the flow path loss that increases in the flow direction of the mixing flow path. .

  Here, the loss in the inflow channel of length L is

It becomes. Therefore, in order to obtain the loss h of h _A1A2 by making the length of the inflow channel A ₂ longer than A ₁ by L _A2 ,

It becomes.

From the above equation, the flow path length L _A2 that should be longer than A ₁ in the inflow path A ₂ is

It becomes.

Similarly, the channel lengths L _A3 to _A5 to be added to the inflow channels A _{3 to} A ₅ respectively

It becomes. Also in the inflow path B ₂ .about.B _5, the flow path length L _B1 ~ _B5 be longer than B ₁ represents can be determined in the same manner as described above, so that the following equation, respectively.

  FIG. 11 schematically shows an embodiment in which the length of each inflow path is suitably changed so that the flow rate is uniform based on the above calculation results.

  The above trial calculation is an example calculated under various assumptions, and the coefficients in the above formula are the inflow path of the mixer and the wall surface properties of the mixing flow path, the flow path width, the flow velocity, and the accompanying factors. It is necessary to change the Re number appropriately and recalculate the trial calculation.

Further, the length L of each inflow path is constant, and the flow rate of each inflow path can be made uniform by changing the pipe diameter d of each inflow path. In this regard, the following estimation was made. The loss of h _A1A2 is obtained with the _tube diameter of A ₂ being d ₂ . However, flow rate:

Is constant.

It becomes.

Likewise A ₃ tube diameter d ₃ of the inlet channel of ~ _5-5 respectively

It becomes.

  If the length of the inflow channel L is 4600 μm and the pitch p of the inflow channel is 200 μm, the tube diameter d5 of the inflow channel A5 needs to be manufactured with a tube diameter of about 70% of the tube diameter d of the inflow channel A1. FIG. 12 schematically shows an embodiment in which the pipe diameter is adjusted based on the trial calculation result.

  This trial calculation is also an example calculated under various assumptions. For the actual inflow channel of the mixer and the wall surface property of the mixing channel, the channel width, the flow velocity, and the accompanying change in the Re number. It is necessary to make a suitable change and recalculate.

  Further, the flow rate can be made uniform by various methods other than the adjustment by the length of the inflow passage and the pipe diameter according to the flow path loss of the mixing flow path as described above. For example, the following embodiment is mentioned.

  The mixer shown in FIG. 13 is a device in which the diameter of the vertical hole communicating with the supply tank and the inflow path is suitably changed, and the inflow path positioned on the downstream side suppresses the flow pressure to equalize the flow rate of each inflow path. is there. The mixer of FIG. 14 changes the back pressure of a supply tank suitably, and aims at equalizing the flow volume of each inflow path similarly. The mixer shown in FIG. 15 has a uniform flow rate by installing various resistors that block the flow of valves and the like in a predetermined inflow path so that the flow is suppressed toward the inflow path located on the downstream side. It is. The mixer of FIG. 16 is provided with means for suitably changing the temperature in the vicinity of each inflow path in the flow direction. That is, the temperature of the inflow channel connected to the upstream portion of the mixing channel is set high, and the temperature of the inflow channel connected to the downstream portion of the mixing channel is set low, thereby changing the viscosity of the reagent solution flowing in, thereby making the flow rate uniform. It is intended.

  Further, as shown in FIG. 17, a shape in which the mixing channel is deepened toward the downstream side is also effective in making the flow rate uniform. When the shape of the mixing channel is constant, each reagent solution flows into the mixing channel, so that the flow rate of the mixing channel increases as it goes downstream, and the channel loss increases accordingly. Therefore, by increasing the cross section of the mixing flow channel in the depth direction (direction perpendicular to the plane where the mixing flow channel and the inflow channel are located) like the mixer of FIG. It is possible to reduce the speed increase in the mixing channel without increasing the thickness. Needless to say, changing the mixing channel so as to increase in the width direction is not preferable because the thickness of each reagent solution layer may be increased to suppress mixing due to molecular diffusion.

  Further, as calculated above, the flow path loss in the mixing flow path is quite large, and it is not easy to equalize the flow rate of each inflow path to a sufficiently satisfactory level. Therefore, as shown in FIG. 18, appropriately adjusting the channel width of the mixing channel is also effective in promoting diffusion mixing. The mixer of FIG. 18 increases the width of the mixing channel in the portion where the reagent solution is multi-layered (that is, the range where the inflow channel is connected), and in the downstream portion where the multi-layer of the formed reagent solution flows. This is a mode in which the width of the mixing channel is sharply narrowed. According to this aspect, as the entire reagent solution multilayer becomes thinner in the downstream portion, each layer is uniformly thinned, so that an extremely thin reagent solution layer with a constant width can be obtained relatively easily. In this case, the width of the mixing channel in the part where the reagent solution is to be multilayered may be increased according to the inflow of the reagent solution (see FIG. 19).

  Furthermore, the other aspect regarding this mixer is shown below.

  In this mixer, a multistage reaction using three or more kinds of reagents can be performed on one plate. In this case, the present invention may be applied to a part of the reagent mixture. For example, as shown in FIG. 20, the reagent solution A and the reagent solution B are rapidly mixed in one inflow path, and the reaction product stream C generated by the first mixing and the reagent solution D from the other inflow path are mixed. Alternately flow into the mixing channel. In the case of mixing the reagent solution A and the reagent solution B, the reaction is immediately completed with almost perfect yield, but this aspect may be considered when the mixing of the reaction product stream C and the reagent solution D is relatively difficult to promote. Would be preferred.

  Moreover, although this mixer may perform multistage reaction on one mixer as mentioned above, each stage can also be performed on each separate mixer. FIG. 21 shows an embodiment in which a plurality of the present mixers are combined to mix three or more kinds of reagent solutions.

  Further, in this mixer, the supply tank for supplying the reagent solution to the inflow path may be provided in the same layer as the inflow path and the mixing flow path if possible (see FIG. 22).

  Moreover, in this mixer, the mixing flow path part through which the multilayer flow of the reagent solution flows can be meandered to promote diffusion (see FIG. 23). In this way, the mixing time can be obtained while keeping the overall size of the mixer small, which is effective in promoting mixing. Furthermore, since the mixing is promoted by the action of centrifugal force at the bent portion of the mixing flow path, it is more effective.

  24 (a) and 24 (b) show a processing device applied to a chemical liquid mixing apparatus as one embodiment of the present invention. FIG. 24 (a) is a cross-sectional view, and FIG. 24 (b) is a front view. It is sectional drawing seen from. The chemical liquid mixing apparatus is configured on, for example, a microchip, and includes a processing chamber 10 in which a disk-shaped processing space S is formed, and a pair of introduction flows that merge from both sides of the processing chamber 10 to the center thereof. The channels 11 and 12 and the outlet channel 13 extending linearly outward in the radial direction are provided on the outer peripheral portion of the processing chamber 10. In this embodiment, four outlet channels 13 are provided at equal intervals in the circumferential direction. However, as long as a radial flow from the center to the outside can be formed, the number of outlet channels 13 is one or more appropriate numbers. Can do.

  In this embodiment, first and second reservoirs 14 and 15 are formed in the first and second introduction flow passages 11 and 12, respectively, and the first and second micropumps P and P, respectively. Is provided. As the micropump P, various known principles and types can be appropriately employed. The first and second reservoirs 14 and 15 communicate with a liquid supply source (not shown).

  Hereinafter, the operation of the micro processor configured as described above will be described.

  When the respective micropumps P are operated, the first and second liquids (chemical solutions) from the first and second reservoirs 14 and 15 respectively have a disc-like shape through the first and second introduction channels 11 and 12. It is introduced into the central part of the processing space S. These two liquids collide with each other at the center of the processing space S, flow in a mixed state and change the direction outward in the radial direction. Since the processing chamber 10 has a small thickness, the two liquids each flow while forming a laminar flow, and in this process, they diffuse and mix with each other at the interface where the two liquids contact. The liquid that has reached the outer periphery flows out of the processor from the outlet channel 13.

  When the fluid moves from the center to the outside in the disc-shaped processing space S, the cross-sectional area of the flow path gradually increases, and the overall flow velocity becomes considerably smaller than that of the introduction flow paths 11 and 12. Therefore, since sufficient time for diffusion at the interface between the two liquids can be obtained, sufficient mixing can be performed even when the mutual diffusion coefficients of the two liquids are small. Moreover, since the cross-sectional area of the flow path is large, the pressure loss in the processing space S that is the mixing portion is reduced, and the performance of the micropump P does not need to be great. Furthermore, since the processing chamber 10 is circular, it can be manufactured with relatively simple processing and therefore at low cost.

  25 (a) and 25 (b) are other embodiments of the present invention, and are sectional views as seen from the same axial direction as FIG. 24 (b). In FIG. 25A, the processing chamber 10A is formed so that the outer peripheral portion of the processing space S expands in a spiral shape, and the outlet channel 13A extends in the tangential direction at the outermost peripheral portion of the maximum diameter of the processing space S. Is formed. Thereby, the swirl component can be given to the flow of the two liquids in the processing chamber 10 to be stabilized. Further, efficient mixing using the entire space is performed without forming a dead zone in which liquid does not flow inside the processing space S. Further, the entire space can be reduced by inclining the outlet channel 13A so as to approach the tangential direction.

  FIG. 25B shows a case in which a plurality of partition members 16 extending in the radial direction are provided so as to partition the processing space S in a spiral shape. Thereby, a spiral flow can be stabilized.

  26 (a) to 26 (c) show another embodiment of the present invention. Two outlet channels 13B are formed so as to face each other at the outer periphery of the processing space S, and the processing chamber 10B. A plurality of partition members 16 extending in the radial direction are provided so as to partition the inner processing space S in a spiral shape. In these embodiments, the angle θ formed between the outlet channel 13B and the radial direction is 90 degrees, and the outlet channel 13B and the partition member 16 are inclined in the same direction. In the embodiment of FIG. 26 (a), as in the case of FIG. 25, a swirl component can be given to the flow to be stabilized. In addition, a dead zone where no liquid flows inside the processing space S is not formed, and efficient mixing using the entire space is performed. Further, the entire space can be reduced by inclining the outlet channel 13B so as to approach the tangential direction.

  In FIG. 26B, in the configuration of FIG. 26A, the partition member 16b is formed to extend to the center of the processing space S toward the introduction flow path. In this way, in addition to the above-described operation of FIG. 26A, the liquid flowing into the processing space S from the introduction flow paths 11 and 12 is guided by the partition member 16b and flows separately. A situation in which the liquid flows while being unevenly distributed is avoided. The partition members 16b may be further extended to the center and connected to each other.

  In FIG. 26C, a second partition member 16 c that partitions a further downstream portion is provided between the partition members 16 b extending to the center of the processing space S. Accordingly, it is possible to prevent a decrease in contact area between two liquids and an increase in pressure loss due to the insertion of a large number of long partition members while realizing the stabilization of the swirl component.

  The angle θ formed between the outlet channels 13A and 13B and the radial direction in FIGS. 25A to 26C is arbitrary from −90 degrees to 90 degrees, and the number of outlet channels 13A and 13B. Is also optional. In addition, the shape, inclination angle, number, etc., of the partition members 16, 16b, 16c can be set as appropriate.

  FIG. 27 shows another embodiment of the present invention, which is a processor for reacting three kinds of gases. In the processing chamber 10C of this embodiment, a dividing plate 17 that divides the processing space S in the thickness direction is provided. In this embodiment, the dividing plate 17 has a diameter that is approximately ½ of the diameter of the processing space S. The processing space S includes a first space S1 and a second space S2 on both sides of the dividing plate 17, and A third space S <b> 3 on the outer side in the radial direction of the dividing plate 17 is formed. The processing chamber 10C has a thickness on the outer side that is thinner than the central portion, so that the flow path cross-sectional area of the third space S3 does not become excessively large. Although only the processing space S is shown in FIG. 27, any of the types shown in FIGS. 24 to 26 can be used for the outer shape of the processing chamber 10C and the arrangement of the lead-out paths.

  In this embodiment, a plurality of columnar bodies 18 formed of a material containing the first catalyst are arranged in the first space S1, and the dividing plate 17 is fixed to one wall of the processing chamber 10C by the columnar bodies 18. Has been. Coaxial first and second introduction flow paths 11C and 12C are connected to the center of the first space S1, and the first and second introduction flow paths 11C are connected to the second space S2. , 12C, a third introduction flow path 12D is connected from the opposite side.

  In the third space S3, a plurality of columnar bodies 19 formed of a material containing the second catalyst and a plurality of heaters 20 for heating to a desired temperature are arranged. The heater 20 has a plate shape extending in the radial direction, and also has a function as the partition member 16 shown in FIG. As the heater 20, a heater using a heating wire, a heater using a Peltier element, or the like can be appropriately employed. In this embodiment, the thickness is reduced at the portion 21 that transitions from the first and second spaces S1, S2 to the third space S3, and the cross-sectional area of the flow path is reduced. Therefore, the flow rate of the gas is increased at the transition portion 21, thereby preventing the heating of the heater 20 from being propagated upstream by heat conduction and causing an undesirable reaction on the upstream side. The first and second catalysts are selected to promote the reaction performed in each space, and the same or different types of catalysts are appropriately selected.

  Hereinafter, the operation of the micro processor according to the second embodiment configured as described above will be described.

  In this processor, the first to third gases flow into the processing space S from the first to third introduction flow paths 11C, 12C, and 12D, respectively, by pressure feeding or suction means (not shown). The first and second gases are introduced into the central portion of the first space S1, mixed here, and then flow outward. At this time, the first catalyst contained in the columnar body 18 promotes the first reaction between the first and second gases, and as a result, a gaseous intermediate is generated.

  This intermediate gas flows out to the transition part 21, joins and mixes with the third gas that has flowed through the second space S2, and further flows outward through the third space. The mixed gas is heated by the heater 20 in the third space S3 to generate a final product by the second reaction caused by the action of the second catalyst, which is discharged from the outlet channel 13B.

  In the above, since the cross-sectional area of the gas flow path decreases with the transition portion 21 to the third space S3 as a boundary, the flow velocity does not greatly decrease in the third space S3. Therefore, the heating of the heater 20 is propagated upstream by heat conduction, and the situation such as deterioration of gas or generation of undesirable reactants is prevented on the upstream side, and efficient and stable reaction processing is performed. Can do.

  28 (a) to 28 (d) show another embodiment of the present invention, which is a liquid mixing apparatus as in FIGS. 24 to 26. FIG. These drawings are the same cross-sectional views as FIG. 24A, and the reservoir and the micropump are omitted.

  In the processing chamber 10E of the embodiment of FIG. 28A, there is also a disk-shaped second processing space S12 on the downstream side of the disk-shaped first processing space S11 as shown in FIG. Is provided. The second processing space S12 communicates with the first processing space S via a communication channel 22 on the outer periphery of the first processing space S11. In this embodiment, the communication flow path 22 is provided so as to communicate with the entire circumference. However, the communication flow path 22 may be provided at a predetermined position in the circumferential direction as in the lead-out flow path 13B shown in FIGS. Moreover, you may arrange | position the division members 16, 16b, and 16c as shown in these figures. In this embodiment, the second processing space S12 is an annular space provided on the second introduction flow path 12E side so as to surround it. An annular outlet channel 13E extending in the axial direction is provided on the inner end side of the second processing space S12.

  In the mixing apparatus of this embodiment, the first liquid and the second liquid are introduced into the central portion of the first processing space S11 and flow outward in the radial direction, as in the previous embodiment, and the outer peripheral portion. Is further introduced into the second processing space S12 from the communication channel 22, flows radially inward, and flows out from the inner end portion through the outlet channel 13E. Thus, by providing two disk-shaped processing spaces S11 and S12, a flow path having a distance nearly twice that of the embodiment shown in FIG. 24 is formed, and therefore the processing time is significantly increased. be able to. Further, since the processing spaces S11 and S12 have a sufficient flow path cross-sectional area, the pressure loss does not become excessively large.

  FIG. 28B shows a mixing apparatus according to another embodiment, in which two introduction channels 11F and 12F are formed on the same side of the processing chamber 10F. Therefore, the first processing space S21 and the second processing space S22 can be formed by the dividing plate 23. In this embodiment, since the outlet channel 13F can be provided on the axis, the structure becomes simpler. In FIG. 28C, a larger number of processing spaces S11 to S15 are provided so as to overlap with each other through the communication channels 22a to 22d. Further, in FIG. 28 (d), a larger number of processing spaces S21 to S24 are provided so as to overlap with each other via the communication channel 25 on the axis. It goes without saying that this makes it possible to obtain a longer processing time.

  FIG. 29 shows another embodiment of the present invention, which is a liquid reaction processor. The structure of the processing chamber 10C is basically the same as that shown in FIGS. 24 to 26, but may be applied to each of the embodiments shown in FIGS. In this embodiment, a pressure sensor 28, a flow velocity sensor 29, a pH sensor 30, a concentration sensor 31, and a temperature sensor 32 are arranged at equal intervals in the circumferential direction in the processing chamber 10J. These sensors measure the physical or chemical characteristic values of the fluid in the processing space S, and these pieces of information are input to a control device (not shown). Based on these information, the control device operates various liquid feeding system and tempering system adjusting means upstream of each introduction flow path 11J, 12J, and reacts to obtain a desired state. Control. Since the flow in the processing space S is symmetric with respect to the central axis, even if the sensors are arranged at different positions in the circumferential direction if the radius is the same, the same measurement as when the state quantity at the same point is measured is possible. .

  For example, the pressure sensor includes a strain gauge type, a piezoresistive effect, a capacitance type, and the like, and the flow rate sensor includes a pitot tube type, a hot wire type, an optical type, an electromagnetic type, and the like. Moreover, there are a glass electrode type, an ISFET electrode type, etc. as pH sensors, and an ion sensor, a biosensor, etc. as concentration sensors. Further, any of a thermocouple, a resistance temperature detector, a thermistor, etc. may be used as the temperature sensor. Note that the type and mounting position of the sensor are not limited to these.

  FIG. 30 shows still another embodiment of the present invention, which is a liquid mixing apparatus. In the processing chamber 10K of this embodiment, the two introduction flow paths 11K and 12K are provided in parallel with the processing space S, and open to the processing space S through the bent portion 33 and the bent portion 34, respectively. By using such a structure, the mixing and reaction apparatus of the present invention can be configured in a more planar manner, and can be easily incorporated into a chip-like microfluidic device.

  FIG. 31 shows an embodiment in which the processing device of the present invention is used in the microchannel. FIG. 31 shows an example of a flow path in which a chemical reaction occurs, and FIG. 31 (a) shows a circular pipe flow path having an inner diameter of 1 mm according to the conventional method. If a 0.5 ml / min chemical solution is introduced here and a circular flow path is allowed to flow until a reaction time of 60 seconds elapses, a circular tube length of about 63 cm is required. FIG. 31 (b) shows a processing device according to the present invention, wherein a processing chamber 10L is formed with a disk-shaped processing space S having an inner diameter of 1 mm in the thickness direction, and an introduction channel 11L having an inner diameter of 1 mm is connected to the center thereof. ing. If a 0.5 ml / min chemical solution is introduced here and the treatment space S is allowed to flow until a reaction time of 60 seconds elapses, the radius of the treatment space S is about 1.3 cm. From this, it can be seen that the reactor can be miniaturized by using the processor of the present invention.

  FIG. 31C shows still another embodiment of the processor of the present invention. In the processing chamber 10M, the thickness of the disk-shaped processing space S is increased toward the outer side in the radial direction. Thereby, the radius of the disk can be further reduced by decelerating the flow velocity in the outer portion of the processing space S. In general, microchemical reactions often use channels with dimensions of about 1 mm or less, but if the thickness of the outer periphery of the processing space S is increased to 3 mm as shown in the figure, a radius of about 9 mm is sufficient. The area of the device can be further reduced.

  FIG. 32 is an example of a flow path for mixing two types of chemical solutions. In FIG. 32 (a), in the processing chamber 10N, the introduction channels 11N and 12N having an inner diameter of 100 (m) are connected to the central part of the disc-shaped processing space S having a thickness of 10 (m) from the direction facing each other. 32 (b) shows a conventional method in which introduction channels 43 and 44 having an inner diameter of 100 (m) are connected to a straight pipe channel 45 having an inner diameter of 10 (m. Generally, in order to promote diffusion. It is desirable to reduce the distance required for diffusion, since both types of chemical solutions in FIG.32 are introduced into a narrow channel having a representative dimension 10 (m), the diffusion distance in the direction orthogonal to the flow is reduced. However, in FIG. 32 (b), the cross-sectional area of the flow path becomes 1/200 after merging and the flow velocity is significantly increased. Therefore, in order to sufficiently advance the diffusion, it is necessary to increase the length of the straight pipe flow path 45 in the flow direction. On the other hand, in FIG. The mixture solution is rapidly decelerated to have the same cross-sectional area as the sum of the cross-sectional areas of the introduction flow paths 11N and 12N at a diameter of 500 (m), and the flow velocity does not increase excessively. Diffusion can be sufficiently advanced without making the diameter excessive.

FIG. 33 shows an embodiment used in a large polystyrene polymerization reactor. When polymerizing 100% pure styrene to polystyrene using a non-catalytic / thermally initiated polymerization reaction, according to known data, if reacted at 160 ° C. for 3 hours, about 90% of the styrene is converted to polystyrene. Consider a reactor charged with 20000 kg / h styrene under these conditions. The specific gravity of styrene at 160 ° C. is about 0.78 g / cm ³ , so the volume flow rate at the inlet is 25.6 m ³ / h. Here, the reaction order of this reaction is 1, and the calculation is approximate, and the change in specific gravity of the solution due to the progress of the reaction is not considered.

Regarding such a reaction, the volume ratio of the complete mixing tank reactor and the plug flow reactor is such that the conversion rate is 90% to 0.9 / (1-0.9) / ln (1 / (1-0.9). From the condition that the reaction time is 3 hours, the volume of the plug flow type is 25.6 × 3 = 76.8 m ³ , and the complete mixing tank type is 76.8 × 3.9 = 299. a 5 m ^3. the plug flow type to achieve this volume, a straight tubular conventional, for example a diameter of 2m × length 24.4 m (FIG. 33 (a)), complete mixing tank type, diameter 7m × length On the other hand, in the processing device of the present invention, the volume is the same as that of the plug flow type, and in a single stage, as shown in FIG. A disk-shaped processing space S having a diameter of 7 m and a thickness of 2 m is formed, and the multi-stage (two stages) has two stages of the processing space S having a diameter of 5 m and a thickness of 2 m, as shown in FIG. Even complete Extremely small than if tank than plug flow tubular becomes possible configuration that does not take the area.

  FIG. 34 shows another embodiment of the present invention, which is an example of an air cleaner for removing toluene which is a harmful substance in the atmosphere. In the processing chamber 10P of this embodiment, only one introduction flow path 11 is provided, and a motor-equipped fan 47 is disposed in this. One wall 50 of the disk-shaped processing space S is made of a transparent material so that sunlight 54 enters the processing space S. On the other wall surface 49 of the processing space S, a heater 51 is provided on the inner side, a titanium oxide layer 52 that is a photocatalyst is formed on an intermediate part, and a cooler 53 is provided on the outer part.

  In such a configuration, the air containing toluene taken in by the motor-equipped fan 47 is sent into the processing space S and flows outward. Then, the heater 51 is preheated to a temperature suitable for the chemical reaction in the inner part, and toluene is decomposed into water and carbon dioxide by the action of sunlight 54 and the catalyst, that is, the photocatalytic reaction, in the intermediate part. And it cools to suitable temperature with the cooler 53 in an outer side part, and is discharged | emitted in air | atmosphere from the derived | lead-out flow path 13B.

  In this embodiment, sunlight is used, but a dedicated lamp may be used. Alternatively, the wall surface 50 may be changed to a light reflective material, and the lamp may be directly attached to the inside of the wall surface 50 facing the processing space S. Further, as the configuration of the processing space S, an appropriate configuration shown in FIGS. 24 to 28 can be adopted.

  FIG. 35 shows another embodiment of the present invention, which is a mixing device that mixes two fluids that are difficult to mix. In the processing chamber 10Q of this embodiment, the ultrasonic oscillation elements 56 are installed evenly in the circumferential direction of the processing space S. As the configuration of the processing space S, an appropriate configuration shown in FIGS. 25 to 26 can be adopted.

For example, substances such as water and oil cannot be mixed by molecular diffusion alone. In this apparatus, by installing the ultrasonic oscillation element 56 in the processing chamber 10Q and irradiating two fluids in the processing space S with ultrasonic waves, mixing is promoted even in fluids that are difficult to mix such as water and oil. The Since the flow velocity decreases from the center of the processing space S toward the outer side in the radial direction, if the ultrasonic oscillation element is installed at a position on the outer side in the radial direction, the effective time of exposure to the ultrasonic wave increases, and the mixing effect is large.

Claims (38)

A fluid mixer having a mixing channel and a plurality of inflow channels connected to the mixing channel, wherein at least two kinds of fluids are respectively introduced into the mixing channel from the plurality of inflow channels, and the fluid is mixed;
The mixing channel is provided with a plurality of channel connecting portions by connecting the plurality of inflow channels at a predetermined interval in the flow direction, and different types of fluids are introduced at adjacent channel connecting portions. A fluid mixer characterized in that the pipe is piped like this. The fluid mixer according to claim 1, wherein the plurality of inflow channels are arranged symmetrically with respect to the mixing channel. The plurality of inflow paths are arranged on substantially the same plane as the mixing flow path, and at least two inflow paths for introducing the same kind of fluid from each of the flow path connecting portions from both sides of the mixing flow path The fluid mixer according to claim 1, wherein the fluid mixer is connected. The fluid mixer according to any one of claims 1 to 3, wherein each of the plurality of inflow passages has a length that is longer toward a downstream side of the mixing passage. The fluid mixer according to any one of claims 1 to 4, wherein each of the plurality of inflow passages has a smaller cross-sectional area as it is located downstream of the mixing passage. 6. The resistor according to claim 1, wherein a resistor is provided in the plurality of inflow passages such that the fluid loss increases as the inflow passage is located downstream of the mixing passage. Fluid mixer. A fluid mixer having a multilayer structure, wherein a supply tank having a mixing channel and a plurality of inflow channels connected to the mixing channel on at least one layer and having at least two kinds of fluids in the upper layer and / or the lower layer, respectively And a fluid is supplied from a predetermined supply tank to each inflow path by providing a vertical hole for communicating the supply tank and the inflow path. The fluid mixer according to any one of the above. 8. The fluid mixer according to claim 7, wherein the diameter of the vertical hole is made smaller toward the downstream side of the mixing channel. The supply tank for supplying the same kind of fluid can be divided into portions that can be fed with different back pressures, and the back pressure can be set to be lower as it is located downstream of the mixing channel. The fluid mixer according to claim 7. The temperature in the vicinity of the plurality of inflow paths can be controlled, and the temperature can be set higher as the temperature is higher on the upstream side of the mixing flow path. The fluid mixer according to item. The fluid mixer according to any one of claims 1 to 10, wherein the depth of the mixing channel is made deeper in a portion located on the downstream side thereof. The cross-sectional area of the mixing flow path in the downstream portion from the range having the flow path connecting portion is made smaller than the cross-sectional area in the upstream portion thereof, according to any one of claims 1 to 11, Fluid mixer. The fluid mixer according to any one of claims 1 to 12, wherein the mixing channel in the downstream portion meanders from the range having the channel connecting portion. A processor that performs a predetermined process on one or more fluids,
A processing chamber forming a disk-shaped processing space;
An introduction flow path for introducing the fluid into the processing chamber;
A lead-out flow path for leading the fluid from the processing chamber,
The processing device, wherein the predetermined processing is performed while the fluid flows in a radial direction in the processing chamber. The processor according to claim 14, wherein the introduction channel is provided on a central side of the processing space, and the outlet channel is provided on an outer peripheral side of the processing space. The processor according to claim 14, wherein the outlet channel is provided on a central side of the processing space, and the introduction channel is provided on an outer peripheral side of the processing space. The processor according to any one of claims 14 to 16, wherein a plurality of the introduction channels are provided, and different fluids are introduced from these introduction channels. The processor according to claim 17, wherein the plurality of introduction flow paths are provided coaxially. A dividing plate that divides the processing space in a thickness direction is provided, and two processing spaces partitioned by the dividing plate are joined in the vicinity of an edge of the dividing plate. Item 19. The processor according to any one of items 14 to 18. The processor according to any one of claims 14 to 19, wherein a plurality of the outlet channels are provided. The processing device according to claim 20, wherein the plurality of outlet channels are arranged in a circumferential direction. The processor according to any one of claims 14 to 21, wherein the outlet channel is provided along a tangential direction of the processing chamber. The processor according to any one of claims 14 to 22, wherein the processing space has a thickness distribution formed in a radial direction. The processing device according to any one of claims 14 to 23, wherein a partition member extending in a radial direction is provided inside the processing space. The processing device according to claim 24, wherein the partition member is provided so as to partition the processing space in a spiral shape. The processor according to any one of claims 14 to 25, wherein a catalyst is provided in the processing space. 27. The processor according to claim 14, further comprising means for irradiating electromagnetic waves to a fluid inside the processing space. The processor according to any one of claims 14 to 27, wherein means for heating or cooling a fluid inside the processing space is provided. The processor according to any one of claims 14 to 28, further comprising means for vibrating or ultrasonically vibrating a fluid inside the processing space. 30. The processor according to any one of claims 14 to 29, wherein means for measuring a physical or chemical characteristic value of a fluid is provided inside the processing space. The processor according to any one of claims 14 to 30, wherein a plurality of the processing spaces are provided, and the fluid sequentially flows through them. 32. The processor according to claim 31, wherein in the processing spaces adjacent to each other, the fluid alternately flows in the opposite directions in the radial direction. The processing device according to any one of claims 14 to 32, wherein a lead-out flow path is provided in a central portion of the second processing space. The processor according to any one of claims 31 to 33, wherein the first and second processing spaces are coaxially connected in multiple stages. 35. The processing device according to claim 14, wherein the introduction channel has an equivalent diameter of 1 cm or less, a diameter of the processing space of 10 cm or less, and a thickness of the processing space of 1 cm or less. . 36. The processing device according to claim 14, wherein the processing space has a thickness of 1 mm or less. One or more fluids are introduced into a processing chamber forming a disc-shaped processing space, and mixing and / or chemical reaction is performed on the one or more fluids while the fluid flows in the radial direction in the processing chamber. A processing method characterized by the above. Using the function to measure one or more of pressure, flow velocity, temperature, pH, etc., measure the mixing situation and chemical reaction situation in real time, and negatively feed back this situation to the pressure and flow velocity of the inflowing fluid 38. The processing method according to claim 37, wherein optimal mixing and / or chemical reaction is performed by changing temperature, pH, concentration and the like.