Flow reactor

Abstract

Provided is a flow reactor that can perform a reaction under appropriate temperature management, can inhibit a reaction fluid and generated gas from being trapped in a heat transfer portion, can be disassembled, has good cleanability, and can perform coating and lining work. The flow reactor is provided with a reaction fluid flow path (11) and a second flow path (21) in a space formed between a concentric inner cylinder (10) and an outer cylinder (20). A spiral heat transfer body (41) is disposed between the inner cylinder (10) and the outer cylinder (20), and the spiral heat transfer body (41) has a substantially triangular cross-sectional shape in an axial cross-sectional view. The space is divided by the spiral heat transfer body (41) into the reaction fluid flow path (11) and the second flow path (21), and heat exchange is performed between a reaction fluid (F1) flowing through the reaction fluid flow path (11) and a heat medium (F2) flowing through the second flow path (21) via the spiral heat transfer body (41).

Description

TECHNICAL FIELD

[0001] The present application relates to a flow reactor, and particularly to a flow reactor having a spiral flow path for flowing a reaction fluid. BACKGROUND

[0002] In the processes of chemical and pharmaceutical manufacturing, toner, inkjet, and the like, quenching, high-speed heating, or precise temperature control are often required. In addition, it is required to reduce the necessary installation space as much as possible, and the size of the equipment itself is also miniaturized, and high performance of the heat exchanger is required. Furthermore, a flow reactor with less adhesion, excellent cleaning properties, pressure resistance, corrosion resistance, and low cost is required.

[0003] Conventionally, as disclosed in Patent Document 1, a shell-and-tube reactor having a plurality of stages is known. The reactor has at least two types of regions, both of which contribute to removing heat from or supplying heat to the system according to the requirements of the system. The reactor has a group of reaction regions, which have a catalyst for promoting a reaction, and also have a tube for removing or supplying heat.

[0004] However, in any of the descriptions in Patent Document 1, in the case of adhesion or the like occurring in the tube, it is difficult to clean, and it is not possible to simply confirm whether cleaning or the like has been performed, or the cleaning state.

[0005] In addition, the amount of heat medium on the shell side is large, and overshoot and undershoot are easily generated. It is basically a classical heat exchanger, so it is difficult to increase the overall heat transfer coefficient dramatically. Furthermore, since the tube is mounted on the tube sheet, it is difficult to use in a reaction that repeatedly expands and contracts due to heat. In addition, it is virtually impossible to perform coating or lining inside the thin tubular heat transfer tube, and it is also difficult to perform coating or lining of corrosion-resistant materials in other flow paths in terms of its structure, and improvement is desired in terms of corrosion resistance and the like. In particular, it is virtually impossible to coat or line the inside of the heat transfer tube with a corrosion-resistant material, and even if it is possible, it cannot be avoided that the mass productivity is poor and it is not practical in terms of cost.

[0006] In Patent Literature 2, there is described a microreactor in which a plurality of supply paths are merged into one reaction flow path, and the reaction is performed while the fluids are circulated, characterized in that the reaction flow path is formed into a spiral flow path by fitting the outer peripheral surface of a core member on a round bar and the inner peripheral surface of an outer cylinder member having a circular cross section into close contact by cutting a spiral thread in either one of the outer peripheral surface of the core member and the inner peripheral surface of the outer cylinder member. However, the heat transfer area is too small, and the thread-like wall surface which is difficult to cut cannot be directly used as a heat exchange surface, and there is no view of increasing the total heat transfer coefficient as much as possible by reducing the heat transfer resistance necessary for the flow reactor. In addition, it is a microreactor which is exclusively used for a micro reaction, and is not designed as a device for performing upsizing. It is difficult to scale up, but even if it is directly upsized, there are many problems such as decomposability or cleanability, and it is difficult to achieve precise temperature control.

[0007] In Patent Literature 3, there is described a tubular flow module having at least two concentric tubes with a spiral feature, in which an inner tube is coaxially arranged inside an outer tube, the maximum diameter of the inner tube is larger than the minimum diameter of the outer tube, and the space between the inner tube and the outer tube becomes a flow path of the fluid. The outer tube and the inner tube with a spiral feature are engaged like a screw and a nut, and since the spiral feature functions like a thread, they are a tubular flow module with a thread fit. The average flow direction of the tubular flow module is the axial direction, and an improved plug flow condition is generated (see Patent Literature 00018). Therefore, the tubular flow module of Patent Literature 3 cannot achieve counterflow flow of spiral flow, and like Patent Literature 2, it cannot be oriented to upsizing, and precise temperature control is difficult.

[0008] Prior Art Documents

[0009] Patent Literature

[0010] Patent Literature 1: Japanese Patent Application Laid-Open No. 2012-529626

[0011] Patent Literature 2: Japanese Patent Application Laid-Open No. 2005-46652

[0012] Patent Literature 3: Japanese Patent Application Laid-Open No. 2015-502842 SUMMARY

[0013] PROBLEMS TO BE SOLVED BY THE INVENTION

[0014] In view of the above circumstances, an object of the present application is to provide a flow reactor in which reaction processing of a reaction fluid can be performed under appropriate temperature management, that is, in a state in which the temperature of the reaction fluid is controlled.

[0015] Another object of the present application is to provide a flow reactor in which promotion of a reaction can be achieved to shorten the reaction time.

[0016] Another object of the present application is to provide a flow reactor having a configuration suitable for inhibiting the reaction fluid, gas generated in the heat transfer portion from being stagnant.

[0017] Another object of the present application is to provide a flow reactor having good cleaning properties.

[0018] Another object of the present application is to provide a flow reactor capable of being disassembled.

[0019] In addition, an object of the present application is to provide a flow reactor that also enables the construction of a coating or a liner.

[0020] Means for solving the problem

[0021] The flow reactor of the present application, which has a reaction fluid flow path for flowing a reaction fluid, is characterized in that a heat transfer body is disposed in a space formed between a concentric inner cylinder and an outer cylinder, the heat transfer body is spirally wound, and in an axial cross-sectional view, the cross-sectional shape is substantially triangular, the space is divided by the heat transfer body into the reaction fluid flow path and a second flow path, and heat exchange is performed between the reaction fluid flowing in the reaction fluid flow path and a heat medium flowing in the second flow path via the heat transfer body.

[0022] The flow reactor of the present application, which has a reaction fluid flow path for flowing a reaction fluid, is characterized in that a heat transfer body is disposed in a space formed between a concentric inner cylinder and an outer cylinder, the heat transfer body is spirally wound, and in an axial cross-sectional view, the cross-sectional shape is substantially triangular, the space is divided by the heat transfer body into the reaction fluid flow path and a second flow path, and heat exchange is performed between the reaction fluid flowing in the reaction fluid flow path and a heat medium flowing in the second flow path via the heat transfer body.

[0023] It is more appropriate that at least either one of the inner cylinder and the outer cylinder is a cylindrical body that is circular in an axial cross-sectional view. Thereby, a convection flow of a spiral flow can be generated in the reaction fluid flowing through the reaction fluid flow path defined by the heat transfer body and the inner cylinder or the outer cylinder, which has a substantially triangular cross-sectional shape.

[0024] Further, it is also preferable that the ratio (λ / μ) of the maximum flow path width (λ) of the counter flow path in the radial direction to the minimum flow path width (μ) of the counter flow path be 2 or more (2 < λ / μ < ∞). Thus, compared to the flow in the axial direction toward the inner cylinder or the outer cylinder, the flow in the helical direction can be made large, and the direction of the flow of the entire counter flow fluid can be made the helical direction.

[0025] Further, the present application can be implemented as a structure in which the heat transfer body is fixed to either one of the side on which the outer cylinder is located and the side on which the inner cylinder is located, is not fixed to the other one of the side on which the outer cylinder is located and the side on which the inner cylinder is located, and has a three-dimensional shape portion having at least one bent portion and capable of forming a space in which fluid can flow on both the inner side and the outer side thereof, the outer angle of all the bent portions present on the flow path constituting surface of the counter flow path being 90 degrees or more.

[0026] Further, the present application can be implemented as a structure in which the counter flow path does not have a horizontal portion in which the counter flow fluid is likely to be stored.

[0027] Further, the present application can be implemented as a structure in which the counter flow path and the second flow path are each spirally wound, and a gap is not present between the adjacent winding portions in the axial direction or a gap of 4 mm or less is present in the radial direction.

[0028] Further, the present application can be implemented as a structure in which the counter flow path and the second flow path are each a substantially triangular shape in cross section in an axial cross-sectional view, the apex angle θ being 30 degrees or more and 125 degrees or less.

[0029] Further, the present application can be implemented as a structure in which the side on which the inner cylinder is located and the side on which the outer cylinder is located are assembled so as to be separable by movement in the axial direction without rotation, and the heat transfer body does not interfere with other portions when moved in the axial direction.

[0030] Further, the present application can be implemented as a structure in which the counter flow path and the second flow path are each a substantially triangular shape in cross section in an axial cross-sectional view, the apex portion having an axial length (a) shorter than the axial length (b) of the inclined surface.

[0031] Further, the present application can be implemented as a structure in which the apex portion of at least either one of the counter flow path and the second flow path has a length (a) in the axial direction, and the cross-sectional area of the flow path is larger compared to the case where the apex portion has no length (a) in the axial direction.

[0032] Further, the present application can be implemented as a structure in which the space formed between the inner cylinder and the outer cylinder in the concentric arrangement has a plurality of the space in a concentric manner.

[0033] Further, the present application can be implemented as a structure in which at least either one of a flow path through which the reaction-use fluid flows including the reaction-use flow path and a flow path through which a heat medium flows including the second flow path is implemented with a coating layer using a corrosion-resistant material, and preferably, the coating layer using the corrosion-resistant material is one of a glass lining or a fluororesin coating layer, a ceramic coating layer.

[0034] Effects of the Invention

[0035] The present application can provide a flow reactor in which a reaction process of a reaction-use fluid can be performed under appropriate temperature management, i.e., in a state in which the temperature of the reaction-use fluid is controlled.

[0036] The present application can provide a flow reactor in which a reaction can be promoted and a reaction time can be shortened.

[0037] The present application can provide a flow reactor having a configuration suitable for suppressing the reaction-use fluid, generated gas from being trapped in a heat transfer portion.

[0038] The present application can provide a flow reactor having good cleaning properties.

[0039] The present application can provide a flow reactor having a configuration that is easy to disassemble.

[0040] The present application can provide a flow reactor in which the application of a coating layer or a lining can also be performed.

[0041] More specifically, in a process of chemical and pharmaceutical manufacturing, a reaction process of toner, inkjet, and the like, quenching, high-speed heating, or precise temperature control, and the like are often required. The reaction-use fluid, which is the object, is a high-viscosity liquid, a suspension containing fine particles, and also often contains adhering substances. Further, in the reaction process, when heating operation is performed with evaporation, if gas trapping occurs, the heat transfer rate decreases to a low order of magnitude that is the same as that of a single-phase flow of the generated gas. This phenomenon is called dry-out, and is caused by the evaporation of a liquid film flowing along a heat transfer surface, and thus the direct contact of a gas phase with the heat transfer surface. Further, the flow reactor needs to be reliably scaled up, and high performance is needless to say, and even if it is upsized, it must be processed in accordance with the calculation.

[0042] To solve these problems, a flow reactor having a configuration in which even if the relationship between the flow rate of the reaction-use fluid and the pressure loss is re-studied, the flow rate of the reaction-use fluid is increased, and the pressure loss is not excessively large is provided. In particular, in the case where the reaction-use fluid is a high-viscosity liquid or a suspension that easily settles, the effect is large, and dirt or adhesion is less.

[0043] In addition, by making the cross-sectional shape of the heat transfer surface substantially triangular, the accumulation of liquid and the generation of gas can be eliminated, and the heat transfer area can be increased. From the physical properties of the reaction fluid, the cross-sectional shape of the heat transfer body is selected to be substantially triangular, and there is also a degree of freedom in design.

[0044] In addition, the amount of the reaction fluid is also small, and it is easy to respond to rapid heating or rapid cooling. At the same time, the amount of the heat medium or the refrigerant is also small, and thus the device can be miniaturized, high performance, and easy to control.

[0045] In addition, the place where the reaction fluid flows can be freely determined to be turbulent flow or laminar flow by controlling the amount of delivery. The flow path of the heat medium or the refrigerant is turbulent flow, and the Reynolds number is greatly increased, and thus the reaction speed can be significantly improved by increasing the total heat transfer coefficient.

[0046] In the present configuration, since it is very simple, it is easy to disassemble or assemble, and it can also be coated or lined with a corrosion-resistant material. BRIEF DESCRIPTION OF DRAWINGS

[0047] Figure 1 is an axial sectional view of a flow reactor of the first embodiment of the present application.

[0048] Figure 2 is an enlarged sectional view of a main part in a state where the inner cylinder and the outer cylinder are separated.

[0049] Figure 3 is an axial sectional view of a flow reactor of the second embodiment of the present application.

[0050] Figure 4 (A) to (F) are axial sectional views of a main part of a flow reactor of the embodiments of the present application, respectively. DETAILED DESCRIPTION

[0051] Hereinafter, the flow reactor of the embodiments of the present application will be described with reference to the drawings. In addition, Figure 2 , Figure 4 The center line described in (A) to (F) indicates the axial direction.

[0052] (Fluid)

[0053] In the embodiment, a fluid containing a substance that is a processing target of the reaction is described as the reaction fluid F1. In the case where the reaction fluid F1 is composed of two fluids, for example, each fluid is described as the reaction fluid F1(A) and the reaction fluid F1(B), and in the case where the two fluids are combined, the fluid after the combination is described as the reaction fluid F1. Hereinafter, the reaction fluid F1 refers to a fluid composed of one fluid, or in the case where two or more fluids are composed, the fluid after the combination of the two or more fluids. In addition, a heat medium that exchanges heat with respect to the reaction fluid F1 is described as the second fluid F2. In addition, another heat medium that exchanges heat with the reaction fluid F1 is described as the third fluid F3.

[0054] As the reaction fluid F1, various fluids such as a gas, a liquid, a suspension, a highly viscous liquid, and the like can be exemplified. In the second fluid F2 and the third fluid F3, a heat medium for heating such as water vapor, hot water, and the like can be exemplified, but a heat medium for cooling can also be used.

[0055] (Summary of the First Embodiment)

[0056] Figure 1 The flow reactor of the illustrated first embodiment is provided with an inner cylinder 10 and an outer cylinder 20 that are concentrically arranged, and as needed, a third cylinder 30 that is concentrically arranged on the inner side of the inner cylinder 10.

[0057] A heat transfer body 41 that is arranged in a spiral shape is arranged on the inner peripheral surface of the outer cylinder 20.

[0058] The space between the inner cylinder 10 and the outer cylinder 20 is divided into two spaces by the heat transfer body 41. The inner side (radial inner side) of the heat transfer body 41 in the two divided spaces constitutes a reaction flow path 11 that is a flow path of the reaction fluid F1, and the outer side (radial outer side) of the heat transfer body 41 in the two divided spaces constitutes a second flow path 21 that is a flow path of the second fluid F2.

[0059] The heat transfer body 41 is fixed to the inner peripheral surface of the outer cylinder 20 in a state of maintaining air tightness and liquid tightness by welding or the like, thereby dividing the space between the inner cylinder 10 and the outer cylinder 20 into the reaction flow path 11 and the second flow path 21 so that the reaction fluid F1 and the second fluid F2 do not mix, and the reaction flow path 11 and the second flow path 21 become flow paths that are arranged in a spiral shape. Heat exchange is performed between the reaction fluid F1 and the second fluid F2 via the heat transfer body 41.

[0060] The inner cylinder 10 and the outer cylinder 20 are assembled in a separable manner, as shown in Figure 2As shown, in the separated state, the heat transfer element 41 and the outer cylinder 20 are separated from the inner cylinder 10. In this separated state, the flow path of the reaction flow path 11 is defined as being separated into the inner cylinder 10 side and the outer cylinder 20 side.

[0061] In this example, the space between the inner cylinder 10 and the third cylinder 30 forms a third flow path 31 for the third fluid F3, through which heat exchange occurs between the reaction fluid F1 and the third fluid F3. Furthermore, since the flow path body 42 is fixed to the outer circumferential surface of the third cylinder 30 in a spiral shape, the third flow path 31 also becomes a spirally surrounding flow path.

[0062] (Fixing and separating the cylinder)

[0063] The inner cylinder 10, outer cylinder 20, and third cylinder 30 are fixed at the flange 40 at the upper end of the cylinders in a separable manner. In this example, the two flanges 40 overlap and sandwich the sealing member, and are assembled separately using a detachable fixing member (not shown) such as bolts, thus becoming a single unit. The upper ends of the inner cylinder 10 and the third cylinder 30 (detachable as needed) are fixed to the upper flange 40, and the upper end of the outer cylinder 20 (detachable as needed) is fixed to the lower flange 40. By separating the upper and lower flanges 40, the inner cylinder 10 and the outer cylinder 20 can be separated. Alternatively, the inner cylinder 10 and the third cylinder 30 can also be separated by making at least one of them detachable from the upper flange 40.

[0064] As described above, the heat transfer element 41 is fixed to the inner circumferential surface of the outer cylinder 20 by welding or the like. Therefore, when the heat exchanger is disassembled by detaching the flange portion 40, the heat exchanger is separated into the outer cylinder 20 with the heat transfer element 41 fixed to its inner circumferential surface, the inner cylinder 10, and the third cylinder 30 with the flow path 42 on its outer circumferential surface. At this time, since there is no object interfering with the heat transfer element 41, the outer cylinder 20 with the heat transfer element 41 and the lower flange portion 40 can be pulled downwards as shown in the figure.

[0065] (Regarding heat transfer element 41)

[0066] The heat transfer element 41 travels axially between the inner cylinder 10 and the outer cylinder 20 in a spiral shape. Figure 1 and Figure 2 As shown, in the axial sectional view, the cross-sectional shape is approximately triangular. In this embodiment, the heat transfer element 41 is fixed to the inner circumferential surface of the outer cylinder 20 by welding or the like.

[0067] Regarding the apex angle θ of the approximate triangle in the axial cross-sectional view of the heat transfer body 41, as the apex angle θ increases, the cross-sectional area (flow path area) of the reaction flow path 11 and the second flow path 21 increases, but the number of rotations of the spiral per unit axial length of the inner cylinder 10 and the outer cylinder 20 decreases. Furthermore, as the apex angle θ moves away from 90 degrees, the narrower portions of the reaction flow path 11 and the second flow path 21 increase, thus increasing the likelihood of fluid blockage. Considering these factors, an apex angle θ of 30 degrees or more and 125 degrees or less is more appropriate.

[0068] In addition, relative to the vertex angle θ of the above approximate triangle, the exterior angle (360-θ) should be above 90 degrees, above 235 degrees and below 330 degrees.

[0069] In a mathematical sense, the two hypotenuses of a triangle intersect at the vertex. However, in industrial production contexts such as metal sheet processing, the triangle typically forms an arc at the vertex or a cross-sectional shape with length in the axial direction. Therefore, the term "approximate triangle" should be understood to encompass not only the mathematical meaning of a triangle but also the shape inherent in these industrial production processes. Thus, the vertex angle θ of an approximate triangle should be understood as representing the intersection of the two hypotenuses and the intersection of their extensions. Furthermore, in the case of a cross-sectional shape with length in the axial direction, as this axial length increases, the likelihood of the reactive fluid F1 becoming blocked between the heat transfer body 41 and the outer circumference of the inner cylinder 10 increases. Therefore, it is more appropriate for this axial length to be shorter than the axial length of one hypotenuse.

[0070] Next, since heat exchange occurs between the reaction fluid F1 and the second fluid F2 via the heat transfer body 41, the thickness t of the heat transfer body 41 is preferably 0.2 mm to 3 mm, more preferably 0.5 mm to 2 mm, considering the efficiency of heat exchange. The thicknesses of the inner cylinder 10, outer cylinder 20, and third cylinder 30 can also be the same. However, they can also be modified to improve the strength of the inner cylinder 10, outer cylinder 20, and third cylinder 30 as structural members, and are not limited thereto.

[0071] The heat transfer element 41 can also be described as being composed of a three-dimensional shape portion 43 having at least one bent portion (in addition to a straight line bent at an angle, a curved portion including an arc-shaped portion is also referred to as a bent portion). The three-dimensional shape portion 43 has the following shape: having at least one bent portion, it can form spaces (reaction flow path 11 and second flow path 21) for fluid flow on both its inner and outer surface sides. Specifically, the three-dimensional shape portion 43 is a strip-shaped body having the shape of dividing a polygonal prism or cylinder along its axial direction. In this example, the three-dimensional shape portion 43 is a strip-shaped body having the shape of dividing a quadrangular prism along its axial direction on the diagonal of a quadrilateral cross-section. The three-dimensional shape portion 43 is wound around the inner circumferential surface of the outer cylinder 20, and its upper and lower end edges 46 are fixed to the inner circumferential surface of the outer cylinder 20. It is more appropriate for the external angle θo formed by the three-dimensional shape portion 43 of the upper and lower end edges 46 and the inner circumferential surface of the outer cylinder 20 to be 90 degrees or more, and more preferably 105 ≤ θo ≤ 160. Furthermore, when the three-dimensional shape portion 43 of the end edge 46 is bent, it is the angle formed by its tangent and the inner circumferential surface of the outer cylinder 20.

[0072] In addition, the outer angle of the bent portion of the three-dimensional shape part 43 refers to the outer angle (360-θ) relative to the vertex angle θ of the above-mentioned approximate triangle and the outer angle θo formed by the three-dimensional shape part 43 of the upper and lower end edges 46 and the inner circumferential surface of the outer cylinder 20.

[0073] (Regarding the flow path 11 for the reaction)

[0074] The reaction flow path 11 is a flow path with a cross-sectional shape that is approximately triangular. It is the flow path of the reaction fluid F1, which is the main object of heat exchange, in the space between the heat transfer body 41 that spirals around the inner circumference of the outer cylinder 20 and the outer circumference of the inner cylinder 10.

[0075] The reaction flow path 11 is defined by the following parts: a bottom surface 12 formed by the outer peripheral surface of the inner cylinder 10; two inclined surfaces, a first inclined surface 13 and a second inclined surface 14; and a top 15 between the first inclined surface 13 and the second inclined surface 14. The top 15 is formed by the inner peripheral surface of the outer cylinder 20, and this part becomes the axial space between the spiral portions of the heat transfer element 41. In addition, if the heat transfer element 41 is made into a denser spiral shape in order to avoid creating this axial space, the top 15 becomes a point-like vertex with no length in the axial cross-sectional shape.

[0076] In this embodiment, the inner cylinder 10 is a circular cylindrical body in the axial sectional view, and its outer circumferential surface is a smooth, cylindrical outer circumferential surface. Similarly, in this example, the outer cylinder 20 is also a circular cylindrical body in the axial sectional view, and its inner circumferential surface is a smooth, cylindrical cylindrical surface.

[0077] If the axial length (a) of the top 15 is increased, the cross-sectional area (flow path area) of the reaction flow path 11 can be increased. However, even if it is increased, the area of ​​the heat transfer body 41, which is directly related to heat exchange, remains unchanged, so the overall heat exchange rate may decrease. Therefore, it is preferable that the axial length (a) of the top 15 is shorter than the axial length (b) of the inclined surfaces 13 and 14.

[0078] In the axial cross-sectional view, it is preferable that the first inclined surface 13 and the second inclined surface 14 are straight lines, but they can also be curved, such as bow-shaped curves. However, it is preferable that the flow paths (reaction flow path 11 and second flow path 21) have a roughly triangular cross-sectional shape, as this shape eliminates the possibility of accumulation of the processed fluids or gases, such as reaction fluid F1 and second fluid F2. Unless there is a particular purpose, it is best to avoid providing, for example, flat horizontal portions or recesses in a part of the flow path.

[0079] Furthermore, in this example, such as Figure 2 As shown, the heat transfer element 41 has a gap (μ) at its base side, which has a generally triangular cross-section forming the axial direction of the reaction flow path 11. In other words, there is a space between the end of the inner circumferential side of the first inclined surface 13 and the bottom surface 12, and there is a space between the end of the inner circumferential side of the second inclined surface 14 and the bottom surface 12. This gap (μ) can also be omitted; if it is provided, a gap (μ) of 4 mm or less is preferable. Furthermore, in other words, a gap (μ) is provided between axially adjacent surrounding portions of the spirally wound reaction flow path 11, that is, between axially adjacent generally triangular cross-sectional shapes. This gap (μ) can also be omitted; if it is provided, a gap (μ) of 4 mm or less in the radial direction is suitable.

[0080] By setting this gap (μ), the separation of the outer cylinder 20 and the inner cylinder 10 can proceed smoothly in the case of a decomposition heat exchanger. However, if the gap is too large, the reaction fluid F1 will not flow in a spiral shape, and the amount of fluid flowing through the axial short circuit will increase, which may reduce the efficiency of heat exchange.

[0081] The gap (μ) can be understood as the maximum flow path width (μ) of the reaction flow path 11 in the radial direction, and the length between the top 15 and the bottom 18 of the reaction flow path 11 defines the maximum flow path width (λ) of the reaction flow path 11 in the radial direction. Here, it is more appropriate for the ratio (λ / μ) of the maximum flow path width (λ) to the minimum flow path width (μ) of the reaction flow path 11 to be 2 or more, preferably 10 or more. In the absence of the gap μ (in other words, when the heat transfer body 41 is in contact with the inner cylinder 10), μ = 0, λ / μ = ∞.

[0082] Furthermore, the above description of the heat transfer element 41, such as the apex angle θ of the approximate triangle in the axial sectional view, also applies to the reaction flow path 11.

[0083] Assume that various fluids, such as gas, liquid, suspension, and highly viscous liquid, flow through the reaction flow path 11 as the reaction fluid F1. Depending on the type of fluid, highly viscous substances (highly viscous materials) or easily settling suspensions may adhere to the reaction flow path 11. In this embodiment, the reaction flow path 11 has an approximately triangular axial cross-section and does not have any narrow sections that would prevent passage, thus creating a structure capable of suppressing the adhesion of highly viscous substances (highly viscous materials) and easily settling suspensions.

[0084] In addition, when disassembling and cleaning, as long as the inner cylinder 10 and the outer cylinder 20 are separated, the outer circumferential surface of the inner cylinder 10 will naturally be exposed, and the entire heat transfer body 41 with an axial cross section of approximately triangular shape will also be exposed together with the inner circumferential surface of the outer cylinder 20.

[0085] In other words, the flow path 11 for the reaction is defined as the inner circumferential surface of the outer cylinder 20 and the radially inner surface of the heat transfer body 41 on the outer cylinder 20 side, and the outer circumferential surface of the inner cylinder 10 on the inner cylinder 10 side. All these surfaces are configured to be directly exposed without being obstructed by other parts when viewed from a radial direction orthogonal to the axial direction.

[0086] Therefore, it is possible to clean every corner of the reaction flow path 11, and it is also easy to confirm the state when cleaning is completed. In contrast, in the shell-and-tube reactor described in the aforementioned Patent Document 1, cleaning is difficult, and it is not easy to confirm the cleaning status.

[0087] The material of each surface along the passage of the reaction fluid F1 in the specified reaction flow path 11 can be selected from metals or the like, depending on the type of reaction fluid F1. Furthermore, it is preferable to coat its surface with a corrosion-resistant material. Examples of corrosion-resistant coatings include glass enamel, fluoropolymer coatings, and ceramic coatings. In this case, as long as the heat transfer element 41 is fixed to the inner circumferential surface of the outer cylinder 20 by welding or the like, and the same coating is applied to the outer circumferential surface of the inner cylinder 10 before inserting the inner cylinder 10 into the outer cylinder 20 for assembly, the entire inner surface of the reaction flow path 11, i.e., the entire flow path constituting surface of the specified reaction flow path 11, can be reliably coated.

[0088] (Regarding the second flow path 21)

[0089] The space outside the heat transfer body 41 in the radial direction (in other words, the space between the heat transfer body 41 and the inner circumferential surface of the outer cylinder 20) forms a second flow path 21 with an approximately triangular axial cross-sectional shape. This second flow path 21 is defined by: a bottom surface 22 formed by the inner circumferential surface of the outer cylinder 20; two inclined surfaces, a first inclined surface 23 and a second inclined surface 24; and a top 25 between the first inclined surface 23 and the second inclined surface 24. The top 25 can be a point-like vertex with no length in the axial cross-sectional shape, or it can be a straight or curved top with length in the axial cross-sectional shape. When the top 25 is set to be a straight or curved top with length in the axial cross-sectional shape, it is preferable that the axial length (a) of the top 25 is shorter than the axial length (b) of the inclined surfaces 23 and 24. It is more appropriate for the first inclined surface 23 and the second inclined surface 24 to be straight in the axial cross-sectional view, but they can also be curved, such as bow-shaped curves.

[0090] Furthermore, the description of the heat transfer element 41, such as the apex angle θ of the approximate triangle in the axial sectional view, also applies to the second flow path 21.

[0091] Unlike the reaction flow path 11, the second flow path 21 is a closed space in the axial cross-sectional view. Therefore, it remains closed by separating only the inner cylinder 10 and the outer cylinder 20. However, the second flow path 21 usually allows hot media such as water vapor, warm water, cold water, and nitrogen to pass through as the second fluid F2. Therefore, unlike the reaction flow path 11, the possibility of fluids adhering is small.

[0092] (Regarding the third flow path 31)

[0093] A spirally extending plate-shaped flow path 42 is fixed to the outer circumference of the third cylinder 30 by welding or the like, thereby making the third flow path 31 a spiral space. The circumferential direction of the third flow path 31 can be the same as or different from the circumferential direction of the reaction flow path 11 and the second flow path 21 (e.g., clockwise and counterclockwise).

[0094] As long as the inner cylinder 10 and the third cylinder 30 are not separated, the third flow path 31 remains closed. However, since the third flow path 31 usually allows hot media such as water vapor, warm water, cold water, and nitrogen to pass through as the third fluid F3, it is less likely to have fluids adhering to it than the reaction flow path 11.

[0095] (Regarding inflows and outflows)

[0096] The inner cylinder 10, outer cylinder 20, and third cylinder 30 each have a dome-shaped bottom 18, bottom 28, and bottom 34, respectively. The space between the bottom 18 of the inner cylinder 10 and the bottom 28 of the outer cylinder 20 is connected to the lower part of the spiral-shaped reaction flow path 11, and the space between the bottom 18 of the inner cylinder 10 and the bottom of the third cylinder 30 is connected to the lower part of the spiral-shaped third flow path 31.

[0097] Figure 1 The lower end of the reaction flow path 11 is connected to the external flow path via the inlet 16. In this example, the inlet 16 is implemented as a structure in which a T-shaped connecting pipe is installed in a through hole opening into the bottom 28 of the outer cylinder 20. The T-shaped connecting pipe consists of a branch pipe and a confluence section where the branch pipes merge, such as... Figure 1 As shown, a static mixer or various continuous mixers, etc., can also be configured at the confluence of the T-shaped connecting pipe. The upper end of the reaction flow path 11 is connected to the external flow path via the outlet 17. In this example, the outlet 17 is configured such that a connecting pipe is installed in a through hole opening in the flange 40. The reaction fluids F1(A) and F1(B) are introduced from the branch pipes of the T-shaped connecting pipe constituting the inflow path 16, respectively, and merge into the same flow path at the confluence. The merged reaction fluid F1 flows into the spiral reaction flow path 11, spiraling upwards, and flows out to the outside from the outlet 17.

[0098] Next, the upper end of the second flow path 21 is connected to the external flow path via the inlet 26. In this example, the inlet 26 is configured to have a connecting pipe installed in the through hole opening into the outer cylinder 20. The lower end of the second flow path 21 is connected to the external flow path via the outlet 27. In this example, the outlet 27 is configured to have a connecting pipe installed in the through hole opening into the outer cylinder 20. The second fluid F2 flows from the inlet 26 into the spiral-shaped second flow path 21, descends in a spiral shape, and flows out from the outlet 27 to the outside.

[0099] Next, the upper end of the third flow path 31 is connected to the external flow path via the inlet 32. In this example, the inlet 32 ​​is configured to have a connecting pipe installed in a through hole opening into the flange 40. The lower end of the third flow path 31 is connected to the external flow path via the outlet 33. In this example, the outlet 33 is configured to have a connecting pipe installed in a through hole opening into the center of the bottom 34, and this connecting pipe extends axially within the cylindrical space inside the third cylinder 30 to a height approximately the same as the outlet 17 of the reaction flow path 11 and the inlet 26 of the second flow path 21. The third fluid F3 flows from the inlet 32 ​​into the spiral-shaped third flow path 31, descends in a spiral shape, and flows out from the outlet 33 to the outside.

[0100] In addition, the inflow and outflow sections of each flow path can also be implemented in reverse.

[0101] The materials for each surface along the passage paths of the second fluid F2 and the third fluid F3, such as the second flow path 21 and the third flow path 31, can be selected from metals or the like, depending on the types of the second fluid F2 and the third fluid F3. However, it is also preferable to pre-coat the surfaces with a corrosion-resistant material. Examples of corrosion-resistant coatings include glass enamel, fluoropolymer coatings, and ceramic coatings.

[0102] (Second Implementation)

[0103] Figure 3 This is an axial cross-sectional view of the flow reactor according to the second embodiment. The flow reactor of this embodiment differs from the flow reactor of the first embodiment in that the third cylinder 30 is disposed outside the outer tube 20. In the following description, the differences will be the focus; for matters not described, the description of the first embodiment above applies.

[0104] In the flow reactor of this second embodiment, the inner cylinder 10, outer cylinder 20, and third cylinder 30 are arranged concentrically towards the outer side in the radial direction. The upper end of the inner cylinder 10 and the heat transfer element 41 (which can be removed as needed) is mounted on the upper flange 40, and the upper end of the outer cylinder 20 (which can be removed as needed) is mounted on the lower flange 40. The two flanges 40 can be disassembled and joined vertically. The upper end of the third cylinder 30 is joined to the outer peripheral surface near the upper end of the outer cylinder 20 by welding or the like, and the lower end of the third cylinder 30 is joined to the outer peripheral surface of the bottom 28 of the outer cylinder 20 by welding or the like.

[0105] The space on the inner surface of the heat transfer body 41, in other words, the space between the heat transfer body 41 and the inner cylinder 10, becomes the second flow path 21. The space on the outer surface of the heat transfer body 41, in other words, the space between the heat transfer body 41 and the outer cylinder 20, becomes the reaction flow path 11. The space between the outer cylinder 20 and the third cylinder 30 becomes the third flow path 31.

[0106] The heat transfer element 41 has a generally triangular cross-sectional shape in the axial cross-section, and the three-dimensional parts 43 are connected to each other via flat cylindrical parts 44. In other words, as a whole, the heat transfer element 41 is also cylindrical, and the shape of the cylindrical wall is a concave-convex shape with three-dimensional parts 43 and flat parts 44, which are spirally wrapped around each other and travel along the axial direction.

[0107] (Regarding each flow path)

[0108] The reaction flow path 11 is defined by a bottom surface 12 formed by the inner circumferential surface of the outer cylinder 20, two inclined surfaces 13 and 14, and a top 15 between the first inclined surface 13 and the second inclined surface 14. The top 15 is formed by a flat portion 44, which is a linear top with length in the axial cross-sectional shape, but it can also be a point-like vertex without length.

[0109] The second flow path 21 is defined by a bottom surface 22, two inclined surfaces 23 and 24, and a top surface 25 between the first inclined surface 23 and the second inclined surface 24. The bottom surface 22 is formed by the outer peripheral surface of the inner cylinder 10. The top surface 25 can be a point-like vertex with no length in the axial cross-sectional shape, or it can be a line-like top with length.

[0110] A spirally extending plate-shaped flow path 42 is fixed to the inner circumferential surface of the third cylinder 30 by welding or the like, thereby making the third flow path 31 a spiral space. The circumferential direction of the third flow path 31 can be the same as or different from the circumferential direction of the reaction flow path 11 and the second flow path 21 (e.g., clockwise and counterclockwise).

[0111] (Regarding inflows and outflows)

[0112] The outer cylinder 20, the third cylinder 30 and the heat transfer body 41 have dome-shaped bottoms 28, 34 and 45 respectively, but the inner cylinder 10 does not have a dome-shaped bottom. Its bottom end is fixed to the inner surface of the bottom 45 of the heat transfer body 41 by welding or the like.

[0113] The lower end of the reaction flow path 11 is connected to the external flow path via the inlet 16. In this example, the inlet 16 is implemented as a structure in which a connecting pipe is installed in a through hole that opens into the bottom 28 of the outer cylinder 20.

[0114] In addition, such as Figure 3 As shown, the reaction catalyst 200 and the catalyst holding plate 201 can also be arranged together at the dome-shaped bottom. In this case, it is also advantageous to facilitate operations such as replacing the reaction catalyst 200. In addition, the catalyst holding plate 201 prevents the reaction catalyst 200 from flowing out.

[0115] The upper end of the reaction flow path 11 is connected to an external flow path via the outlet 17. In this example, the outlet 17 is configured such that a connecting pipe is installed in a through hole opening in the flange portion 40. The reaction fluid F1 flows into the spiral-shaped reaction flow path 11 from the inlet portion 16 and rises spirally, then flows out to the outside from the outlet 17.

[0116] Next, the upper end of the second flow path 21 is connected to the external flow path via the inlet 26. In this example, the inlet 26 is configured to have an L-shaped bent connecting pipe installed in a through hole opening into the inner wall surface near the upper end of the inner cylinder 10. The lower end of the second flow path 21 is connected to the external flow path via the outlet 27. In this example, the outlet 27 is configured to have an L-shaped bent connecting pipe installed in a through hole opening into the inner wall surface near the lower end of the inner cylinder 10, the bent connecting pipe extending inside the cylindrical space inside the inner cylinder 10 until its axial position is approximately the same height as the inlet 26.

[0117] The second fluid F2 flows into the spiral second flow path 21 from the inlet 26, descends while spiraling, and flows out to the outside from the outlet 27.

[0118] Next, the upper end of the third flow path 31 is connected to the external flow path via the inlet 32. In this example, the inlet 32 ​​is configured such that a connecting pipe is installed in a through hole opening near the upper end of the outer peripheral surface of the third cylinder 30. The lower end of the third flow path 31 is connected to the external flow path via the outlet 33. In this example, the outlet 33 is configured such that a connecting pipe is installed in a through hole opening near the lower end of the bottom 34 of the third cylinder 30. The third fluid F3 flows from the inlet 32 ​​into the spiral-shaped third flow path 31, descends in a spiral shape, and flows out from the outlet 33 to the outside.

[0119] In addition, the inflow and outflow sections of each flow path can also be implemented in reverse.

[0120] (Separation of the cylinder)

[0121] When the heat exchanger is disassembled by releasing the detachable connecting members (not shown) such as bolts on the upper and lower flanges 40, it can be separated into an outer cylinder 20 with the third cylinder 30 attached, an inner cylinder 10, and a heat transfer element 41. The outer cylinder 20 with the third cylinder 30 attached and the lower flange 40 can be pulled downwards as shown in the figure. As a result, the reaction flow path 11 is separated into two states, inner and outer, with the flow path forming surface of the reaction flow path 11 defined as the inner cylinder 10 side and the outer cylinder 20 side. The flow path forming surface of the reaction flow path 11 is defined as the inner circumferential surface of the outer cylinder 20 on the outer cylinder 20 side and the radially outer surface of the heat transfer element 41 on the inner cylinder 10 side. All these surfaces are configured to be directly exposed without being obstructed by other parts when viewed from a radial direction orthogonal to the axial direction. Therefore, as in the first embodiment, the reaction flow path 11 becomes extremely easy to clean.

[0122] In the first embodiment, the outer angle θo is the angle formed by the three-dimensional shape portion 43 and the outer cylinder 20. In this embodiment, the outer angle θo is the angle formed by the three-dimensional shape portion 43 and the flat portion 44. In either case, since the outer angle θo is an obtuse angle of 90 degrees or more, the open state without any narrow parts is achieved in the separated state. Therefore, cleaning the reaction flow path 11 is extremely simple, and the cleaning status is easy to confirm.

[0123] (about Figure 4 )

[0124] In addition to the embodiments described above, the present invention can be implemented with various modifications. (See also...) Figure 4 Explain these examples of changes.

[0125] Heat transfer element 41 can be as Figure 4 As shown in (A), it is disposed on the outer peripheral surface of the inner cylinder 10, or as shown in [A], it can also be disposed on the outer peripheral surface of the inner cylinder 10. Figure 4 (B) is arranged on the inner circumferential surface of the outer cylinder 20. Alternatively, the heat transfer element 41 may not have the flat portion 44 and the three-dimensional portion 43 may be fixed on the circumferential surface of the cylinder, or it may have both the three-dimensional portion 43 and the flat portion 44 and be cylindrical in shape.

[0126] like Figure 4 As shown in (A), the radial width S of the space between the inner cylinder 10 and the outer cylinder 20 is preferably 4 mm to 75 mm, and more preferably 10 mm to 50 mm.

[0127] Should Figure 4 (B) can also be considered a variation of the second embodiment. In the second embodiment, the top 25 of the heat transfer body 41 faces the outer peripheral surface of the inner cylinder 10. In contrast, in this variation, the top 25 of the heat transfer body 41 faces the inner peripheral surface of the outer cylinder 20. In this example, a gap (d) is provided between the outer peripheral surface of the flat portion 44 of the heat transfer body 41 and the inner peripheral surface of the outer cylinder 20. In other words, a space is provided between the end edge 46 of the three-dimensional shape portion 43 and the inner peripheral surface of the outer cylinder 20. This gap (d) can also be omitted, but it is more appropriate for the gap (d) to be 3 mm or less. In other words, a gap (d) is provided between the axially adjacent surrounding portions of the spiral-shaped second flow path, that is, between the axially adjacent approximately triangular cross-sectional shapes and approximately triangular cross-sectional shapes. This gap (d) can also be omitted, and when a gap (d) is provided, it is suitable to set it to 3 mm or less in the radial direction. By setting this gap (d), the second flow path 21 can be enlarged. Conversely, if the gap is too large, the second fluid F2 will not flow in a spiral shape but will instead pass through a short circuit in the axial direction, resulting in a larger amount of fluid flowing, which may reduce the efficiency of heat exchange.

[0128] Next, the third tube 30 can be as followsFigure 4 As shown in (C), it is configured and fixed to the outside of the outer cylinder 20, or as shown in (C). Figure 4 (D) The configuration is fixed inside the inner cylinder 10. Alternatively, the third cylinder 30 can be omitted and the reaction flow path 11 and the second flow path 21 can be used instead.

[0129] like Figure 4 As shown in (E), two sets of heat transfer bodies 41 can also be used. In this case, it can be represented that one heat transfer body 41 is fixed to the outer circumferential surface of the inner cylinder 10 and the other heat transfer body 41 is fixed to the inner circumferential surface of the outer cylinder 20. If the space between the two sets of heat transfer bodies 41, 41 forms a reaction flow path 11 for the flow of the reaction fluid F1, then when the inner cylinder 10 is separated from the outer cylinder 20, the reaction flow path 11 becomes separated into two states, inner and outer, and the flow path forming surface of the reaction flow path 11 is defined to be separated into the inner cylinder 10 side and the outer cylinder 20 side. The flow path forming surface of the reaction flow path 11 is defined to be the surface inside the heat transfer body 41 in the radial direction on the outer cylinder 10 side, and the surface outside the heat transfer tube 41 in the radial direction on the inner cylinder 20 side. These surfaces are configured to be directly exposed without being obstructed by other parts when viewed from a radial direction orthogonal to the axial direction.

[0130] The space between one heat transfer element 41 and the inner cylinder 10, and the space between the other heat transfer element 41 and the outer cylinder 20, constitute the second flow path and the third flow path. Additionally, in Figure 4 In (E), the two sets of heat transfer bodies 41 are arranged with the tops of the roughly triangular axial cross sections facing each other, but the spacing between them can also be staggered, etc.

[0131] Figure 4 (F) is a variation of the second embodiment, in which a fourth cylinder 50 can be concentrically arranged further inside the inner cylinder 10, and a heat transfer element 41 can be arranged in the space between the inner cylinder 10 and the fourth cylinder 50, thus allowing for the arrangement of multiple heat transfer elements 41. In the concentrically arranged inner cylinder 10 and fourth cylinder 50, from the perspective of their radial inward / outward relationship, the inner cylinder 10 is positioned further outward than the fourth cylinder 50, and the fourth cylinder 50 is positioned further inward than the inner cylinder 10. Therefore, the inner cylinder 10 corresponds to the outer cylinder 20, and the fourth cylinder 50 corresponds to the inner cylinder 10. Thus, ​ (F) is a structure in which two concentric spaces are formed between the inner cylinder 10 and the outer cylinder 20, and multiple spaces formed between the concentric inner cylinder and the outer cylinder are concentrically arranged.

[0132] In any of the above examples, the inner cylinder 10 side and the outer cylinder 20 side are designed to be assembled in a manner that allows them to be separated solely by axial (vertical) movement without rotation, and the heat transfer element 41 is sized to not interfere with other parts when moving axially (vertically). Specifically, in the case of a cylindrical inner cylinder 10 and outer cylinder 20 with a fixed radius, if the heat transfer element 41 is fixed to the inner cylinder 10 side, the maximum outer diameter of the heat transfer element 41 is set to be smaller than the inner diameter of the outer cylinder 20. Furthermore, when the heat transfer element 41 is fixed to the outer cylinder 20 side, the minimum inner diameter of the heat transfer element 41 is set to be larger than the outer diameter of the inner cylinder 20. Additionally, the present invention can also be implemented in which the inner cylinder 10 and the outer cylinder 20 are approximately conical cylinders whose radii vary with axial orientation. In this case, if the inner cylinder 10 can be separated from the outer cylinder 20 by moving the inner cylinder 10 upwards as shown in the figure, then with the heat transfer element 41 fixed to the inner cylinder 10 side, the maximum outer diameter of the heat transfer element 41 in each section orthogonal to the axial direction is set to be smaller than the inner diameter of the outer cylinder 20 above that section. Conversely, if the heat transfer element 41 is fixed to the outer cylinder 20 side, the minimum inner diameter of the heat transfer element 41 in each section orthogonal to the axial direction is set to be larger than the outer diameter of the inner cylinder 20 above that section.

[0133] Explanation of reference numerals in the attached figures

[0134] F1 reaction fluid

[0135] F2 Second Fluid

[0136] F3 Third Fluid

[0137] 10 Inner Tube

[0138] 11. Flow path for reaction

[0139] 12 Bottom

[0140] 13 First inclined plane

[0141] 14 second bevel

[0142] 15 Top

[0143] 16 Inflow Section

[0144] 17 Outflow Department

[0145] 18 bottom

[0146] 20 outer barrel

[0147] 21 Second Flow Path

[0148] 22 bottom

[0149] 23 First inclined plane

[0150] 24 second slope

[0151] 25 top

[0152] 26 Inflow Section

[0153] 27 Outflow Department

[0154] 28 bottom

[0155] 30 Third tube

[0156] 31 Third Flow Path

[0157] 32 Inflow Section

[0158] 33 outflow part

[0159] 34 bottom

[0160] 40 flange portion

[0161] 41 Heat transfer body

[0162] 42 flow path body

[0163] 43 Three-dimensional shape section

[0164] 44 flat sections

[0165] 45 bottom

[0166] λ is the maximum flow path width for the reaction flow path.

[0167] μ gap (minimum flow path width for reaction flow)

[0168] d gap

Claims

1. A flow reactor comprising a helical, surrounding flow path for flowing a reaction fluid, characterized in that, A spirally arranged heat transfer element is disposed within the space formed between the concentric inner and outer cylinders. The space is divided into a reaction flow path and a second flow path by the heat transfer body, and heat exchange occurs between the reaction fluid flowing through the reaction flow path and the heat medium flowing through the second flow path via the heat transfer body. The inner cylinder, the outer cylinder, and the heat transfer element are assembled in a manner that allows them to be separated into a side containing the outer cylinder and a side containing the inner cylinder. In a state where the flow path is separated into the side containing the outer cylinder and the side containing the inner cylinder, it is stipulated that the flow path constituting surface of the reaction flow path is separated into the side containing the outer cylinder and the side containing the inner cylinder, and that all surfaces of the flow path constituting surface of the reaction flow path are directly exposed without being obstructed by other parts when viewed from a radial direction orthogonal to the axial direction. The reaction flow path and the second flow path are both spiral-shaped flow paths. The ratio (λ / μ) of the maximum flow path width (λ) of the reaction flow path in the radial direction to the minimum flow path width (μ) of the reaction flow path is 2 or more, that is, 2≤λ / μ<∞.

2. The flow reactor according to claim 1, characterized in that, The heat transfer element is fixed to either the side where the outer cylinder is located or the side where the inner cylinder is located, but not to either the other side. It also has a three-dimensional shape with at least one bent portion that allows fluid to flow through both its inner and outer surfaces. The exterior angle of all the folded portions appearing on the flow path constituting the specified reaction flow path is 90 degrees or more.

3. The flow reactor according to claim 1 or 2, characterized in that, The reaction flow path does not have a horizontal section where the reaction fluid may accumulate.

4. The flow reactor according to claim 1 or 2, characterized in that, There is no gap between adjacent circumferential portions in the axial direction of the reaction flow path, or there is a gap of less than 4 mm in the radial direction.

5. The flow reactor according to claim 1 or 2, characterized in that, The cross-sectional shape of the reaction flow path and the second flow path in the axial sectional view is approximately triangular with a vertex angle θ of more than 30 degrees and less than 125 degrees.

6. The flow reactor according to claim 1 or 2, characterized in that, The inner cylinder side and the outer cylinder side are assembled such that they can be separated by axial movement without rotation, and the heat transfer element does not interfere with other parts when moving along the axial direction.

7. The flow reactor according to claim 1 or 2, characterized in that, The reaction flow path and the second flow path have a cross-sectional shape of approximately a triangle in an axial sectional view, consisting of two inclined planes, a bottom plane, and a top plane, wherein the axial length (a) of the top plane is shorter than the axial length (b) of the inclined planes.

8. The flow reactor according to claim 7, characterized in that, The cross-sectional area of ​​the flow path is enlarged by the top of at least one of the reaction flow path and the second flow path having a length (a) in the axial direction, compared to the case where the top is a vertex without a length (a) in the axial direction.

9. The flow reactor according to claim 1 or 2, characterized in that, The space formed between the concentrically arranged inner cylinder and the outer cylinder has multiple concentric spaces.

10. The flow reactor according to claim 1 or 2, characterized in that, At least one of the flow path for the flow of the reaction fluid, including the reaction flow path, and the flow path for the flow of the heating medium, including the second flow path, is coated with a corrosion-resistant material.

11. The flow reactor according to claim 10, characterized in that, The coating using corrosion-resistant materials is one of glass lining, fluororesin coating, or ceramic coating.

12. The flow reactor according to claim 3, characterized in that, There is no gap between adjacent circumferential portions in the axial direction of the reaction flow path, or there is a gap of less than 4 mm in the radial direction.

13. The flow reactor according to claim 3, characterized in that, The cross-sectional shape of the reaction flow path and the second flow path in the axial sectional view is approximately triangular with a vertex angle θ of more than 30 degrees and less than 125 degrees.

14. The flow reactor according to claim 4, characterized in that, The cross-sectional shape of the reaction flow path and the second flow path in the axial sectional view is approximately triangular with a vertex angle θ of more than 30 degrees and less than 125 degrees.

15. The flow reactor according to claim 3, characterized in that, The reaction flow path and the second flow path have a cross-sectional shape of approximately a triangle in an axial sectional view, consisting of two inclined planes, a bottom plane, and a top plane, wherein the axial length (a) of the top plane is shorter than the axial length (b) of the inclined planes.

16. The flow reactor according to claim 4, characterized in that, The reaction flow path and the second flow path have a cross-sectional shape of approximately a triangle in an axial sectional view, consisting of two inclined planes, a bottom plane, and a top plane, wherein the axial length (a) of the top plane is shorter than the axial length (b) of the inclined planes.

17. The flow reactor according to claim 5, characterized in that, The reaction flow path and the second flow path have a cross-sectional shape of approximately a triangle in an axial sectional view, consisting of two inclined planes, a bottom plane, and a top plane, wherein the axial length (a) of the top plane is shorter than the axial length (b) of the inclined planes.

18. The flow reactor according to claim 6, characterized in that, The reaction flow path and the second flow path have a cross-sectional shape of approximately a triangle in an axial sectional view, consisting of two inclined planes, a bottom plane, and a top plane, wherein the axial length (a) of the top plane is shorter than the axial length (b) of the inclined planes.

19. The flow reactor according to claim 3, characterized in that, The space formed between the concentrically arranged inner cylinder and the outer cylinder has multiple concentric spaces.

20. The flow reactor according to claim 4, characterized in that, The space formed between the concentrically arranged inner cylinder and the outer cylinder has multiple concentric spaces.

21. The flow reactor according to claim 5, characterized in that, The space formed between the concentrically arranged inner cylinder and the outer cylinder has multiple concentric spaces.

22. The flow reactor according to claim 6, characterized in that, The space formed between the concentrically arranged inner cylinder and the outer cylinder has multiple concentric spaces.

23. The flow reactor according to claim 7, characterized in that, The space formed between the concentrically arranged inner cylinder and the outer cylinder has multiple concentric spaces.

24. The flow reactor according to claim 8, characterized in that, The space formed between the concentrically arranged inner cylinder and the outer cylinder has multiple concentric spaces.

25. The flow reactor according to claim 3, characterized in that, At least one of the flow path for the flow of the reaction fluid, including the reaction flow path, and the flow path for the flow of the heating medium, including the second flow path, is coated with a corrosion-resistant material.

26. The flow reactor according to claim 4, characterized in that, At least one of the flow path for the flow of the reaction fluid, including the reaction flow path, and the flow path for the flow of the heating medium, including the second flow path, is coated with a corrosion-resistant material.

27. The flow reactor according to claim 5, characterized in that, At least one of the flow path for the flow of the reaction fluid, including the reaction flow path, and the flow path for the flow of the heating medium, including the second flow path, is coated with a corrosion-resistant material.

28. The flow reactor according to claim 6, characterized in that, At least one of the flow path for the flow of the reaction fluid, including the reaction flow path, and the flow path for the flow of the heating medium, including the second flow path, is coated with a corrosion-resistant material.

29. The flow reactor according to claim 7, characterized in that, At least one of the flow path for the flow of the reaction fluid, including the reaction flow path, and the flow path for the flow of the heating medium, including the second flow path, is coated with a corrosion-resistant material.

30. The flow reactor according to claim 8, characterized in that, At least one of the flow path for the flow of the reaction fluid, including the reaction flow path, and the flow path for the flow of the heating medium, including the second flow path, is coated with a corrosion-resistant material.

31. The flow reactor according to claim 9, characterized in that, At least one of the flow path for the flow of the reaction fluid, including the reaction flow path, and the flow path for the flow of the heating medium, including the second flow path, is coated with a corrosion-resistant material.

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