JP2014147925A - Multitubular reactor - Google Patents

Abstract

PROBLEM TO BE SOLVED: To reduce the pressure loss of a heat medium without deteriorating its heat exchange performance.SOLUTION: The multitubular reactor comprises, on both the edge parts of a reaction vessel 1, a reaction raw material distribution header 3 partitioned with tube plates 2 and 4; and a reaction product assembly header 5. The annular region between the respective tube plates 2 and 4 is provided with a tube group 6 made of a plurality of heat transfer tubes 7 connected to the respective headers 3 and 5 and filled with a catalyst 8, and the inside and the outer circumferential side are made into a heat medium dispersed region 9 and a heat medium assembled region 10. The heat transfer coefficient on the side of a reaction raw material 15 made into the factor of the rate-limiting of a heat transfer coefficient is fixed as the heat transfer coefficient on the inside of the tube. In this way, even if reduction in the flow velocity or the change in the flow velocity of a heat medium 13 flowing outwardly from the inside of the radial direction of the tube group 6 from the heat medium dispersed region 9 to the heat medium assembled region 10 is caused, its heat passing rate is made stable even without being reduced.

Description

  The present invention relates to a multitubular reactor used for performing a catalytic reaction while controlling reaction temperature conditions.

  In the process of continuously producing reaction products from reaction raw materials by catalytic reaction, in order to prevent temperature changes accompanying the progress of catalytic reaction, which is exothermic reaction or endothermic reaction, indirect contact with the heat medium during the catalytic reaction is performed. The reaction temperature condition is kept constant by performing simultaneous heat exchange in parallel.

  As an apparatus for efficiently carrying out the catalytic reaction while controlling the reaction temperature condition using heat exchange between this kind of heat medium and reaction raw materials and reaction products, for example, production of acrylic acid, ethylene acid, There are multi-tubular reactors (tubular reactors) widely used in the manufacturing process of methacrylic acid and other various chemical substances.

  The multitubular reactor is roughly classified into an in-tube catalyst type and an out-of-tube catalyst type.

  In general, a multi-tubular reactor of the in-tube catalyst type is provided with a reaction material distribution chamber partitioned by a tube plate at one end of a reaction vessel, and partitioned by a tube plate at the other end of the reaction vessel. A collection chamber for the reaction product produced is provided. A tube group of a plurality of parallel heat transfer tubes is arranged between the tube plates, and both end portions of each heat transfer tube are attached so as to communicate with both the distribution chamber and the collecting chamber. In each of the heat transfer tubes, a catalyst is filled.

  As described above, the multi-tube reactor of the in-tube catalyst type in which the catalyst is filled in each heat transfer tube, the space between the tube plates in the reaction vessel and the space outside the heat transfer tubes is a heat medium flow. It is an area.

  The heat medium flow area includes one end of the heat medium flow area close to one of the tube plates and the other end of the heat medium flow area close to the other tube plate. The heating medium inlet and outlet are respectively provided in the section, and further baffles (baffle plates) are provided at a plurality of intervals from the one end to the other end in the heating medium circulation area. The configuration is widely adopted. According to this configuration, the heating medium that flows into the heating medium circulation region from the inlet of the heating medium sequentially bypasses the baffles in the process of flowing toward the outlet of the heating medium. As a result, in the heat medium flow region, the flow direction of the heat medium is always a flow in a direction orthogonal to the longitudinal direction of each heat transfer tube of the tube group (hereinafter referred to as a tube group cross flow). It is trying to hit. Moreover, in the heat medium flow region, the flow rate of the heat medium is increased by restricting the cross-sectional area of the heat medium flow path by the baffles.

  Therefore, in the conventional tube catalyst type multi-tube reactor having the above-described configuration, in the heat medium circulation region, the tube group cross-flow of the heat medium is generated in a state where the flow velocity is increased, The heat transfer coefficient between the heat transfer tubes and the heat medium in contact with the outer surface thereof (hereinafter referred to as the heat transfer coefficient outside the tubes) is increased (for example, see Patent Document 1).

  In general, an external catalyst type multi-tube reactor has a plurality of parallel cooling pipes (cooling pipes) arranged in a reaction vessel, and one end side and the other end side of each cooling pipe. The cooling medium distribution pipe and the collecting pipe are connected to each other. The outside of each cooling pipe in the reaction vessel is configured to be filled with a catalyst.

  Furthermore, as one of the tube-type reactors of this type of extra-catalyst type, for example, a reaction raw material and a reaction product are passed through the outer peripheral portion and the central portion of the reaction vessel, but the catalyst cannot pass through. A reaction material dispersion chamber in which an outer peripheral section and a central section partitioned by a catalyst holding partition plate having (openings) are formed, and one of the sections communicates with a gas inlet. And the other compartment serves as a reaction product collecting chamber communicating with the gas outlet, and the reaction raw material is circulated inward or outward along the radial direction in the catalyst layer outside each cooling pipe. (For example, refer to Patent Document 2).

  Normally, in a multitubular reactor, in order to maintain a certain reaction temperature condition when performing a catalytic reaction, the heat medium is a reaction raw material so that the heat capacity of the heat medium is increased. It is made to supply in large quantities compared with the supply amount.

JP 2006-510471 A JP-A-55-149640

  However, among the multi-tube reactors of the in-tube catalyst type, when the gas is circulated as the reaction raw material and the reaction product in each heat transfer tube filled with the catalyst, or when the heat medium exchanges heat outside the heat transfer tube In a multi-tube reactor in which a phase change such as evaporation or condensation occurs between a liquid and a gas, and the flow rates of the reaction raw materials and reaction products in each heat transfer tube are set low. In some cases, the heat transfer coefficient between each heat transfer tube and the reaction raw material or reaction product in contact with its inner surface (hereinafter referred to as the heat transfer coefficient inside the tube) is smaller than the heat transfer coefficient outside the tube. is there.

  In this case, the heat passage rate (overall heat transfer coefficient) in the tube wall inside / outside through the tube wall of each heat transfer tube between the reaction raw material and reaction product and the heat medium is the heat inside the tube. It depends heavily on the transmission rate. Therefore, the heat transfer coefficient inside the tube is rate-limiting with respect to the entire heat transfer rate in the tube wall inside / outside direction.

  As described above, when the heat transfer coefficient inside the tube is rate-limiting with respect to the heat passage rate in the tube wall inside and outside, as shown in Patent Document 1, a plurality of baffles are provided in the heat medium circulation region. Even if the heat transfer rate outside the pipe is increased by generating a cross flow of the pipe group of the heat medium in the state where the flow velocity is increased in the heat medium circulation region, the heat transfer rate in the inside / outside direction of the pipe is improved. It hardly contributes to the improvement of the heat exchange performance by.

  In addition, in the one shown in Patent Document 1, since the flow direction of the heat medium is folded back and forth by each baffle in the heat medium circulation region, the pressure loss increases and the heat is generated by each baffle. Since the cross-sectional area of the flow path of the medium is limited, the actual situation is that the pump power for supplying the heat medium is increased.

  Since the one disclosed in Patent Document 2 is a multi-tubular reactor of an external catalyst type, the heat transfer coefficient between each cooling pipe and the cooling medium in contact with the inner surface thereof, that is, heat transfer inside the pipe. The rate is nearly uniform across all cooling tubes.

  On the other hand, since it is the reaction raw material and reaction product that are gases that flow through the catalyst layer outside each cooling pipe, the heat between each cooling pipe and the reaction raw material and reaction product in contact with the outer surface thereof. The heat transfer rate outside the tube, which is the transfer rate, becomes a rate-limiting factor with respect to the heat passage rate in the tube wall inside and outside.

  At this time, in the one disclosed in Patent Document 2, the change in the flow rate of the reaction raw material and the reaction product accompanying the change in the cross-sectional area of the flow channel near the center of the reaction vessel and the outer periphery is the outside of the tube. In order to greatly affect the heat transfer rate, a large difference occurs in the heat passage rate in the tube wall inside and outside the cooling tube near the center of the reaction vessel and the cooling tube near the outer periphery of the reaction vessel. In the vicinity of the center and the outer periphery of the reaction vessel, it is difficult to make the temperature conditions uniform, and there is a possibility that the catalytic reaction is biased, and it is difficult to make the catalytic reaction proceed uniformly in the reaction vessel.

  Therefore, the present invention reduces the pressure loss of the heat medium without degrading the heat exchange performance when the heat transfer coefficient inside the tube is smaller than the heat transfer rate outside the tube, which is the in-tube catalyst type. It is possible to reduce the pump power for the heat medium, and to suppress the possibility that the heat transfer rate is uneven for each heat transfer tube in the reaction vessel. It is an object of the present invention to provide a multitubular reactor capable of proceeding with the above.

  In order to solve the above problems, the present invention, corresponding to claim 1, is a reaction raw material distribution header formed by partitioning with a tube plate at one axial end in a cylindrical reaction vessel, and the reaction vessel The reaction product assembly header formed by partitioning at the other axial end with another tube plate, and the annular region excluding the central portion and the outer peripheral portion in the space between the tube plates in the reaction vessel A tube group comprising a plurality of heat transfer tubes parallel to the axial direction of the reaction vessel, and both ends of each heat transfer tube communicating with the reaction raw material distribution header and the reaction product assembly header, and each heat transfer tube And between the tube plates in the reaction vessel, a space in the central portion inside the tube group and a space in the outer peripheral portion outside the tube group. One of the spaces is the heat medium dispersion region, and the other space is the heat medium assembly A heat medium supply pipe communicated with the heat medium dispersion area, a heat medium discharge pipe communicated with the heat medium assembly area, a reaction raw material inlet communicated with the reaction raw material distribution header, and A multi-tube reactor having a configuration in which a reaction product outlet communicated with the reaction product assembly header is provided.

  Further, according to claim 2, in the above configuration, the inner peripheral heat medium dispersion plate and the outer peripheral heat medium dispersion plate are disposed at the inner peripheral side and outer peripheral side positions of the tube group between the tube plates. A configuration is adopted in which the group and the heat medium dispersion region and the heat medium assembly region are provided in a partitioning manner.

  Further, corresponding to claim 3, in each of the above-mentioned configurations, the heat medium supply pipe is disposed through the inside of the reaction product assembly header, and after passing through each heat transfer tube, the reaction product flowing to the reaction product assembly header And the flow of the heat medium flowing through the heat medium supply pipe are opposed to each other.

According to the multitubular reactor of the present invention, the following excellent effects are exhibited.
(1) When the heat transfer coefficient inside the tube is smaller than the heat transfer coefficient outside the tube, the heat exchange performance through the tube wall of each heat transfer tube inside and outside each heat transfer tube is not reduced. The pressure loss of the heat medium can be reduced, and the pump power required for the heat medium supply pump can be reduced.
(2) Furthermore, it is possible to suppress the possibility that the heat transfer rate is uneven for each heat transfer tube in the reaction vessel. Therefore, the catalytic reaction can proceed evenly in each heat transfer tube.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 shows an embodiment of a multitubular reactor according to the present invention, in which FIG. The other form of implementation of this invention is shown, (a) is sectional drawing in reaction container axial center position, (b) is a BB direction arrow directional view of (a). The further another form of implementation of this invention is shown, (a) is sectional drawing in reaction container axial center position, (b) is a CC direction arrow directional view of (a). It relates to the flow analysis performed on the multitubular reactor of the present invention, (a) is a diagram showing an analysis model of the multitubular reactor of the present invention used for the analysis, (b) is an analysis model of the comparative example FIG. FIG. 9 shows the results of flow analysis performed on the multitubular reactor of the present invention, and (a) shows the pressure distribution on the heat medium side in the multitubular reactor of the present invention in comparison with the comparative example, (B) is an enlarged view showing the pressure distribution on the heat medium side in the multi-tubular reactor of the present invention.

  Hereinafter, embodiments for carrying out the present invention will be described with reference to the drawings.

  1 (a) and 1 (b) show an embodiment of the multitubular reactor of the present invention.

  That is, as shown in FIG. 1, the multitubular reactor of the present invention is a reaction raw material partitioned by a tube plate 2 at one end portion (lower end portion in the figure) in the axial direction in a cylindrical reaction vessel 1. A distribution header 3 is provided. Further, a reaction product assembly header 5 partitioned by another tube plate 4 is provided at the other end portion (upper end portion in the figure) in the axial direction in the reaction vessel 1.

  Between the tube plates 2 and 4 in the reaction vessel 1, a plurality of transmission lines arranged parallel to the axial direction of the reaction vessel 1 are arranged in an annular region excluding the central portion and the outer peripheral portion of the reaction vessel 1. A tube group 6 composed of heat tubes 7 is arranged, and both ends of each heat transfer tube 7 are connected to the reaction raw material distribution header 3 and the reaction product assembly header 5 respectively. Further, each heat transfer tube 7 is filled with a catalyst 8. In FIG. 1A, for convenience of illustration, the number of heat transfer tubes 7 is reduced as compared with FIG. 1B. Moreover, in FIG.1 (b), description of the catalyst with which each heat exchanger tube 7 was filled is abbreviate | omitted.

  The space inside the tube group 6 between the tube plates 2 and 4 in the reaction vessel 1 is a heat medium dispersion region 9, and the outer peripheral portion outside the tube group 6. The space is a heat medium assembly region 10.

  In the heat medium dispersion region 9, the downstream end of the heat medium supply pipe 11 piped from the other end in the axial direction of the reaction vessel 1 through the inside of the reaction product assembly header 5 is the center of the tube plate 4. The part is penetrated and connected in communication. On the other hand, a heat medium discharge pipe 12 is connected to the heat medium assembly region 10 through one place in the circumferential direction of the outer peripheral wall of the reaction vessel 1. As a result, when a heat medium (heat medium) 13 is supplied from an external heat medium supply source (not shown) to the upstream end of the heat medium supply pipe 11, the heat medium 13 passes through the heat medium supply pipe 11. Then, it flows into the heat medium dispersion region 9. The heat medium 13 that has flowed into the heat medium dispersion region 9 passes between the heat transfer tubes 7 of the tube group 6 arranged around the heat medium dispersion region 9 toward the heat medium assembly region 10. It begins to flow. At this time, the flow of the heat medium 13 is uniform in the circumferential direction as the heat transfer tubes 7 forming the tube group 6 become resistance and pressure loss occurs. In such a state that the heat transfer tubes 7 are dispersed, the heat transfer tubes 7 are passed toward the outer peripheral side.

  After that, the heat medium 13 that has passed through the tube group 6 from the inside in the radial direction to the outside while being dispersed in the circumferential direction as described above is a heat medium assembly provided on the outer peripheral portion in the reaction vessel 1. After being assembled in the region 10, it is discharged to the outside through the heat medium discharge pipe 12. The heat medium 13 discharged to the outside is, for example, guided to a heat exchanger (not shown), and when the catalytic reaction to be performed in the multi-tubular reactor of the present invention is an exothermic reaction, heat is dissipated (heat recovery), If the catalytic reaction is an endothermic reaction, the temperature is raised and then returned to the heating medium supply source (not shown) and recirculated. Therefore, by continuously supplying the heat medium 13 from the heat medium supply source (not shown) to the heat medium supply pipe 11, in the multitubular reactor of the present invention, the heat medium 13 around each heat transfer pipe 7. Can be continuously distributed.

  A reaction material inlet 14 communicating with the reaction material distribution header 3 is provided at one end of the reaction vessel 1 in the axial direction. Thus, when the reaction raw material 15 supplied from the reaction raw material inlet 14 flows into the reaction raw material distribution header 3, the reaction raw material 15 is dispersed in the reaction raw material distribution header 3, and then each of the transmission lines forming the tube group 6. The heat pipe 7 is supplied evenly.

  A reaction product outlet 16 communicating with the reaction product assembly header 5 is provided at a position where it does not interfere with the heat medium supply pipe 11 at the other end in the axial direction of the reaction vessel 1. Thereby, after the reaction product 17 produced | generated by the catalytic reaction in each said heat exchanger tube 7 to which the reaction raw material 15 is supplied from the said reaction raw material distribution header 3 is aggregated by the said reaction product assembly header 5, The reaction product is taken out through the reaction product outlet 16. Furthermore, the flow of the reaction product 17 led from the heat transfer tubes 7 through the reaction product assembly header 5 to the reaction product outlet 16 and supplied to the heat medium dispersion region 9 through the heat medium supply tube 11. By making the flow of the heating medium 13 counter flow, the heating ability or cooling ability of the heating medium 13 can be used effectively.

  In the present embodiment, the heat medium 13 is liquid, and the reaction raw material 15 and the reaction product 17 have a lower (smaller) heat transfer coefficient with respect to the tube wall of the heat transfer tube 7 than the heat medium 13. ) Shall be gas.

  The heat medium 13 is a cooling medium, depending on whether the catalytic reaction that generates the reaction product 17 from the reaction raw material 15 in each heat transfer tube 7 is an exothermic reaction or an endothermic reaction, or A heating medium may be used. In addition, the heat medium 13 may be appropriately selected and used in a kind that can meet the temperature conditions desired for the catalytic reaction.

  When using the multitubular reactor according to the present invention having the above-described configuration, first, the external heating medium supply source (not shown) is previously set to a desired temperature as a reaction temperature condition for performing a catalytic reaction described later. The heat medium 13 with the temperature adjusted is continuously supplied to the upstream end of the heat medium supply pipe 11.

  As a result, the heat medium 13 passes through the heat medium supply tube 11 and the heat medium dispersion region 9 in the reaction vessel 1 and is uniformly dispersed in the circumferential direction and the longitudinal direction of each heat transfer tube 7. It becomes possible to continuously circulate between the heat transfer tubes 7 forming the group 6. For this reason, each heat exchanger tube 7 is subjected to heat exchange with the heat medium 13 on the outer surface side thereof.

  Thereafter, the heat medium 13 after being subjected to heat exchange with each of the heat transfer tubes 7 is discharged to the outside through the heat medium assembly region 10 on the outer periphery of the tube group 6 and the heat medium discharge tube 12. Become.

  At this time, the inner surface of each heat transfer tube 7 and the catalyst 8 inside the heat transfer tube 7 are always maintained at the predetermined reaction temperature conditions in accordance with the heat exchange between the heat transfer tubes 7 and the heat medium 13 flowing outside the heat transfer tubes 7. Will come to be.

  In this state, when the reaction raw material 15 is supplied from the reaction raw material inlet 14 by a reaction raw material supply means (not shown), the reaction raw material 15 is dispersed in the reaction raw material distribution header 3 and then into the heat transfer tubes 7. Supplied on average.

  In each of the heat transfer tubes 7, a reaction product 17 is generated from the supplied reaction raw material 15 under the predetermined reaction temperature condition due to the presence of the catalyst 8 filled in the heat transfer tubes 7. A catalytic reaction is carried out. At this time, regardless of whether the catalytic reaction is an exothermic reaction or an endothermic reaction, the heat exchange with the heat medium 13 continuously flowing outside the heat transfer tubes 7 causes heat generated by the heat generation or endotherm. Is continuously absorbed, and the catalyst 8 in each heat transfer tube 7 can be maintained at the predetermined reaction temperature condition.

  The reaction products 17 generated by the catalytic reaction in the heat transfer tubes 7 are guided from the heat transfer tubes 7 to the reaction product assembly header 5 and are temporarily assembled in the reaction product assembly header 5. Then, it is recovered to the outside through the reaction product outlet 16.

  Thus, according to the multitubular reactor of the present invention, the reaction raw material 15 and the reaction product 17 as the gas to be circulated inside each heat transfer tube 7, and the heat medium 13 to be circulated outside each heat transfer tube 7. The reaction product 17 is continuously produced from the reaction raw material 15 by the above catalytic reaction while maintaining the reaction temperature condition in each heat transfer tube 7 by heat exchange with the heat transfer tube 7 through the tube wall. Can do.

  At this time, the flow direction of the heat medium 13 to exchange heat with the heat transfer tubes 7 is changed from the heat medium dispersion region 9 provided in the center of the reaction vessel 1 to the heat medium assembly region 10 provided in the outer periphery. Since it is outward (radial direction) along the radial direction, the flow of the heating medium 13 is folded many times like a conventional multi-tubular reactor with a baffle in a conventional heating medium circulation region. There is nothing. Further, in the flow path of the heat medium 13 from the heat medium dispersion region 9 to the heat medium assembly region 10, the cross-sectional area is not limited by the baffle. For this reason, in the multitubular reactor of the present invention, the pump power for supplying the heat medium 13 can be reduced.

  In the multi-tubular reactor of the present invention, the flow path of the heat medium 13 flows around each heat transfer tube 7 of the tube group 6 as the flow path of the heat medium 13 is not limited by the cross-sectional area due to the baffle as in the prior art. The average flow velocity of the heat medium 13 becomes slow, and as the flow velocity of the heat medium 13 decreases, the heat transfer coefficient outside the heat transfer tubes 7 decreases.

  However, as described above, in the multi-tubular reactor of the present invention, the reaction raw material 15 and the reaction product 17 to be circulated inside the heat transfer tube 7 are gases, and the heat transfer coefficient inside the tube is outside the tube. Since the heat transfer coefficient is smaller than the heat transfer coefficient, the heat transfer coefficient in the tube wall direction of each heat transfer tube 7 in which the heat transfer coefficient inside the tube is a rate-determining factor is a decrease in the heat transfer coefficient outside the tube. Little affected. Therefore, the multitubular reactor of the present invention does not cause a decrease in heat exchange performance. This is also clear from the results of numerical analysis of Example 1 described later.

  Furthermore, in the multitubular reactor of the present invention, the reaction raw material 15 is supplied to each heat transfer tube 7 on average as described above. Therefore, there is no difference in the flow rate of the reaction raw material 15 and the reaction product 17 in each heat transfer tube 7, and therefore there is no difference in the heat transfer coefficient inside the tube for each heat transfer tube 7.

  On the other hand, the flow rate of the heat medium 13 of the heat transfer medium 13 flows from the inner peripheral side toward the outer peripheral side of the tube group 6 because the flow path cross-sectional area increases as it goes outward in the radial direction. The inner peripheral portion is maximum and decreases as it goes outward in the radial direction. Therefore, between the heat transfer tubes 7 arranged at different positions in the radial direction of the tube group 6, a difference occurs in the heat transfer coefficient outside the tubes according to the change in the flow rate of the heat medium.

  However, as described above, in the multi-tubular reactor of the present invention, the heat transfer coefficient inside the tube is a rate-determining factor with respect to the heat transfer rate inside and outside the tube wall of each heat transfer tube 7, Even if the heat transfer tubes 7 arranged at different positions in the radial direction of the tube group 6 have a large flow rate change in the heat medium 13 on the outside of the tube, there is a large difference in the heat passage rate in the tube wall inner / outer direction. It does not occur and is stable throughout. This is also clear from the results of numerical analysis in Example 2 described later.

  Therefore, according to the multi-tubular reactor of the present invention, it is possible to suppress the possibility that the heat transfer rate is biased with respect to all the heat transfer tubes 7 in the reaction vessel 1. Thus, the catalytic reaction can be allowed to proceed evenly.

  Furthermore, when the heat medium 13, which is a fluid with good heat transfer characteristics, is flowed as a cross flow on the outside of the heat transfer tube 7, the heat transfer is compared to the case where the heat medium 13 is flowed on the inside of the heat transfer tube 7. The rate can be improved. Therefore, the multi-tubular reactor of the present invention has a heat transfer rate significantly higher than that of a multi-tubular reactor in which the reaction raw material is circulated in the radial direction of the reaction vessel in the radial direction of the reaction vessel. It becomes possible to improve.

  Next, FIGS. 2A and 2B show a modification of the embodiment of FIGS. 1A and 1B as another embodiment of the present invention.

  That is, the multitubular reactor according to the present embodiment has the same configuration as that of FIGS. 1A and 1B, and replaces the heat medium supply pipe 11 and the heat medium discharge pipe 12 so that each pipe in the reaction vessel 1 is replaced. Between the plates 2 and 4, the space on the outer periphery outside the tube group 6 is a heat medium dispersion region 9 communicating with the heat medium supply tube 11, and the central portion inside the tube group 6 is located in the center. The space is defined as a heat medium assembly region 10 that communicates with the heat medium discharge pipe 12.

  Other configurations are the same as those shown in FIGS. 1A and 1B, and the same components are denoted by the same reference numerals.

  When the multitubular reactor according to the present embodiment having the above-described configuration is used, the heat transfer tube 7 is supplied from an external heating medium supply source (not shown) in the same manner as shown in FIGS. The heating medium 13 in a state in which the temperature is adjusted in advance to a desired temperature as a reaction temperature condition for performing the catalytic reaction is continuously supplied to the upstream end of the heating medium supply pipe 11.

  Thereby, the heat medium 13 flows into the heat medium dispersion region 9 provided on the outer periphery of the tube group 6 through the heat medium supply pipe 11 in the reaction vessel 1. Thereafter, the heat medium 13 that has flowed into the heat medium dispersion region 9 passes between the heat transfer tubes 7 of the tube group 6 disposed inside the heat medium dispersion region 9, and thus the heat medium assembly region 10. It flows inwardly along the radial direction of the reaction vessel 1 toward. At this time, the flow of the heat medium 13 is uniform in the circumferential direction as the heat transfer tubes 7 forming the tube group 6 become resistance and pressure loss occurs. In the state of being dispersed to each other, it passes between the heat transfer tubes 7 toward the inner peripheral side.

  Thereby, in each heat exchanger tube 7 of the said tube group 6, heat exchange with the said heat medium 13 comes to be performed in the outer surface side.

  Thereafter, the heat medium 13 after being subjected to heat exchange with each heat transfer tube 7 is assembled in the heat medium assembly region 10 inside the tube group 6 and then passed through the heat medium discharge tube 12 to the outside. It will be discharged.

  Therefore, also in the present embodiment, the inner surface of each heat transfer tube 7 and the catalyst 8 inside the heat transfer tube 7 are subjected to heat exchange between the heat transfer tube 7 and the heat medium 13 flowing outside the heat transfer tube 7. The reaction temperature condition can always be maintained.

  Therefore, also in the present embodiment, as in the embodiment of FIGS. 1 (a) and 1 (b), the supply is performed in the heat transfer tubes 7 in the presence of the catalyst 8 under the predetermined reaction temperature condition. The catalytic reaction for generating the reaction product 17 from the reaction raw material 15 to be performed can be performed, and the same effects as those in the embodiment of FIGS. 1A and 1B can be obtained.

  Next, FIGS. 3A and 3B show an application example of the embodiment of FIG. 1 as still another embodiment of the present invention.

  That is, the multi-tubular reactor according to the present embodiment has a configuration similar to that shown in FIGS. 1A and 1B, inside the tube group 6 between the tube plates 2 and 4 (the center of the reaction vessel 1). A heat medium dispersion region 9 communicating with the heat medium supply pipe 11, an inner peripheral heat medium dispersion plate 18 as a cylindrical heat medium dispersion plate extending in the axial direction of the reaction vessel 1, The tube group 6 is arranged so as to be separated from the installation location of the tube group 6. 3 (a) and 3 (b), the inner peripheral heat medium dispersion plate 18 has the same diameter as the heat medium supply pipe 11, and is provided at a position continuous in the axial direction of the heat medium supply pipe 11. Is shown.

  The inner peripheral heat medium dispersion plate 18 allows the heat medium 13 to pass in and out of the cylindrical peripheral wall, and causes some pressure loss when the heat medium 13 passes through the peripheral wall. Thus, it is possible to promote the dispersion of the heat medium 13 flowing from the heat medium dispersion region 9 into the installation location of the tube group 6 in the circumferential direction and the longitudinal direction of each heat transfer tube 7. In addition, if this inner periphery part heat-medium dispersion | distribution board 18 is equipped with the dispersion | distribution function of the heat medium 13 as mentioned above, for example, the structure which provided the slit and opening which are not shown in a surrounding wall, or a surrounding wall is a mesh, Arbitrary configurations such as a configuration formed of a punching metal may be adopted.

  Further, in the present embodiment, a cylindrical heat medium dispersion extending in the axial direction of the reaction vessel 1 is located outside the tube group 6 between the tube plates 2 and 4 (near the outer periphery of the reaction vessel 1). The outer peripheral heat medium dispersion plate 19 as a plate is provided so as to partition the heat medium collecting region 10 communicating with the heat medium discharge pipe 12 and the installation location of the tube group 6.

  The outer peripheral heat medium dispersion plate 19 includes a peripheral wall configured to promote dispersion in the circumferential direction of the heat medium 13 and the longitudinal direction of each heat transfer tube 7 similar to the inner peripheral heat medium dispersion plate 18. .

  Other configurations are the same as those shown in FIGS. 1A and 1B, and the same components are denoted by the same reference numerals.

  According to the multi-tubular reactor of the present embodiment having the above-described configuration, in addition to being able to obtain the same effect by using the same as shown in FIGS. 1 (a) and 1 (b), The inner peripheral heat medium dispersion plate 18 and the outer peripheral heat medium dispersion plate 19 can smoothly flow the heat medium 13 in the heat medium dispersion region 9 and the heat medium assembly region 10, and the heat medium 13. Dispersibility in the circumferential direction of the flow and the longitudinal direction of the heat transfer tube 7 can be improved. For this reason, since the multi-tubular reactor of the present embodiment can contact the heat transfer medium 13 more evenly with respect to the heat transfer tubes 7 of the tube group 6, the heat exchange performance is further improved. The improvement and further uniformization of the catalytic reaction in each heat transfer tube 7 can be achieved. In addition, when the number of the heat transfer tubes 7 arranged in the radial direction of the tube group 6 is small due to the fact that the reaction vessel 1 is small, or the ratio of the tube pitch and the tube diameter of the heat transfer tubes 7 in the tube group 6 When (pipe pitch / tube diameter) is large, the flow resistance of the tube group cross-flow of the heat medium 13 is considered to be small. In this case, the inner peripheral heat medium dispersion plate 18 and the outer peripheral part are considered. Dispersibility in the circumferential direction of the flow of the heat medium 13 and the longitudinal direction of the heat transfer tube 7 can be maintained by setting a large resistance when the heat medium 13 passes through the heat medium dispersion plate 19.

  In addition, this invention is not limited only to the said embodiment, In the structure similar to embodiment of Fig.3 (a) (b), as shown to Fig.2 (a) (b), By replacing the heat medium supply pipe 11 and the heat medium discharge pipe 12, the space outside the outer peripheral heat medium dispersion plate 19 is provided between the tube plates 2 and 4 in the reaction vessel 1. The heat medium dispersion region 9 that communicates with the tube 11 may be used, and the space inside the inner periphery heat medium dispersion plate 18 may be the heat medium assembly region 10 that communicates with the heat medium discharge tube 12. Even with such a multi-tubular reactor, the same effects as those of the embodiment of FIGS. 3A and 3B can be obtained.

  In each of the above embodiments, the space partitioned by the tube plate 2 on one end side of the reaction vessel 1 is used as the reaction raw material distribution header 3 communicating with the reaction raw material inlet 14, and the tube plate 4 on the other end side of the reaction vessel 1. Although the configuration in which the space partitioned by the reaction product outlet header 5 communicating with the reaction product outlet 16 is shown, the reaction raw material inlet 14 and the reaction product outlet 16 are replaced with each other, The reaction raw material distribution header 3 communicating with the reaction raw material inlet 14 may be provided on the end side, and the reaction product assembly header 5 communicating with the reaction product outlet 16 may be provided on one end side of the reaction vessel 1. In this case, the flow directions of the reaction raw material 15 and the reaction product 17 are opposite to those in the above embodiments, but the same effects as those in the above embodiments can be obtained.

  Each heat transfer tube 7 in the tube group 6 can cause a pressure loss with respect to the flow of the heat medium 13 that passes through the tube group 6 radially outward or inward. As long as it is possible to promote dispersion in the direction and the longitudinal direction of each heat transfer tube 7, a square arrangement or any other arrangement other than those shown in the figure may be adopted, and the diameter of each heat transfer pipe 7 may be adopted. The number and the arrangement pitch may be changed as appropriate.

  The ratio between the axial dimension and the diameter dimension of the reaction vessel 1, the installation position of each tube plate 2 and 4 in the reaction vessel 1, the volume of the reaction raw material distribution header 3 and the reaction product assembly header 5, and each tube plate 2 4, the volume of the heat medium dispersion region 9 and the heat medium assembly region 10 (the dimension in the radial direction of the reaction vessel 1), the heat medium supply pipe 11, the heat medium discharge pipe 12, the reaction raw material inlet 14, and the reaction product outlet. The size and arrangement of 16 may be appropriately changed from those shown in accordance with conditions desired for the catalytic reaction to be performed.

  The reaction raw material 15 and the reaction product 17 may be liquids other than gas. Also in this case, the heat transfer coefficient between the reaction raw material 15 and the reaction product 17 with the inner surface of the heat transfer tube 7, that is, the heat transfer coefficient inside the tube is made smaller than the heat transfer coefficient outside the tube. It shall be.

  The multi-tubular reactor of the present invention can be applied to the case where the catalytic reaction in the production process of ethylene acid, methacrylic acid and other various chemical substances and other catalytic reactions are carried out in addition to the acrylic acid production application. Good.

  The multitubular reactor of the present invention may be used in a posture in which the axial direction of the reaction vessel 1 is oriented in any direction other than the vertical direction.

  If each heat transfer tube 7 needs to be supported for steadying at an intermediate position in the longitudinal direction, it may be supported by a tube support material such as a rod baffle in which wires and rods are combined in a lattice shape.

  Of course, various modifications can be made without departing from the scope of the present invention.

About the multitubular reactor of the present invention having the configuration shown in FIGS. 1 (a) and 1 (b), the heat transfer tube 7 and the reaction raw material 15 (and the reaction product 17), which is a gas flowing through the heat transfer tube 7, are used. heat transfer coefficient between (heat transfer coefficient of the tube side) h _i, and the heat transfer rate (heat transfer coefficient of the abluminal between the heating medium 13 of the liquid circulating outside the heat transfer tube 7 and the heat transfer tubes 7 ) h _o and, the heat transfer coefficient K through the tube wall of the heat transfer tube 7 from the heating medium 13 to the reaction material 15 (and reaction products 17), the pressure in the reaction feed 15 (and reaction products 17) side Numerical analysis was performed on the loss and the pressure loss on the heat medium 13 side.

  The calculation of the heat transmission rate K was performed based on the following formula.

  The analysis results are shown in Table 1 below.

Comparative Example 1 in Table 1 is a conventional multi-tubular reactor of a tube-in-tube type and a tube group cross-flow type, in which the heat medium 13 is placed in three places in the longitudinal direction of the heat transfer tube 7 in the heat medium flow region. A four-stage flow path configuration is provided by providing two donut-shaped baffles and one disk-shaped baffle for changing the flow direction. The configuration of the comparative example 1, in the same manner as described above, the heat transfer rate of the reaction material 15 side (the heat transfer coefficient of the tube side) h _i and the heat transfer rate of the heat medium 13 side (the heat transfer coefficient of the abluminal) h _This is a numerical analysis of _o , the heat transfer rate K, the pressure loss of the reaction raw material 15, and the pressure loss on the heat medium 13 side.

  In this case, the configuration of the multi-tube reactor of Comparative Example 1 is as follows. The diameter, tube pitch and number of the heat transfer tubes 7, the filling conditions of the catalyst 8 in the heat transfer tube 7, the flow rate of the reaction raw material 15, and the flow rate of the heat medium 13 The height of the reaction vessel 1 was set in the same manner as in the multitubular reactor of the present invention. Further, in both the present invention and Comparative Example 1, conditions were set so that the flow rate of the heat medium 13 was 1/4 times the flow rate at the outer peripheral portion of the reaction vessel 1.

In Table 1 below, the heat transfer coefficients h _i and _ho and the heat transfer coefficient K are the heat transfer coefficients on the reaction raw material 15 side based on the configuration of the in-tube catalyst type common to the present invention and Comparative Example 1. (The heat transfer coefficient inside the tube) h _i is set to 1.0 as a reference, and the analysis results of the above items of the present invention and Comparative Example 1 are normalized (non-dimensional). . Similarly, regarding the pressure loss, the value of the analysis result of the pressure loss on the reaction raw material 15 side based on the configuration of the in-pipe catalyst type common to the present invention and Comparative Example 1 is set to 1.0 as a reference, and The analysis results of the above items of Comparative Example 1 are normalized. In addition, the pressure loss value (marked with * in Table 1) on the heat medium 13 side in Comparative Example 1 is a value under a condition where there is no gap between each heat transfer tube 7 and the baffle (no gap leak). Actually, there are many cases where a minute gap is provided between each heat transfer tube 7 and the baffle. Therefore, the value of * must be treated as reference data. Normally, the ratio of the gap leak flow rate to the total flow rate of the heat medium 13 is often set to 50% or less, so even if there is a gap leak, the pressure loss on the heat medium 13 side is shown in Table 1. The order does not change for the value 4.4 shown in. Therefore, the pressure loss on the heat medium 13 side is sufficiently smaller in the multitubular reactor of the present invention than in Comparative Example 1.

As is clear from the above results, the multitubular reactor of the present invention is a heat transfer tube as compared to the multitubular reactor of the in-pipe catalyst type and the tube group cross flow type equipped with the baffle of Comparative Example 1. 7 and the heat transfer rate h _o on the heat transfer medium 13 side are reduced, but the heat transfer rate h _i on the heat transfer tube 7 and the reaction raw material 15 side which is a rate-determining factor with respect to the heat transfer rate K does not change. The passage rate K is 0.92, and the heat exchange performance is hardly lowered as compared with the value 0.97 of the heat passage rate K of Comparative Example 1.

  Moreover, in the present invention, the pressure loss on the heat medium 13 side is 0.1, which can be greatly reduced as compared with the value 4.4 of the pressure loss on the heat medium 13 side in Comparative Example 1. It turns out that you can. Therefore, in the multitubular reactor of the present invention, it is possible to reduce the pump power for the heat medium 13.

For-tube reactor of the present invention having the structure shown in FIG. 1 (a) (b), the heat transfer rate of the Example 1 and the same reaction material 15 side (tube side heat transfer coefficient) and h _i, heat transfer coefficient of the heat medium 13 side and (heat transfer coefficient of the abluminal) h _o, the overall heat transfer coefficient K, and each of the heat transfer tubes 7 of the central portion and the peripheral portion of the reaction vessel 1, and numerical analysis for their average The analysis result was compared with Comparative Example 2.

  Comparative Example 2 is a multi-tubular reactor of an external catalyst type in which a heat medium is circulated in a heat transfer tube and a catalyst is filled outside the heat transfer tube, and a radial direction is formed in the catalyst layer. This is a numerical analysis of the configuration of a multitubular reactor of a type in which reaction raw materials (and reaction products) flow inward.

Table 2 below, the multi-tube reactor of the present invention, (the heat transfer coefficient of the tube side) heat transfer rate of the reaction material 15 side h _i and the heat transfer rate of the heat medium 13 side (heat transfer abluminal For the rate) _ho and the heat transfer rate K, the central and peripheral heat transfer tubes 7 of the reaction vessel 1 and their average analysis results are shown.

Further, Table 3 below, for the comparative example 2, and the heat transfer coefficient h _o of the abluminal a heat transfer rate of the reaction raw material side, the heat transfer coefficient of the tube side is a heat transfer coefficient of the heat medium side h _i And about the heat transfer rate K, the center part of the reaction container 1, the heat exchanger tube of a peripheral part, and those average analysis results are shown.

  Tables 2 and 3 are based on the above average values for the heat transfer coefficient on the reaction raw material 15 side (in the present invention, the heat transfer coefficient inside the pipe, and in the comparative example 2 on the outside of the pipe). 0.0, the analysis results of the above items of the present invention and Comparative Example 2 are normalized.

Table 4 shows the results of comparing the above average values for the heat transfer coefficient inside the tube, the heat transfer coefficient outside the tube, and the heat transfer rate K for the present invention and Comparative Example 2. In Table 4, the value of the analysis result of the heat transfer coefficient (the heat transfer coefficient h _i on the reaction raw material 15 side) inside the pipe of the present invention is set to 1.0 as a reference, and the present invention and the comparative example 2 described above are used. The analysis results for each item above are standardized.

As is apparent from Table 2, in the present invention, in the heat transfer tubes 7 in the central portion and the peripheral portion of the reaction vessel 1, the heat flow rate of the heat medium 13 changes due to the change in the channel cross-sectional area in the inner and outer directions. Regarding the heat transfer coefficient on the medium 13 side, the central portion is 18.3 and the peripheral portion is 8.0, and a large difference occurs in the radial direction inside and outside. However, the heat transfer coefficient h _i of the reaction material 15 side of the tube side are the constant from the center to the periphery, with respect to the heat transfer coefficient K of the heat transfer coefficient h _i of the reaction material 15 is rate-limiting factor, The central portion of the reaction vessel 1 is 0.95 and the peripheral portion is 0.89, and the variation of the heat transfer rate K with respect to the average value 0.92 is within a narrow range of −3.8% to + 2.7%. ing. Therefore, in the present invention, it has been found that even the heat transfer tubes 7 arranged at different positions in the radial direction in the reaction container 1 do not cause a large difference in the heat transfer rate K. Therefore, in the multitubular reactor of the present invention, the possibility that the heat transfer rate K is biased can be suppressed for all the heat transfer tubes 7 in the reaction vessel 1. It is possible to allow the catalytic reaction to proceed.

On the other hand, as is apparent from Table 3, in Comparative Example 2, the heat transfer coefficient h _i inside the tube, which is the heat transfer coefficient on the heat medium side, is constant in the heat transfer tube from the center to the periphery of the reaction vessel. is there. On the other hand, in the heat transfer tubes in the central part and the peripheral part of the reaction vessel 1, the flow rate of the reaction raw material changes in accordance with the change in the channel cross-sectional area in the inner and outer directions. for some pipe outside the heat transfer coefficient h _o, at the center 1.25, 0.79 at the periphery, a difference depending on the presence position in the radial direction of the inner and outer heat transfer tube occur. For this reason, the heat transfer rate K, which is the rate-determining factor of the heat transfer coefficient on the reaction raw material side, is 1.13 at the center of the reaction vessel 1 and 0.74 at the periphery, which is an average of the heat transfer rate K. With respect to the value of 0.92, the deviation is large, from −19.5% to + 22.6%. Therefore, in the case of the comparative example 2, it has been found that the heat transfer rate K is a large variation of ± 20% with respect to the average value between the heat transfer tubes arranged at different radial positions in the reaction vessel. did. Therefore, in Comparative Example 2, it is difficult to perform an even catalytic reaction at different positions in the radial direction in the reaction vessel due to the bias of the heat transfer rate K.

Further, as apparent from Table 4, the reaction material 15 when placed 1.0 heat transfer coefficient h _i of the side, the heat transfer coefficient of the tube outer is the heat transfer coefficient of the reactant side of the Comparative Example 2 of the present invention Is 0.26. From the above, in the multi-tubular reactor of the present invention, the heat transfer coefficient h _i of the reactants 15 to be rate-limiting factor for the inner and outer direction of the heat transfer coefficient K of the heat transfer tube 7, the reaction feed side in the Comparative Example 2 It was found that the heat transfer coefficient can be improved as compared with the heat transfer coefficient. As a result, the multitubular reactor of the present invention can significantly improve the heat transfer rate K as compared with the extratubular catalyst type multitubular reactor as in Comparative Example 2 above. Become.

  For the multitubular reactor of the present invention having the configuration shown in FIGS. 2 (a) and 2 (b), an analysis model of the pipeline network as shown in FIG. 4 (a) is set, and the pressure distribution on the heat medium 13 side is set. The flow analysis was conducted by the analysis method of the pipeline network.

  FIG. 4B is an analysis model of a pipe network set as a comparative example, which is a conventional pipe-catalyzed multi-tubular reactor of the pipe group cross flow type similar to Comparative Example 1 in Example 1 above. There was also a flow analysis on the pressure distribution on the heat medium 13 side by the same method as described above.

  4A and 4B, the left end indicates the axial center position of the reaction vessel 1 (see FIG. 2), and the right end is the outer peripheral portion of the reaction vessel 1.

  In FIG. 4A, reference numeral 9 denotes a heat medium dispersion region, and reference numeral 10 denotes a heat medium assembly region.

  On the other hand, in FIG. 4B, symbols St1 to St4 are divided by two donut-shaped baffles b1 and b3 provided at the upper and lower portions of the heat medium flow area and one disk-shaped baffle b2 therebetween. The flow paths in the first to fourth stages formed in this way are shown. Reference numeral 20 denotes a lower header serving as a heat medium dispersion region provided in the outer periphery of the first-stage flow path St1, and reference numeral 21 denotes a heat-medium assembly provided in the outer periphery of the fourth-stage flow path St4. This is the upper header that is the area.

  Furthermore, in FIG. 4 (a) (b), the broken line in a figure has shown the installation area | region of the pipe group 6 (refer FIG. 2). In addition, the numbers with circles in the figure indicate the numbers of the nodes that become the pressure observation positions. The numbers in the diagrams of FIGS. 4A and 4B indicate the channel numbers between the nodes. In FIG. 4B, the flow paths 42 to 49, the flow paths 50 to 57, and the flow paths 58 to 65 are the heat transfer pipe 7 (see FIG. 2) of the tube group 6, the baffle b1, the baffle b2, and the baffle b3. The flow path by the clearance leak through the micro clearance gap provided between these is shown.

  The analysis results are shown in FIGS. 5 (a) and 5 (b).

  “●” in FIGS. 5A and 5B indicate the analysis result of the pressure distribution on the heat medium 13 side by the analysis model of the multitubular reactor of the present invention shown in FIG. 4A.

  On the other hand, “◯” and “Δ” in FIG. 5A indicate the analysis results of the pressure distribution on the heat medium 13 side by the analysis model of the comparative example shown in FIG. In addition, “◯” is the result under the condition that there is no gap leak due to the flow paths 42 to 49, the flow paths 50 to 57, and the flow paths 58 to 65, as in the first comparative example of the first embodiment. “Δ” is the result under the condition that there is a gap leak through the flow paths 42 to 49, the flow paths 50 to 57, and the flow paths 58 to 65.

  5A and 5B, the vertical axis represents the pressure value on the heat medium 13 side, and the flow path outlet side (“◯” and “Δ”) of the heat medium 13 represents those in FIG. ) Node 41, “●” has the pressure value of node 11) in FIG. 4A as a reference value (= 0). Furthermore, the result of pressure loss (= inlet pressure−outlet pressure) under the condition of no gap leak corresponding to Comparative Example 1 of Example 1 indicated by “◯” is the same as in Example 1 above. Normalized to take a value of .4. Further, the horizontal axis is a value obtained by making the installation region of the tube group 6 dimensionless by setting it in a range of 0.25 to 1.0 in the radial direction. Each of the pressure distributions shown in FIGS. 5 (a) and 5 (b) indicates that the inlet side of the heat medium 13 (“◯” and “Δ” is the node 2 in FIG. 4B, and “●” is in FIG. ) Takes the maximum value, and the pressure value means the pressure loss value in the installation region of the tube group 6 (within the broken lines in FIGS. 4A and 4B).

  From the results of “●” in FIGS. 5A and 5B, in the multitubular reactor of the present invention having the configuration shown in FIGS. 2A and 2B, the pressure loss on the heat medium 13 side is 0.1. It turns out that it is a grade. This result is in good agreement with the analysis result of the pressure loss on the heat medium 13 side according to Example 1 shown in Table 1 above. In addition, since the said Example 1 respond | corresponds to the structure of the multi-tubular reactor of this invention shown to FIG. 1 (a) (b), it is shown in FIG. 4 (a) used for the above-mentioned flow analysis. In the analysis model, the flow direction of the heating medium 13 is reversed in the radial direction outward and inward. Therefore, although not shown in the case of Example 1 above, if a flow analysis is performed on the pressure distribution on the heat medium 13 side and the analysis result is plotted in the same manner as in FIGS. 5A and 5B, the radius is large. It is easy to see that the pressure of the heat medium 13 decreases as it becomes, and shows a downward tendency. Furthermore, in the case of Example 1, the difference between the maximum pressure value and the minimum pressure value, that is, the pressure loss value is the same as that shown in FIG.

  Further, by comparing the results of “●” and “Δ” in FIG. 5 (a), the multi-tubular reactor of the present invention having the configuration shown in FIGS. 2 (a) and 2 (b) is shown in FIG. 4 (b). In the comparative example shown in FIG. 5, the pressure loss of the heat medium 13 is about 1.8 when the gaps are leaked by the flow paths 42 to 49, the flow paths 50 to 57, and the flow paths 58 to 65. It was also found that the pressure loss on the heat medium 13 side can be greatly reduced.

1 reaction vessel, 2 tube plate, 3 reaction material distribution header, 4 tube plate, 5 reaction product assembly header, 6 tube group, 7 heat transfer tube, 9 heat medium dispersion region, 10 heat medium assembly region, 11 heat medium supply tube , 12 Heat medium discharge pipe, 14 Reaction raw material inlet, 16 Reaction product outlet, 18 Inner peripheral heat medium dispersion plate, 19 Outer peripheral heat medium dispersion plate

Claims (3)

A reaction material distribution header formed by partitioning with a tube plate at one axial end in a cylindrical reaction vessel;
A reaction product assembly header formed by partitioning with another tube plate at the other axial end in the reaction vessel;
It consists of a plurality of heat transfer tubes parallel to the axial direction of the reaction vessel disposed in an annular region excluding the central portion and the outer peripheral portion in the space between the tube plates in the reaction vessel, and both end portions of the heat transfer tubes A tube group formed by communicating with the reaction raw material distribution header and the reaction product assembly header, and a catalyst filled in each heat transfer tube,
In addition, between the tube plates in the reaction vessel, a heat medium is dispersed in one of the central space inside the tube group and the outer peripheral space outside the tube group. Region, the other space as the heat medium assembly region,
Furthermore, a heat medium supply pipe communicated with the heat medium dispersion area, a heat medium discharge pipe communicated with the heat medium assembly area, a reaction raw material inlet communicated with the reaction raw material distribution header, and the reaction product A multitubular reactor having a structure in which a reaction product outlet communicated with an assembly header is provided.   The inner peripheral heat medium dispersion plate and the outer peripheral heat medium dispersion plate are partitioned at the inner peripheral side and outer peripheral side positions of the tube group between the tube plates, and the tube group is divided from the heat medium dispersion region and the heat medium collection region. The multi-tubular reactor according to claim 1, wherein the multi-tubular reactor is provided in an arrangement.   The heat medium supply pipe is arranged through the inside of the reaction product assembly header, and after passing through each heat transfer tube, the flow of the reaction product flowing to the reaction product assembly header and the flow of the heat medium flowing through the heat medium supply tube The multitubular reactor according to claim 1 or 2, wherein the counter flow is counterflow.

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