JP2002292274A - Flow type fine reaction passage, reaction apparatus and reaction method - Google Patents

Abstract

PROBLEM TO BE SOLVED: To suppress clogging of a main flow passage (reaction passage) and to improve the reaction rate in a flow type fine reaction passage, a reaction apparatus and a reaction method. SOLUTION: In the flow type fine reaction passage 31 provided with a main flow passage RA having a fine flow passage cross-sectional surface area and an introducing flow passages RB joined to the main flow passage RA and for joining/reacting a 1st reaction fluid FA passing through the main flow passage RA with a 2nd reaction fluid FB passing through the introducing flow passage FB, a discharge port 33a of the tip of an inserted part 33b formed in the main flow passage RA by extending the introducing flow passage RB and a wall surface 32a forming the main flow passage RA are separated from each other.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a flow-type micro reaction channel, a reaction apparatus, and a reaction method for causing a chemical reaction while flowing a reaction fluid in a micro flow channel.

[0002]

2. Description of the Related Art In recent years, since a chemical reaction can be performed efficiently, a technique of causing a chemical reaction while allowing two or more reactants to flow through a reaction path having a small flow path cross-sectional area has been attracting attention. This is because the specific surface area (surface area per unit volume) of the reactant in the reaction path can be increased by making the flow path cross-sectional area of the reaction path very small, and a high heat exchange efficiency with the outside can be obtained. Since the ratio of the area of the interface between the reactants to the flow rate of the reactants (that is, the contact area between the reactants) is increased, a high mass transfer efficiency between the reactants is obtained, and the chemical reaction can be performed efficiently. it is.

[0003] Regarding a flow-type chemical reaction method using such a microchannel, for example, in a liquid phase reaction, P.I. Fl
etcher et al. reported that they carried out a Suzuki coupling reaction and were able to synthesize the desired product, cyanobiphenyl, in a higher yield compared to large-scale experiments [Chemistry in Britain, 1999 ( Nocv.),
35-38].

[0004] J. J. R. Burns et al. Reported on the performance of a nitration reaction (TransIchemE, Vol 77, Part 77).
A, May 1999, 206-211); J. Harri
Son et al. reported that a diazo coupling reaction was performed using an electric pumping method (J. Am. Chem. Soc. 19
97, 119, 8716 to 8717), further, R. D. Chamb
ers et al. report a fluorination reaction in a microchannel (WO99 / 22857). Also, M.
Gheorghe et al., Have reported on electrolytic oxidation reaction (Proc.SPIE-Int.Soc.Opt.Eng.3680, 1159~1163,
1999).

Although not intended for chemical synthesis, many examples relating to rapid analysis and analysis of a small amount of a sample using a chemical reaction channel having a small channel cross section as described above have been reported. For example, D.I. Jed H
Arrison has reported on microanalysis (Science, 1993, 261, 895). Hereinafter, an example of a specific configuration of a flow-type reaction apparatus using such a microchannel,
This will be described with reference to FIGS.

[0006] apparatus shown in FIG. 14 (a), as shown, and is configured to include introduction pipe 101A, 101B and the reaction tube 102. Inlet tube 101A, different reaction fluids with each other, which is injected into the 101B F _A, F _B flows from one another opposite direction with respect to the confluent portion 102b of the T-connector 102a, to flow inside of the reaction tube 102 in a mixed state.

[0007] The reaction tube 102 is placed in a thermostat 103, and the mixture is kept at a temperature optimum for the reaction.
The reaction is allowed to proceed while flowing through the inside of the tube. Then, it is fed in a constant temperature bath 103 downstream of the distillation apparatus 104, the target substance (reactant) is taken out by the distillation separator 104. In the example shown in FIG. 14A, two types of reaction fluid F
_A, there is shown an example to perform a chemical reaction by F _B, the type of the reaction fluid is not limited to this, Figure 14 reaction fluid introducing unit 101 (a) for example, in FIG. 14 (b) Instead of the reactant introduction unit 101 'shown in the figure, a chemical reaction can be performed by three different reaction fluids F _A , F _B , and F _C. That is, first, the reaction fluids F _A and F _B
14, flows into the junction 102b of the T-type connector 102a through the introduction pipes 101A and 101B in the same manner as in FIG. 14 (a), and is mixed and reacted. Further, at the junction 102b 'of the T-type connector 102a', the introduction pipe is mixed with the reactant fluid F _C fed is made to react from 101C.

[0008]

However, in the above-described reaction apparatus shown in FIGS. 14A and 14B, since the cross-sectional areas of the flow paths 101A to 101C and 102 are very small, 101A~101C, likely to occur is obstruction in the 102. If a blockage occurs in the flow paths 101A to 101C and 102, the flow of the reaction fluids F _A , F _B , F _{C, and the} like is impeded. which leads to deterioration of safety deterioration of and operation.

The smaller the equivalent diameter of the flow path, the greater the possibility of blockage in the flow path.
The equivalent diameter d of the flow path such as 1A to 101C and 102 is 1
In the case of a microchannel having a diameter of 000 μm (1 cm) or less, the occurrence of blockage is extremely concerned compared to a channel having a diameter larger than that. The equivalent diameter ds is defined by the flow path cross-sectional area As and its circumferential length Ls according to the following equation (1). If the flow path is circular, the diameter becomes the same. ds = 4 × As / Ls (1)

[0010] although it depends on the equivalent diameter of the channel, several μm number to 1
Occlusion may also be caused by a minute solid of about 0 μm (a minute foreign substance or the like mixed in a reaction substrate or a fluid (chemical substance)). A method has been reported in which a reaction fluid is allowed to flow through a flow channel after filtering fine particles to remove fine solids.

[0011] However, solid or in a chemical reaction
When the highly viscous liquid is produced, of course, these
The product can not be removed in advance as described above. Therefore,
Reaction device as shown in FIGS. 14 (a) and (b)
To reactions that produce solids or highly viscous liquids.
It is extremely difficult to do. In particular, such microchannel
In the reaction channel they are often distributed in a laminar flow region. this
Therefore, for example, in the case shown in FIGS.
These reactions fluids F _A, F_BIs the merging section 102
b, 102b '
And the reaction fluid F through the interface S_A, F_BIs mass transfer (expansion)
To react).

[0012] The reaction fluid F _A in the reaction proceeds, a mixture of F _B, the reaction fluid F _A, the reaction product and the wall surface 10 at the same time the F _B
2c is a state in which the product is most likely to adhere to the wall surface 102c, and therefore, the product is in contact with the wall surface 102c.
Once in contact with the c, already reactant fluid F _A, it is preferred that the reaction of F _B was complete. However, FIG.
As (b), when the interface S is formed, in the interface S, the reaction fluid F _A in the reaction in progress, a mixture of F _B,
As shown in FIG. 16 (a), the interface S is in contact with the wall surface 102c at the edge Sa, so that the product is centered on the edge Sa.
It will adhere to, this would lead the inner wall 102
Product c is attached one after another, there is a risk that eventually the reaction tube from being closed.

Further, the fluid in the fine channel as described above
(Sample) F_A, F_BThe reaction fluid F _A, F_BThrough but the interface S
Performed by diffuse. Therefore, the fluid F
_A, F_BIncrease the speed of the reaction between
That) for the fluid F_A, F _BDegree of diffusion between
It is important to increase the degree of diffusion
Can be realized by increasing the area of the interface S.

[0014] However, the area of the interface S (interfacial area) are those corresponding to the representative diameter of the reaction channel (representative length), Figure 16
If the cross-sectional area of the reaction flow path 101D is circular as shown in (a), the representative diameter becomes the flow path diameter b at the maximum, and the cross-sectional area of the reaction flow path 101C 'as shown in FIG. Is a square, the maximum representative length is one side length a of this square. Therefore, by increasing the interfacial area, the fluid F _A, there is a limit in increasing the rate of reaction between F _B, no remarkable effect is obtained.

[0015] The present invention has been made in view of the above-described problems, and can suppress blockage of a main flow path (reaction tube).
It is an object of the present invention to provide a flow-type micro reaction channel, a reaction apparatus, and a reaction method capable of improving a reaction rate.

[0016]

For this reason, the flow-type microreaction channel of the present invention (Claim 1) comprises a main flow channel having a fine flow channel cross-sectional area and one or more flow channels converging with the main flow channel. A flow-type minute reaction flow path having an introduction flow path, wherein the first reaction fluid flowing through the main flow path and the second reaction fluid flowing through the introduction flow path join / react with each other; The discharge ports at the distal end of the insertion section formed in the main flow path are extended from one or more of the introduction flow paths, and the wall surface forming the main flow path is separated from each other.

In this case, the equivalent diameter of the cross section of the main flow path is 1
cm or less (claim 2). Further, the insertion portion is distally, have parallel portion that flows and main channel parallel to the wall surface forming the main flow path, from the discharge port, the flow direction of the first reaction fluid in the It is preferable that the second reaction fluid is discharged in the same direction (claim 3).

Further, the distance between the tip of each of the insertion portions and the wall surface forming the main flow path is 500 μm.
It is preferable that the above setting be made (claim 4). Further, it is preferable that the length of the parallel portion is longer than 100 times the equivalent diameter of the cross section of the introduction flow channel (claim 5). Further, the equivalent diameter of the cross section of the introduction channel is 500 μm to 1 mm.
(Claim 6).

In this case, the cross section of the introduction path may be circular (claim 7), or the cross section of the introduction path may be rectangular (claim 8). In addition, it is preferable that the number of the introduction flow paths merging with the main flow path is in a range of 1 to 3 (claim 9). The reactor of the present invention (Claim 10)
Has at least one flow-type microreaction channel according to any one of claims 1 to 9, and has at least one of a main flow channel and an introduction flow channel of the flow-type microreaction channel. It is characterized by comprising a reaction fluid driving device for flowing the reaction fluid.

[0020] In this case, a plurality of flow through-type fine reaction flow channel juxtaposed to form a reaction channel assembly so as to be integrated, it may be constituted by stacking a plurality of the reaction flow passage assembly (claim 1
1). Further, in order to adjust the temperature of the reaction fluid in the flow-type micro reaction channel, a temperature control flow channel for flowing the temperature control fluid is provided adjacent to the flow-type micro reaction channel. it is preferable (claim 12).

In addition, the flow-type minute reaction channel has 100 or more channels.
It is preferable that provided for in the range of 3000 (claim 13). The reaction method of the present invention (claim 14),
For the first reaction fluid flowing through the main flow path of the small flow passage cross-sectional area, from the introduction passage, the second reaction fluid, is characterized in that for combining so as not to contact the wall surface forming the main flow path I have.

[0022]

Embodiments of the present invention will be described below with reference to the drawings. 1 to 11 are views showing a flow-type micro reaction channel, a reaction apparatus, and a reaction method as one embodiment of the present invention. The reaction apparatus as an embodiment of the present invention, as shown in FIG. 1, the predetermined reaction substrate and the tank 1A for accommodating the (first reaction fluid) F _A, prescribed reaction substrate (the second reaction fluid) tank 1 for accommodating the F _B
B and the reaction substrate F _A and reactant F _B and is reacted predetermined material (product, the desired product) and the reactor (reaction channel assembly) 3 to produce a reaction substrate F from the tank 1A the _a, and a pump (reaction fluid circulating device) 2A for feeding to the reactor 3 via a pipe P _a, the reactant F _B from the tank 1B,
It is configured to include a pump (reaction fluid circulating device) 2B for feeding to the reactor 3 via a pipe P _B.

[0023] Incidentally, the reaction fluid F _A, in the case of a F _B is hard to flow is dissolved in advance in a solvent tank 1A, 1B
You may make it supply to. Further, etc. using pre filter to prevent the reactor 3 is closed, the fluid F _A, F _B
From may be previously remove fine dust or the like. Specifically, for example, a tank 1 fluid F _A, the F _B through the filter
A and 1B may be supplied, or a filter may be interposed in the pipes P _A and P _B.

[0024] Inside the reactor 3, and where adapted to circulate the heat medium F _H as further temperature adjusting fluid, thereby the reaction substrate F _A that flows through the reactor 3 and the reactant F _B but it is adapted to be adjusted to the optimum temperature for the reaction. The heat medium F _H is driven by the pump 2H. After being sent to the reactor 3, the heat medium F _H is heat-exchanged by the heat exchanger 5 and then again pumped through the pipe P _H.
To be sent to Although the temperature adjusting fluid using heating medium is here intended to be set according to the type of reaction, sometimes cooling medium is used.

The fluid F _G from the reactor 3 is sent to the pipe P through _G purification device 4, in this purification unit 4, a given substance (object from a fluid F _G by a known method such as distillation or extraction being adapted material) F _S is purified target substance F _S
Is fed to the tank 1C via the pipe P _S, the residue (material removal target substance F _S from a fluid F _G) F _D is adapted to be fed to the tank 1D. Incidentally, as sent to the reactor 3 the residue F _D again, by circulating the residue F _D between the tank 1D and the reactor 3, efficiently configured to produce a target substance F _S You may.

As shown in FIG. 2A, a plurality of reactors 3 (here, four reactors) as one embodiment of the present invention are used.
Flow type micro-channel (hereinafter, simply referred to as reaction channel) 3
1 is configured to integrally mounted side by side in parallel to the casing 30. Further, adjacent to each reaction channel 31,
The heating medium F _H pipe for circulating (temperature adjusting flow path) 35 is provided a fluid F _A that flows through the reaction channel 32, so as to heat the F _B.

In FIG. 2 (a), the reaction apparatus is shown as having a configuration in which four flow-type micro reaction channels are provided for convenience. However, from the viewpoint of productivity of the target substance, many flow-type micro reaction channels are used. It is preferable to have a reaction channel, for example,
The number is 50 to 5,000, and more preferably 100 to 3,000. In any case, the number of flow-type minute reaction channels provided in the reaction apparatus is appropriately set.
It doesn't matter.

As shown in FIGS. 2 (a) and 2 (b), each reaction channel 31 has a circular tube (hereinafter referred to as a pipe or outer tube) 32 having a small inner diameter, and a tip (discharge port) at the outer tube 32. A circular pipe (hereinafter, referred to as a pipe or an inner pipe) 33 into which the 33d is inserted is configured. Discharge port 33a at the tip of inner tube 33
It is positioning spaced apart from the outer tube wall surface 32a. Here, the inner tube 33 is inserted substantially perpendicularly to the outer tube 32, the insertion portion 33b is bent in the direction of flow of the reaction fluid F _A in the outer tube 32, outer tube wall 32
a substantially has a parallel parallel portion 33d.

Here, the minute inner diameter means that the equivalent diameter of the flow path in the tube wall is 1 cm or less. Further, the discharge port 33a means a space (that is, a cross section of the flow path) surrounded by an inner wall surface at the tip of the inner pipe 33. Also, referring to FIGS. 1 and 2 (a), the outer tubes 32 of each reaction channel 31 are gathered at the upstream end and the downstream end of the reactor 3, respectively, and the upstream port thereof is connected to an external port. is connected to the pipe P _a, the downstream port 3C is connected to an external pipe P _G. Similarly, each pipe 35 for temperature adjustment are assembled respectively at the upstream and downstream ends of the reactor 3, the upstream port and the downstream port is connected to an external pipe P _H, respectively.

[0030] As described above, by the configuration shown in FIG. 1,
The reaction substrate F is supplied from the tank 1A to the outer tube 32 of each reaction channel 31.
_A is supplied, it is made from the same time the tank 1B so that reactant F _B in the inner tube 33 of the reaction channel 31 is supplied.
Then, as shown in FIG. 2 (b), the inner tube 3 is connected to a flow path (main flow path) R _A in the outer pipe 32 through which the reaction substrate F _A flows.
Channel formed in the 3 so that the reaction agent F _B from (introduction channel) R _B is discharged. Accordingly, the downstream side from the tip 33a of the inner tube 33, the main passage R _A, the reaction fluid F _A, and the F _B functions as the reaction channel for reaction (reaction regions) R _R.

The introduction flow path R in the outer pipe 32_BIs but an extension
Preceding the insertion portion 33b of the inner tube 33 formed so as to be
Discharge port 33a of the end, the main passage R as described above_AForm
Is spaced apart from the outer tube inner wall surface 32a which, also, this
Of the insertion portion 33b is substantially parallel to the outer tube inner wall surface 32a.
It is set to be (insertion portion 33b outside tube wall
Had 32a substantially parallel to the parallel portion 33d distally
). Further, the reaction channel R _R(The main channel R_A) Has an equivalent diameter
A microchannel of 1 cm or less;_A, F_BYes
Also in the laminar flow state, the reaction channel R_RWill flow in.

[0032] Therefore, as shown in FIG. 2 (b), (c) , in a state where the reactant F _B is completely included in the reactant F _A, reactant fluid F _A, F _B is the reaction channel R _Because we distribute _R ,
Reactant fluid F _A, the interface S of the F _B is adapted to be completely separated from the outer tube wall surface 32a. In interfacial S, the reaction fluid F _A, react with the purified solid material (or high viscosity liquid material) by the F _B, the reaction fluid F _A in the reaction in progress, but a liquid mixture of F _B are mixed at the same time, Interface S is outer tube inner wall 3
2a is completely separated from the inner wall surface 32a.
In addition, the contact between these solid substances and the liquid mixture at the same time is prevented.

Further, since the reactant F _B is completely included in the reactant F _A, reactant fluid F _A, the interface F _B is, reactant F _B
Since it is formed on the outer peripheral surface, the interface area can be increased as compared with the conventional case. For example, as shown in FIG. 3, the inner diameter (reaction channel R diameter _R) phi _A of the outer tube 32 and 2r, the reaction fluid F _A the same amount to each other in the reaction channel R _R, circulating F _B as, i.e., the reaction fluid F _a in the reaction channel R _R, so that the flow area is F _B flows equal, when setting the inner diameter phi _B of the inner tube 33, an inner diameter phi _B is, r / √2.

On the other hand, according to the above-described prior art, if the same amount of the reaction fluids F _A and F _B are allowed to flow, the interface S
Are formed as shown by a two-dot chain line in FIG. The ratio of the interface area between the flow-type microreaction channel of the present invention and the conventional flow-type microreaction channel is determined by the interface length (inner pipe 33) indicated by a dashed line.
(= 周 2πr) and the interface length indicated by the two-dot chain line (up to the inner diameter length 2r of the outer tube 32). In the example shown in FIG. Is about 2.22 times that of the conventional reaction channel. Also, if the pipes 32 and 33 was a square, respectively, when the same calculation, the reaction flow path of the present invention, over the prior art, 2√2 (= 2.
83) field area of the times can be obtained.

As described above for the description of the prior art,
The area is increased, via the interface S reaction substrate F_ABut
Reactant F_BVelocity and reactant F_BBut the reaction substrate F
_ATo increase the rate of diffusion into the
Therefore, in the present reaction channel, the reaction fluid F_A, F_Bof
The reaction can be performed efficiently. Main reaction channel
3 is described above, but as shown in FIGS.
The discharge port 33a at the tip of the inner pipe 33 is
a from the fluid F _A, F_BInside the interface
It is intended to be separated from the wall surface 32a.
The distance d between the mouth 33a and the inner wall surface 32a is particularly limited.
Not limited to, at least the fluid F _A, F_BProduct of (mixed
In a state in which liquid and solid or high-viscosity liquid) are mixed, flow
Body F_A, F_BInterface S of, stable and spaced apart from the inner wall surface 32a
Is preferably set to 50 μm or more so that
Preferably 100 μm or more, most preferably 500 μm
m or more. Here, the inner wall surface 3 according to the discharge port 33a
The distance d from the fluid F_A, F_BFlow direction to a vertical
In the direction, the fluid in the discharge port 33a F_BOuter edge of
(I.e. the inner wall surface 33e of the inner tube 33) between the inner wall surface 32a
Indicates the narrowest distance.

It should be noted, the introduction path R equivalent diameter of the flow path cross-sectional area (inner diameter here is the inner tube 33) _B are, for example 10μm~5
mm, preferably 100 μm to 3 mm, more preferably 500 μm to 1 mm. The length L of the parallel portion 33d is preferably the traveling direction of the fluid F _B through the parallel portion 33d is a distance sufficient to settle in a direction along the parallel portion 33d, for example, the discharge port 33a
Introduction passage equivalent diameter of the cross section of the R _B (inner tube 33, here in
Is a inner diameter) 0.5 times excess of D (L / D> 0.5), long (L / D> 5) is favored over 5 times, 5
It is more preferably longer than 0 times (L / D> 50), and most preferably longer than 100 times (L / D> 100).

Further, the inner wall surface 33e of the outer tube wall surface 32a and the inner tube 33, the sample liquid F _A, as long as it does not adversely affect the F _B and its synthesis reaction is not limited to the material, and polishing, For example, work such as providing fine unevenness, or surface treatment such as coating treatment may be performed. Also,
The downstream side of the outer tube wall surface 32a in a particularly inner tube discharge port 33a to the (i.e. reaction regions R _R located) within the wall, the sample liquid F _A, a catalyst for promoting or inhibiting the synthesis of F _B May be carried.

Further, sample liquid F _A, the purification of F _B, the tank 1A, may be previously performed before the placing in 1B,
It may be performed in the pipe 32, 33. Similarly, the purification treatment after the synthesis reaction may be performed in the pipes 32 and 33 in addition to the purification device 4 or instead of installing the purification device 4. The content of the purification is not limited, but includes, for example, pH adjustment, removal of unnecessary water-soluble inorganic salts, removal of unnecessary fat-soluble inorganic salts, removal of unnecessary water-soluble organic substances, removal of unnecessary fat-soluble organic substances. Removal, etc., and specifically, for example, is performed by extraction and purification by adding other chemicals, or a property that an objective substance or an unnecessary substance is separated under specific conditions such as a specific temperature or a specific pressure. It is performed using.

Further, in the reaction region R _R of the outer tube 32, the temperature / pressure of the fluid need not be uniform, for example, the temperature distribution by heating locally using a heating means such as a heater (not shown) Alternatively, a pressure distribution may be provided by disposing a pressure resistor in the outer tube 32. Further, by arranging a plurality of introduction passages for reactant F _B as the inner tube 33 so that the discharge port is in a different position with respect to the flow direction of the reactant F _A, the sample liquid F in the reaction region R _{R a,} may have a distribution in concentration of F _B. In any event, such temperature / pressure / density distribution in the reaction zone R _R may be appropriately selected depending on the reaction.

Each of the pipes 32 and 33 does not need to have a uniform cross section of the flow path, and may be changed as necessary. For example, the cross section diameter of the flow path may be increased or decreased. Absent. The chemical reaction performed using the present flow-type micro reaction channel, reaction apparatus and reaction method is not limited at all, and examples thereof include an esterification reaction, a transesterification reaction, an amidation reaction, a transamidation reaction, and an acid anhydride. things synthesis reaction, the acid chloride synthesis reaction, hydrolysis reaction, dehydration reaction, reduction reaction, reductive amination reaction, oxidation reaction, dehydrogenation reaction, a nitro group synthesis reaction, nitration reaction, electrolytic oxidation, electrolytic reduction reaction, Electrolytic coupling reaction, Hoffman rearrangement reaction, Schmidt reaction, Curtius reaction, Rosen reaction, alkene oxide rearrangement reaction, ether rearrangement reaction, other rearrangement reaction, Diels-Alder reaction, hetero Diels-Alder reaction, other concerted reaction, hydrogen cyanide reaction,
Quaternary Hofmann elimination reaction of the ammonium salt, dealcoholization reaction of ethers, decarboxylation reaction, de-SO ₂ reaction, nucleophilic substitution reaction, halogenation reaction, halogen addition reaction, hydrogen halide addition reaction Michael addition reaction, hydrin hydroboration ,
Hydroformylation reaction, cyanohydrin reaction, acetal reaction, hemiacetal reaction, aldol reaction, Wit
tig reaction, alkylation reaction, other addition reactions, acylation reactions, Suzuki coupling reactions, the diazotization reaction, diazo coupling reaction, addition reaction of an organometallic, metal exchange reaction of the organic metal.

Examples of the halogenation reaction include chlorination, bromination, fluorination, and iodination. The target reaction substrate is not limited, and examples thereof include aromatic compounds, heterocyclic compounds, carbonyl-containing compounds, and sugars. Can be Examples of the addition reaction of an organic metal include an addition reaction of an organolithium compound to an organic functional group and an addition reaction of a Grignard reagent to an organic functional group. Specific examples of the functional group used in the reaction include a cyano group, an alkylcarbonyl group, an arylcarbonyl group,
Examples include an alkoxycarbonyl group, an aryloxycarbonyl group, and an aminocarbonyl group, specifically, an acyl group, a methoxycarbonyl group, an ethoxycarbonyl group,
Propyloxy carbonyl group, an aminocarbonyl group, dimethylaminocarbonyl group. Specific examples of Grignard reagents include methyl magnesium bromide, ethyl magnesium bromide, propyl magnesium bromide, phenyl magnesium bromide, methyl magnesium chloride, ethyl magnesium chloride, propyl magnesium chloride, and phenyl magnesium chloride.

[0042] The reduction reaction, metals, alloys, it is possible to use a metal hydride, in particular as a metal hydride, lithium aluminum hydride, sodium aluminum hydride, lithium borohydride, borohydride It is possible to use sodium and their deuterium substitutes. The metal-exchange reaction of an organic metal includes a reaction between an organic metal compound and a compound having active hydrogen, and a reaction between an organic metal compound and a compound having a halogen atom. Examples of the reaction between the organometallic compound and the compound having active hydrogen include a lithiation reaction of a secondary amine, and specifically, a synthesis reaction of lithium diisopropylamide from butyllithium and diisopropylamine.

[0043] Also, when the reaction substrate and reaction agents is a liquid,
The use of a reaction solvent is not essential, it may be present if desired. Specific examples of preferred solvents include water, liquid ammonia, organic solvents, supercritical solvents, and ionic liquids. As the organic solvent, aliphatic hydrocarbons, aromatic hydrocarbons, ketones, aldehydes, et -
Examples include ters, esters, amines, sulfoxides, alcohols, nitriles, heteroaromatic compounds, halogen solvents, carboxylic acids, and mineral acids include sulfonic acids and phosphoric acids. As the supercritical solvent, supercritical water, supercritical carbon dioxide and the like can be used.
Further, a mixture of these at an arbitrary ratio, the reaction substrate itself, a reactant, a target substance, or a reaction solution can be used as a solvent.

The reaction fluid may be a fluid between miscible with each other, it may be a fluid between immiscible. Fluids that are mixed are solutions that use the same or relatively similar organic solvents, or solutions that use a highly polar organic solvent such as methanol and water, and fluids that are not mixed are hexane. And a solution using a highly polar solvent such as methanol.

The products produced by the present flow-type micro reaction channel, reaction apparatus and reaction method are not limited, but if they are solid, for example, metals, alloys, metal oxides,
Quaternary ammonium salts, quaternary pyridinium salts, alkali metal halide salts, alkaline earth metal halide salts, alkali metal hydroxides, alkaline earth metal hydroxides, boron-containing compounds, aluminum alkoxides, polymers, condensates and the like Is a mixture containing

The flow-type fine reaction flow channel according to an embodiment of the present invention is carried out by the reactor is constructed as described above, the following technique (reaction method according to one embodiment of the present invention) [Hereinafter, FIG. 1 and FIG.
This will be described with reference to FIG. In other words, the reaction substrate F _A is supplied from the pump 2A to the outer tube 3 of each reaction channel 31 of the reactor 3.
2 and likewise by the pump 2B, the reactant F _B
Is supplied to the inner pipe 33 of each reaction channel 31 of the reactor 3.
The heat medium F _H is circulated by a pump 2H, in the reactor 3 by the heating medium F _H is the reaction fluid F _A, is controlled to the optimum temperature for the reaction of F _B.

[0047] Incidentally, if it is necessary, the sample liquid F _A, in the pipe 32, 33 prior to passed through F _B to the reactor 3,
Solvent or may be allowed to flow inert gas into the reaction,
If necessary, the reactor itself may be dried. Each reaction channel 31 in the reactor 3, an inner tube 33, the reactant F _B, to discharge the reactant F _A flowing through the outer tube 32.
The outer tube 32 is a laminar flow state, a state in which reactant F _B is completely enclosed by reaction substrate F _A as shown in FIG. 2 (c), fluid interface S is separated from the inner wall surface 32a Formed.

[0048] Therefore, the reaction fluid F _A, the reaction product of F _B, the reaction fluid F _A, F liquid mixture and the inner wall surface 3 at the same time _B
There is an advantage that contact with the outer tube 2a can be suppressed, and the blockage of the outer tube 32 can be prevented, thereby stably producing the target substance. Further, since the area of the interface S may be increased from the conventional reaction fluid F _A, can increase the reaction rate of the F _B, there is an advantage that it is possible to improve the productivity of the target substance.

The insertion portion 33b of the inner tube 33 has a parallel portion 33d formed substantially in parallel with the outer tube inner wall surface 32a on the distal end side, and the insertion portion 33b is provided inside the outer tube 32 (in the main flow path). since directed in the traveling direction of the reactant F _a of R _a), reactant F _B from the discharge port 33a (insertion portion 33b)
Flows parallel to the inner wall surface 32a in the same direction as the reaction substrate F _A , so that the above-mentioned state in which the interface S is separated from the inner wall surface 32a can be stably realized, and the above-mentioned advantages can be more effectively obtained.

[0050] Further, the temperature control fluid (heat medium in this case)
The reaction temperature (the temperature in the reactor 3) can be controlled by F _H , and there is an advantage that the reaction can be effectively performed. In particular, when the reaction is performed at a high or low temperature, heat recovery can be measured by the heat exchanger 5, and there is an advantage that the recovered heat can be reused. Further, the flow-type minute reaction channel, the reaction apparatus, and the reaction method are not limited to the above-described embodiments, and various modifications can be made without departing from the gist of the present invention. Hereinafter, FIGS. 4 to 1
Various modifications to the above-described embodiment will be described with reference to FIG. 1, but the same components and the like as those in the above-described embodiment will be denoted by the same reference numerals, and description thereof will be omitted.

[0051] In the above embodiment, as shown in FIG. 2 (b), the inner tube 33 constituting the introducing flow passage R _B, is folded inside the straight outer tube 32 which constitutes the main passage R _A The distal end of the insertion portion 33b is made parallel to the inner wall surface 32a of the outer tube. For example, as shown in FIG.
The straight inner tube 33 is inserted through the bent portion of
3b may be configured to be parallel to the downstream inner wall surface 32a (to have a parallel portion).

[0052] In the aforementioned embodiment, as shown in FIG. 2 (b), the insertion portion 3 of the inner tube 33 to be inserted into the outer tube 32
3b has a parallel portion 33d on the distal end side thereof, which is parallel to the outer tube inner wall surface 32a. As shown in FIGS. 5B and 5C, the discharge port 33a is separated from the inner wall surface 32a. If so, it is not necessary to provide a parallel portion in the insertion portion 33b.

[0053] Even in such a case, reactant F _B discharged at a distance from the inner wall surface 32a, so that flow parallel to the inner wall surface 32a so as to be drawn into the reactant F _A reactant F _B is a state of being contained in the reaction substrate F _a,
Reactant fluid F _A, it is possible to spaced from the inner wall surface 32a of the interface F _B, the same effect as the above embodiment can be obtained.

[0054] In FIG. 5 (b), the ejection surface 33a of the inner tube 33 is formed in parallel to the flow direction of the reactant F _A,
Figure 5 (c), the ejection surface 33a is formed to be inclined relative to the direction of flow of the reaction substrate F _A. In the aforementioned embodiment, as shown in FIG. 2 (a) ~ (c) , the main passage R _A, although a configuration in which a single inlet path R _B,
If the outer tube wall surface 32a and the discharge port of the introducing flow channel constituting a main channel and spaced apart from each other both, may also be merged multiple introduction channel into the main channel R _A, for example, FIG. 6 (a ),
As shown in (b), the inner tube 33A, 3
Multiple tubes 3B are arranged coaxially may be inserted (double tube in this case), in this case, is the fluid fluid (fluid F ₂ in this case) containing therein the (fluid F ₁ in this case) ,
Further, it is included in another fluid (here, the fluid F ₃ ). Unlikely that products of solid or highly viscous liquid adheres against the discharge port of the inner tube 33B, but using a fluid which reacts to each other and the fluid F ₃ of the innermost of the fluid F ₁ and outermost by suitable amount supplying an inert fluid in the reaction of the fluid F _1, F ₃ as a fluid F ₂ flowing between these fluids F _1, F _3, substantially completely suppress the adhesion of the product to such a discharge port wall it can.

The supply amount of the inert fluid F ₂ is as follows.
It can suppress the adhesion of the product to the discharge port wall surface of the inner tube 33B, and is set so as not to inhibit the reaction of the fluid F _1, F _3. 6A and 6B, the inner pipe 33A,
Although the distal end of 33B is a parallel portion parallel to the outer tube inner wall surface 32a, a configuration without such a parallel portion is also possible.

[0056] Alternatively, as shown in FIG. 7 (a) ~ (c), in the outer tube 32, both the inner pipe 33C so as to be parallel to the outer tube wall surface 32a, may be inserted side by side 33D ( each inlet flow path R _D, may also be) and on-site so as to be parallel to the inner wall surface 32a of the R _E, as shown in FIG. 7 (d), in the outer tube 32, both the outer tube wall surface 32a it may be inserted side by side inner pipe 33C~33F in parallel (or may be arranged so as to be parallel to each introduction channel R _C to R _F the inner wall surface 32a).

FIGS. 6 (a) and 6 (b) and FIGS.
(D), the the case of merging the plurality of introduction passages into the main channel R _A from these introduction channel R _A, respectively, a fluid containing the fluid containing the reaction substrate, the reaction agent, It is possible to supply a fluid irrelevant to the reaction or a reactant or the like that deactivates the reaction substrate, but the types of fluids (second reaction fluids) supplied from these introduction channels are different from each other. The same type or different types may be used. For example, in the flow-type micro reaction channel shown in FIG. 7A, the same type of fluid (here, fluid F _B ) is supplied from pipes 33C and 33D, while the flow shown in FIGS. 7B and 7C. the type fine reaction flow channel, pipe 34C, different types of fluids F _B from _34D, the F _C are supplied. Alternatively, as the flow-type fine reaction flow channel shown in FIG. 7 (d), the pipe 34C, respectively supplying the fluid F _B from 34E, the pipe 33D, may be respectively supplying fluid F _C from 33F.

Further, the discharge ports 34C-a to 34C-3
4F-a, as shown in FIG. 7 (a), (b), it may be installed in the same position relative to the flow path direction (d), the 7
They may be set at different positions as shown in FIG. In addition, in the flow-type minute reaction channel shown in FIGS. 7A to 7D, all or a part of each introduction channel is further replaced with the one shown in FIG.
It is also possible to form a multiple tube as shown in FIGS. In this case, the outermost tube side of each of the multiple tubes [FIG.
6 (a) and 6 (b), a fluid F ₃ ] is supplied to a reaction fluid supplied from each inner tube [FIGS. 6 (a) and 6 (b), a fluid F ₁ ,
F ₂ ] by making the fluid inert to the reaction
Fluids F ₂ , F ₃ are applied to multiple tubes or single tubes adjacent to each other.
That product adheres contact can be greatly reduced.

As described above, by combining a plurality of introduction paths into one main flow path, a plurality of different reactions can be simultaneously or continuously performed in one reaction flow path. Also, the number of such reactions is not limited. However, since the main flow path is also a minute flow path, the number of inner pipes (introduction paths) that can be arranged in the outer pipe 32 (main flow path R _A ) is about 1 to 5, preferably 1 to 3.
It is a book.

FIGS. 6A and 6B and FIG. 7A
When a plurality of introduction flow paths are merged into the main flow path as shown in (d), it is only necessary that both the wall surface constituting the main flow path and the discharge port of each introduction flow path are separated, and the main flow path is formed. Each of the distances L _{1 to} L ₁₄ between the wall surface and the discharge ports of each of the introduction flow paths may be the same or different, and is generally 10 μm or more, preferably 50 μm or more, and particularly preferably. It is at least 100 μm, most preferably at least 500 μm.

Further, in the above-described embodiments and modified examples, the example in which the main flow path and the introduction path are each configured as a flow path having a circular cross section by using a circular pipe has been described. is not limited to a circle, for example, FIG. 8
It may be rectangular as shown in (a) and (b). FIG.
(A), the reaction flow path, square tubes forming the main passage R _A 3
In FIG. 8 (b), the reaction flow path forms the introduction flow paths R _B and R _C in a double tube configuration in which the tip of the square pipe 33G forming the introduction flow path R _B is inserted into 2A. Square tube 33G, 33H
Is formed in a triple tube configuration coaxially inserted into the square tube 32A.

[0062] In addition, it may not be similar to the introduction path of the cross-sectional shape as the sectional shape of the main flow channel, for example, the flow path cross-sectional shape of the main flow passage R _A rectangular, the flow path cross-sectional shape of the introduction path R _B circular The configuration may be as follows. When a plurality of introduction paths are joined to the main flow path, the cross-sectional shapes of these introduction paths may be different from each other. Further, in the above embodiments and modifications described above, although an example of forming the main passage R _A and introduction channel R _B with a tube, as shown in FIG. 9, by providing a groove in the substrate 50 it may constitute the main passage R _a and introduction channel R _B. In this case, so as to extend the introduction channel R _B, main channel insertion portion 51 of the R _A introduction flow path into the R _B is formed, the tip of the discharge port 51a of the insertion portion 51, a main passage R _A It is formed apart from the wall surface 50a to be formed.

Further, in the above-described embodiment, the reactor is constituted by using one reaction channel assembly 3 in which a plurality of reaction channels 31 are integrally formed. For example, as shown in FIG. a plurality of reaction channels assembly 3 in the thickness direction may be formed (here, five are) reactor 3 by stacking '. In this case, the reactant F
Pipe P _A for _A, the reactor 3 'is branched outside of which is connected to the reaction channel assembly 3, similarly, the pipe P _B for reactant F _B, the reactor 3' branches outside the Each reaction channel assembly 3
It is connected to the.

[0064] Also, the pipe P _G for the fluid F _G is branched by the reaction channel assembly 3 connection port 3C [refer to FIG. 2 (a)]
It is connected to the. Also, the pipe P for the heating medium F _H
The _H, in upstream / downstream of the reactor 3 ', the branch / by set, and so as to circulate the heating medium F _H on each reaction channel assembly 3. Alternatively, the reactor may be configured by providing a plurality of (here, six) reaction channels 31 around one reaction channel 31 as shown in FIG.

When the reaction channel 31 having a rectangular channel cross section as shown in FIGS. 8A and 8B is used, for example, the reactor 3 'in FIG. May be configured as shown in FIG. The reactor is configured such that a reaction channel 31 and a heat medium channel 35 having substantially the same size and shape as the reaction channel 31 are alternately arranged vertically and horizontally.

When a plurality of reaction channels 31 are integrally formed as described above, it is possible to cause different synthesis reactions to be performed in the respective reaction channels 31. Further, as described above, the flow-type micro reaction channel, the reaction apparatus, and the reaction method of the present invention have excellent effects in preventing / blocking and improving the reaction rate in mixing / reaction of a reaction fluid under a laminar flow state. what it is intended capable of exhibiting, which is not limited to the mixing / reaction under laminar flow conditions may be used in the mixing / reaction of the reaction fluid in a state where turbulent flow conditions or turbulent flow and laminar flow mingling It is.

[0067]

EXAMPLES (A) Example A reaction apparatus as an example of the present invention is a Benzaldehyde / THF
And MeMgBr / THF.
As shown in (a) and (b), 0.9 mol / l (mole / liter) of a benzaldehyde THF solution (Benzal
dehyde / THF), dry THF (THF) and 0.9 mol /
TH of 1 (mol / liter) methylmagnesium bromide
Syringe pumps (reaction fluid driving devices) 2A, 2B, 2C for supplying the F solution (MeMgBr / THF), a circular pipe 32 forming a main flow path, and a circular pipe 33 forming an introduction path
And a flow-type micro reaction channel 31 having A and 33B. The THF is Benzaldehyde / THF and M
It is inert to the reaction with eMgBr / THF, and is for preventing the product generated by such reaction from adhering to the circular tube 33B.

[0068] ¥ tube 32 has one end connected to the syringe pump 2A, NH ₄ C by the other end syringe pump 2D
l _aq. is supplied and the downstream side is configured as an acid treatment line 60, and the circular tube 33A is connected to one end side (insertion portion) 3
3A-b is inserted parallel to the circular tube 32, the other end is connected to the syringe pump 2B, and the circular tube 33B has one end (insertion portion) 33B-b inserted parallel to the circular tube 33A,
The other end is connected to the syringe pump 2C. And
The inner wall surface 32a and the circular tube 33A of the circular tube 32, 33B of the discharge port 33A-a, both 33B-a are spaced apart from each other.

Each of the circular tubes 32, 33A and 33B is made of stainless steel. The circular tube 32 has an inner diameter of 4 mm and an outer diameter of 6 mm, the circular tube 33A has an inner diameter of 2 mm and an outer diameter of 3 mm, and the circular tube 33B has an inner diameter of 0.6 mm. The diameter is 1.6 mm. In addition, circular pipe 32,
33A, the length of the reaction region R _R between the merging portion of 33B and NH ₄ Cl _aq. Injection unit 2m, length of NH ₄ Cl _aq injection portion downstream of the acid treatment line 60 is set to 1m I have.

By operating the syringe pumps 2A to 2D,
Benzaldehyde / THF, THF, MeMgBr / THF and NH ₄ Cl _aq.
At a flow rate of 0.1 to 1.0 ml (milliliter) /
When the mixture was supplied to the reaction channel 31 for 30 minutes and reacted for 30 minutes, no blockage was observed in the reaction channel 31. (B) Comparative Example FIGS. 13 (a) and 13 (b) show a conventional reactor having the T-shaped flow-type minute reaction channel 103, and the reactor 1 shown in FIG.
03, and the circular pipe 101A for Benzaldehyde / THF, MeMgBr
It has a circular tube 101B for / THF and a reaction tube 102 on the downstream side of the junction of the circular tubes 101A and 101B. The reaction tube 102, FIG. 12 (a), the a carried out as in the reaction tube 32 according to the embodiment, an inner diameter of 4 mm, an outer diameter of 6mm stainless steel of the present invention shown in (b). FIG.
The same components as those of the reactors of (a) and (b) are denoted by the same reference numerals, and description thereof is omitted.

With this configuration, the syringe pump 2
A, 2C, actuates the 2D, Benzaldehyde / THF, MeM
gBr / THF and NH ₄ Cl _aq .
When the reaction flow was supplied to the reaction channel 103 at 0 ml (milliliter) / min (that is, when the reaction was performed under the same conditions as in the above-described embodiment of the present invention), the reaction channel 103 was closed approximately 10 days after the start of the reaction. I have. (C) Conclusion Accordingly, it was demonstrated that the flow-type microreaction channel, the reaction apparatus, and the reaction method of the present invention can stably perform the synthesis reaction as compared with the related art.

[0072]

As described in detail above, according to the present invention,
Since the second reaction fluid can be joined to the first reaction fluid flowing through the main flow channel from the introduction flow channel so as not to come into contact with a wall surface forming the main flow channel, the second reaction fluid can be mixed with the first reaction fluid. will be completely included in the reaction fluid, can separate the interface between the reaction fluid, the wall forming the main flow path,
This can prevent the solid or high-viscosity liquid generated by the reaction of the reaction fluid and the reaction fluid mixture in the course of the reaction from simultaneously contacting and adhering to the wall surface, thereby suppressing blockage of the main flow path. There is an advantage that you can.

Further, since the second reaction fluid is completely contained in the first reaction fluid, the interface between these reaction fluids, that is, the reaction fluid, is smaller than that in the case where the conventional minute reaction passage is used under the same conditions. There is an advantage that the contact surface can be increased, and the reaction speed can be improved.

[Brief description of the drawings]

FIG. 1 is a schematic perspective view showing the entire configuration of a reaction apparatus as one embodiment of the present invention.

FIG. 2 is a view showing a reaction apparatus as one embodiment of the present invention, in which (a) shows a reactor (reaction channel assembly) thereof;
FIG. 1B is a schematic perspective view showing the overall configuration of FIG. 1B, and FIG.
(C) is a schematic enlarged perspective view showing a main configuration of a flow-type fine reaction flow channel.

FIG. 3 is an enlarged schematic cross-sectional view showing a configuration of a flow-type micro reaction channel as one embodiment of the present invention.

FIG. 4 is a schematic perspective view showing a configuration of a modified example of the reactor as one embodiment of the present invention.

5 (a) to 5 (c) are schematic longitudinal sectional views showing, on an enlarged scale, main components of a modified example of a flow-type micro reaction channel as one embodiment of the present invention.

[Figure 6] is a diagram showing a modification of the flow-type fine reaction flow channel according to an embodiment of the present invention, (a) is a schematic perspective view showing the enlarged main portion thereof configured, (b) is is a schematic longitudinal sectional view showing an enlarged main portion thereof configured.

7 (a) ~ (d) is a schematic enlarged perspective view showing a main configuration of a modification of the flow-type fine reaction flow channel according to an embodiment of the present invention.

8 (a), it is a schematic perspective view showing an enlarged main portion configuration of a modification of the flow-type fine reaction flow channel according to an embodiment of the (b) the present invention.

FIGS. 9 (a) and 9 (b) are schematic perspective views showing, on an enlarged scale, main parts of a modification of the flow-type micro reaction channel as one embodiment of the present invention.

FIG. 10 is a schematic perspective view showing an enlarged main part configuration of a modified example of the reactor (reaction channel assembly) according to one embodiment of the present invention.

11 is a schematic perspective view showing the overall configuration of a modification of the reactor according to an embodiment (reaction channel assembly) of the present invention.

FIGS. 12A and 12B are diagrams showing a reaction apparatus and a flow-type minute reaction channel according to an embodiment of the present invention, wherein FIG. 12A is a schematic system diagram of a reaction fluid line, and FIG. FIG. 2 is a schematic cross-sectional view showing a configuration of a main part of a reaction channel.

[Figure 13] is a diagram showing a conventional reactor and the flow type micro-channel as a comparative example for an embodiment of the present invention, (a) is a schematic diagram of the reaction fluid line,
(B) is a schematic cross-sectional view showing a configuration of a main part of the flow-type micro reaction channel.

[14] (a), it is a schematic diagram showing the structure of (b) the distribution-type reactor using a conventional fine channel.

FIGS. 15A and 15B are schematic diagrams showing a configuration of a merging section of a flow-type reaction apparatus using a conventional microchannel.

FIG. 16 is a schematic arrow view showing a configuration of a junction of a flow-type reaction apparatus using a conventional microchannel.

[Explanation of symbols]

1A~1D tanks 2A, 2B, 2C pump (reaction fluid circulating device) 2D, 2H pump 3,3 'reactor 4 purifier 5 heat exchanger 30 casing 31 reaction channels (flow type micro-channel) 32, 33, 33A to 33H Pipes 32a, 50a Inner wall of outer tube (wall surface forming main flow path) 33a, 51a Discharge port 33b, 51 Discharge section 33d Parallel portion 35 Pipe for temperature adjustment 50 Substrate 60 Acid treatment lines P _A , P _B , P _G , P _H pipes R _A main flow path R _B introduction flow path R _R reaction flow path (reaction area) F _A reaction substrate (first reaction fluid) F _B , F _C reactant (second reaction fluid) F _S target substance F _D residual substance F _H Heat medium (fluid for temperature control)

──────────────────────────────────────────────────続 き Continued on the front page (51) Int.Cl. ⁷ Identification symbol FI Theme coat ゛ (Reference) C07C 33/22 C07C 33/22 F term (Reference) 4G075 AA01 AA52 AA63 BA06 BB02 BB03 BB07 BD15 BD22 CA02 CA03 DA02 DA12 EB21 EB27 EC01 EC03 FA12 4H006 AA02 AC22 AC41 BB15 BD81 FC52 FE11

Claims (14)

[Claims] A first reaction fluid flowing through the main flow path, comprising: a main flow path having a minute flow path cross-sectional area; and one or more introduction flow paths merging with the main flow path. A flow-type micro-reaction channel for merging / reacting with a second reaction fluid flowing through the insertion channel, wherein the one or more introduction channels are extended to form an insertion portion formed in the main channel. A flow-type minute reaction channel, wherein each discharge port at the tip and a wall surface forming the main channel are separated from each other. Wherein, wherein the equivalent diameter of the cross section of the main flow passage is less than 1cm, flow-type fine reaction flow channel according to claim 1, wherein. 3. The insertion portion has a parallel portion on the distal end side that is parallel to a wall surface forming the main flow path, and the insertion portion has the same direction as the flow direction of the first reaction fluid from the discharge port. the second reaction fluid, characterized in that it is configured to discharge, according to claim 1 or 2 flow type micro-channel according to. 4. The flow-type microscopic device according to claim 3, wherein a distance between each of the distal end of each of the insertion portions and a wall surface forming the main flow path is set to 500 μm or more. reaction channel. 5. The flow-type minute reaction channel according to claim 3, wherein the length of the parallel portion is longer than 100 times the equivalent diameter of the cross section of the introduction channel. 6. An equivalent diameter of a cross section of the introduction flow path is 500 μm.
The flow-type minute reaction channel according to any one of claims 1 to 5, wherein the diameter is from m to 1 mm. 7. The flow-type micro reaction channel according to claim 1, wherein a cross section of the introduction channel is circular. 8. The flow-type micro reaction channel according to claim 1, wherein a cross section of the introduction channel is rectangular. 9. The method according to claim 1, wherein the number of said introduction flow paths merging with said main flow path is in a range of 1 to 3.
A flow-type micro reaction channel according to any one of the preceding claims. With equipped 1 or more flow-through micro-channel according to 10. any one of claims 1 to 9, in each of the main channel and the introduction flow path of the flow through type fine reaction flow channel A reaction device comprising a reaction fluid drive device for flowing a reaction fluid to the reaction device. 11. A flow channel assembly formed by integrating a plurality of the flow-type minute reaction channels juxtaposed side by side, and stacking a plurality of the reaction channel assemblies. the reaction apparatus according to claim 10. 12. A temperature control channel for flowing a temperature control fluid is provided adjacent to the flow-type microreaction channel in order to adjust the temperature of the reaction fluid in the flow-type microreaction channel. The reactor according to claim 10 or 11, wherein the reaction is performed. 13. The flow-type minute reaction channel has 100 to 3 flow channels.
Equipped range pieces of 000 and wherein the being,
The reactor according to any one of claims 10 to 12. 14. A first reaction fluid flowing through a main flow path having a small flow path cross-sectional area is joined with a second reaction fluid from an introduction flow path so as not to contact a wall forming the main flow path. A reaction method, characterized in that: