JPS607929A - Reactor and its use - Google Patents

Abstract

PURPOSE:To make thinner the wall thickness of an outer shell of a reactor by constructing each cooling pipe to have <=45 deg. inclination to the horizontal line to enable packing of catalyst with no difficulty and by constructing to permit passing of cooling liquid through the inside of the cooling pipes. CONSTITUTION:Gaseous products are obtd. by allowing gaseous starting material to contact with grain catalyst at reaction temp. and under reaction pressure in a reactor having covers 2, 3 at both ends and cylindrical shell 1 having a central axis inclining with <=45 deg. to the horizontal direction. Vertical side walls of the square cylindrical reaction chamber 8 contg. packed catalyst having its four vertices on the external shell 1 are made impermeable for the gas and its bottom surface except the part near both end covers is constructed so as to function as a gas-peremeable catalyst receiver 6a. Many cooling pipes 15 parallel to the central axis are provided to the reaction chamber 8 in order to let the coolant pass through, and the coolant is allowed to flow through an inlet pipe 18, flow diversing structure 16, cooling pipe 15, flow confluencing structure 17, and outlet pipe 19, in order. Further, an inlet of the starting gas and an outlet of the starting gas are provided to a part of the external shell 1.

Description

DETAILED DESCRIPTION OF THE INVENTION The present invention provides a reactor for a highly exothermic catalytic chemical reaction in which both the raw materials and products at the reaction temperature and pressure saw are gaseous. Regarding its usage.

Conventionally, a reactor with a main structure similar to a shell-and-tube heat exchanger is used as a reactor to carry out such a large exothermic reaction, and the tube is filled with a catalyst. The main method is that the raw material gas is made to flow through the tube, and the reaction heat generated inside the tube is removed from the outside of the tube, that is, from the shell side, using a cold ffl agent such as water in a boiling state under pressure. has been used. In such conventional reactors, when the reactor is enlarged, the outer shell of the reactor becomes extremely thick because it is necessary to withstand the steam pressure outside the duplex, that is, on the shell side, and the reactor itself becomes thick. The disadvantage is that the weight of the tube is significantly large, and there is no suitable method for reducing the thermal stress that occurs in the tube sheet and the joint between the tube sheet and the tube due to the temperature difference between the outer shell and the tube. Other issues remain.

The inventor of this invention previously published Japanese Unexamined Patent Application Publication No. 55-1999. 149640
and US Pat. No. 4,321,234, proposed a new type of reactor that improved the drawbacks of the above conventional methods. In this proposed reactor, two coaxial cylindrical gas-permeable catalyst receivers with different diameters are installed vertically, and the catalyst is packed between the two catalyst receivers, and the catalyst is vertically installed inside the catalyst layer. The basic structure of the reactor was that a large number of cooling pipes were arranged in a number of concentric circles coaxial with the catalyst receiver. In this improved reactor, gas is forced to flow radially through the catalyst bed, and coolant is passed from the bottom to the top of the cooling tube. At this time, the coolant is supplied from the bottom of the reactor and is divided into each cooling pipe from a number of annular distribution pipes installed at the bottom of the reactor, and the coolant flowing out from each cooling pipe is symmetrically arranged above and below. The coolant is merged into a collecting pipe having a substantially similar structure, and is discharged from the reactor through a coolant discharge pipe located at the top of the reactor. In this improved reactor, the catalyst is introduced from the catalyst inlet installed at the top of the reactor shell, passes through the gap between the adjacent collecting tubes, and is filled into a predetermined position. At the time of discharge, the catalyst in the catalyst layer passes through the gap between the adjacent distribution pipes and flows out of the reactor from the catalyst outlet installed at the lower part of the reactor shell. When this improved reactor as described above is used for a highly exothermic catalytic reaction, it is necessary to install a large number of cooling pipes within the catalyst layer. The distance between them becomes significantly smaller. It has therefore been found that the gaps between adjacent annular manifold pipes and annular distribution pipes become extremely small, leading to difficulties in filling and discharging the catalyst.

The purpose of this invention is to propose a reactor that further improves the drawbacks of the previously improved reactor and a method for using the same.

The reactor according to the present invention has the following structure, that is, it has lids at both ends, and the central axis has an inclination of 45 mm with respect to the horizontal direction.
A reaction for catalytic reactions in which a raw material that is gaseous at the temperature and pressure of the reaction is brought into contact with a particulate catalyst in a cylindrical shell at a temperature below 1) A rectangular cylinder having a square or rectangular cross section in the direction perpendicular to the central axis and having four vertices of the square or rectangle all in contact with the outer shell, inside the outer shell; (2) Of the surfaces surrounding the rectangular cylindrical reaction chamber, two opposing surfaces parallel to the central axis are substantially perpendicular and serve as gas-impermeable side walls; At least a portion of the lower surface of the cylindrical reaction chamber excluding a portion close to the rain jacket is used as a gas-permeable catalyst receiver; (2) a space surrounded by the upper surface of the reaction chamber and the upper part of the outer shell is used as an upper gas passage; ■ A space surrounded by the lower surface of the reaction chamber and the lower part of the outer shell is a lower gas passage; ■ A large number of cold II pipes parallel to the central axis are installed in the reaction chamber to allow coolant to flow; (1) One end of each cooling pipe is an inlet pipe for the coolant passing through one of the lids and extending from outside the outer shell into the inner shell. The other end of each cooling pipe is connected to the other end through a merging structure for merging the coolant in each cooling fill pipe. (1) communicating with a coolant outlet pipe that passes through one of the lids and reaches the outside of the outer shell for allowing the coolant after merging to flow out of the outer shell; An inlet for the raw material gas is installed in the outer shell part that contacts a part of one of the gas passages, and an outlet for the reaction product gas is installed in the outer shell part that contacts a desired other part of both gas passages. This is a reactor.

The content of this invention will be explained in detail below using the drawings. 1 and 2 are schematic vertical cross-sectional views of an example of the reactor of the present invention installed horizontally, in order to explain the present invention in detail. FIG. 1 is a vertical sectional view along the central axis of this reactor, and FIG. 2 △ is a sectional view perpendicular to the central axis of the reactor in FIG.
FIG. 2B is a cross-sectional view perpendicular to the central axis at section B-8 of the reactor in FIG. 1, viewed in the direction of the arrow. Figures 1 and 2
In Figures A and B, 1 is a cylindrical reactor shell with lids 2 and 3 on both ends. The inside of this shell is surrounded by gas-impermeable, substantially vertical side walls 4 and 5, a catalyst receiver 6, and a catalyst presser 7, and has a substantially square or substantially rectangular cross-sectional shape perpendicular to the central axis of the shell. A rectangular cylindrical reaction chamber 8 is installed.

In this example, the catalyst receiver 6 is composed of a gas-permeable catalyst receiver 6a located at the center with respect to the central axis direction and gas-impermeable catalyst receivers 6b at both ends of the reaction chamber.

The gas permeable catalyst receiver 6a is a combination of a commonly used perforated plate and one or two meshes. Although the catalyst retainer 7 is not absolutely necessary in the reactor of this invention, it is used in this example, and is composed of a catalyst retainer net 7a in the center and gas-impermeable catalyst retainer plates 7b at both ends. Ru. Space 1 surrounded by the upper part of the outer shell and the upper surface of the reaction chamber
3 is the upper gas passage. Further, a space 14 surrounded by the lower part of the outer shell and the catalyst receiver 6 is a lower gas passage. Inside the reaction chamber 8, a large number of cooling pipes 15 are installed parallel to the central axis of the outer cylindrical part, and one end of these cooling pipes is connected to the cooling pipe 1.
Dividing flow Ml structure 1 for diverting the coolant supplied from the coolant inlet pipe 18 to be distributed to each cooling pipe.
6, the other end is connected to a merging structure 17 for merging and coordinating the coolant flowing out from each cooling ill pipe into one coolant outlet pipe. In this example, since the branching structure 16J5 and the merging structure 17 are configured substantially symmetrically, the details will be mainly explained regarding the branching structure. That is, this branching structure 16 is configured to cool NJ supplied from the coolant inlet pipe 18.
The agent is branched into a large number of connecting pipes 16b in the primary branch pipe 16a, and is then branched into a large number of secondary branch pipes 16c connected to the large number of connecting pipes 16b, and is further branched into a large number of cooling pipes 15. It is structured like this. Each cooling pipe 1
The cold IJJ agent flowing out from 5 passes through the primary merging pipe 17a, the connecting pipe 17b and the secondary merging pipe 17c in this order, joins together, and flows out of the reactor from the coolant outlet 19. Further, in this example, the primary branch pipe 16a and the connecting pipe 16
A tubular member having a circular cross-sectional shape is shown in b as the secondary flow branch pipe 1.
A tubular member having an angular cross-sectional shape is used for 6c. Further, both ends of the primary flow branch pipe and the secondary flow branch pipe are sealed. It is also possible to use a tubular member with a circular cross-sectional shape for the secondary flow branch pipe 16c, or conversely, a tubular member having a circular cross-sectional shape can be used.
It is also possible to use a tubular member having an angular cross-sectional shape for a.

Regarding these points, the same applies to the primary merging pipe 17a and the secondary merging pipe 17c. If the number of cooling pipes is extremely small, the primary branch pipe and the secondary merging pipe may be omitted and the coolant inlet pipe 18 or one coolant outlet pipe may be directly connected to the connecting pipe 16b or 17b, respectively. On the other hand, if the number of cooling pipes is very large, the desired number of separate flow pipes and connecting pipes can be added between the primary flow pipe and the secondary flow pipe to separate the flow. The structure can be easily assembled. Also, if there are many cooling pipes,
As shown in FIG. 1, the assembly of the branching and merging structures can be facilitated by installing adjacent secondary branching pipes 16C and primary merging pipes 17a at slightly different positions in the direction of the central axis. I can do it. These merging structures and branching structures allow the coolant supplied from the coolant inlet pipe 18 to flow into each cooling pipe in a distributed manner, and then the coolant discharged from these cold MJ pipes is combined into t L, and cooled. Agent outlet pipe 19
It is a structure for discharging from the inside, and does not necessarily have to be symmetrical. Furthermore, there are many ffg implementations for these branching and merging structures and the structures at both ends of the reactor that are closely related to these structures, and the details will be described later.

In the example shown in FIGS. 1 and 2, the reaction chamber 8 is divided into two small reaction chambers 8a and 8b arranged in the direction of the central axis by a baffle plate 24 installed at approximately medium heat of the central axis. This is an example. This baffle plate 24 similarly divides the upper gas passage into two parts 13a and 13b arranged in the central axis direction. Therefore, the catalyst is filled into the space outside the cooling pipes of both reaction chambers through catalyst inlets 25a and 25b installed in reaction chambers 8a and 8b, respectively. When discharging the catalyst, the catalyst discharge ports 26a and 26b are used, respectively. When charging the catalyst, use the catalyst inlets 25a and 25.
The catalyst introduced from the outlet 26a flows down the gap between adjacent cooling pipes and is filled into the reaction chamber. It flows out of the outer shell by gravity from 26b and 26b.
In either case, if the inclination of the central axis with respect to the horizontal direction is too steep, both the charging and discharging of the catalyst cannot be performed reliably, so the inclination of the central axis with respect to the horizontal direction is 45 degrees or less. It is necessary. In the reactor of this invention, in which the length of the central axis is at least 1.5 times the diameter of the outer shell, each reaction chamber is reliably filled with catalyst regardless of whether or not the central axis is inclined. Further, it is desirable to provide two or more catalyst inlets and two or more catalyst outlets so that the catalyst can be easily discharged from each reaction chamber. In this example, approximately in the center of the small reaction chambers 8a and 8b, there is a vibration plate located approximately perpendicular to the central axis for the purpose of preventing vibration of each cold 1iI tube when the coolant is caused to flow through the cooling tube at high speed. A perforated plate 34 is installed. A cooling pipe passes through each of the six holes of this perforated plate. This vibrating porous plate 34 is not absolutely necessary for the reactor of this invention.

In the example of FIGS. 1 and 2, the raw material gas is supplied from the raw material gas port 21 to the upper gas passage 13a, passes through the catalyst layer and the gas permeable catalyst receiver (3a from top to bottom,
The gas is temporarily discharged into the lower gas passage 14. Next, the gas moves through the lower gas passage 14 in the central l-axis direction, and then the reaction chamber 8
b, passes through the catalyst layer of the reaction chamber 8b from bottom to top, passes through the upper gas passage 13b, and flows out of the reactor from the gas outlet 22. While the gas passes between the catalyst particles in the reaction chambers 8a and 8b, a chemical reaction occurs that corresponds to the composition of the raw gas and the performance of the catalyst.

The heat generated by this chemical reaction is removed by the coolant flowing through the cooling pipe 15.

As is clear from the above structural description, the heat transfer area of the cooling pipe at both ends of the reaction chamber 8 is smaller than that at the center of the reaction chamber, and therefore more gas flows through both ends of the reaction chamber. To prevent this, the catalyst receivers at both ends are made of gas-impermeable catalyst receivers 6b.
Furthermore, even when using the catalyst holder 7, it is desirable that both ends of the catalyst holder be made into gas-impermeable catalyst holder plates 7b. For similar reasons, it is often desirable to fill both ends of the reaction chamber with particulate material that has no catalytic action and has a large resistance to gas flow. For filling and discharging such particulate matter,
Inlets 25c and 25d and outlets 26c and 26d for this particulate material can also be installed near both ends of the reaction chamber. Further, in this example, an orifice perforated plate 27 is provided on the extended surface of the baffle plate 24 in the lower gas passage 14.
is installed. This orifice porous plate 27 is for ensuring uniform gas flow in a cross section parallel to the lower catalyst receiver of each reaction chamber, and is located at the center of the lower gas passage 14 on the extended surface of the baffle plate 24. It is best to install it on the entire surface of the cross section perpendicular to the axis. Further, for the same purpose, a perforated plate 28 can be installed between the upper surface of the reaction chamber and the lower catalyst receiver.

This porous plate 28 is preferably installed over the entire surface of the cross section parallel to the catalyst receiver of the reaction chamber. Since the catalyst used in the reactor of this invention is often small particles, this perforated plate 2
No. 8 installation causes little inconvenience in charging and discharging the catalyst. The reactor of this example can also be used as a single reaction chamber reactor without installing the baffle plate 24 and the orifice plate 27. In this case, the gas outlet 22
Instead, a gas outlet 23 (indicated by a dotted line) may be installed on the lower surface of the outer shell 1.

In the examples shown in Figures 1 and 2, the reaction chamber and the upper gas passage are divided into two in the direction of the central axis, and the raw material gas is introduced from the upper part of the outer shell of one of the small reaction chambers. It is also possible to divide the reaction chamber into two by a baffle plate (not shown) that partitions the reaction chamber and the lower gas passage in the direction of the central axis.

In this case, both the gas inlet and outlet would be installed at the lower part of the outer shell where the small reaction chambers 8a and 8b are located, but they are not shown for ease of understanding. When dividing the reaction chamber into three or more small reaction chambers, a baffle plate that divides the reaction chamber and the lower gas passage in the direction of the central axis and a baffle plate that divides the reaction chamber and the upper gas passage in the direction of the central axis are used. baffle plates may be installed alternately, but these are not shown because they are easily understood. When the reaction chamber 8 is divided into two or more small reaction chambers in this way, gas is made to flow through these small reaction chambers in series.

Therefore, whether the gas outlet 22 has an even number of small reaction chambers or
Alternatively, depending on whether the number is odd, it will be placed at the top or bottom of the shell. When the raw material gas port 21 is installed in the lower part of the outer shell, the above relationship regarding the gas inlet and gas outlet is reversed. In addition, both side walls of the reaction chamber 4 d3
In order to maintain the pressure in the space 29 between the walls 4 and 5 and the side of the outer shell at approximately the same pressure as the pressure in the reaction chamber, small pressure equalizing holes 30 are installed in the side walls 4 and 5 of the reaction chamber, respectively. is preferred.

For the same purpose, the two joining lines that join the side wall 4 and the outer shell 1 and the two joining lines that join the side wall 5 and the outer shell 1 are not entirely welded, and the parts that are not welded are It is also possible to omit the pressure equalizing hole 30 by allowing some gas to flow between the rain space 29 and the upper or lower gas passage. Further, the coolant that is allowed to flow inside the cooling pipe will be described later.

Next, the advantages of this inventive reactor will be described. In the reactor according to the invention, each cold Ml tube makes an angle of 45 degrees or less with the horizontal. Therefore, the catalyst introduced from the catalyst inlet 25 passes through the gap between the adjacent cold Lj pipes and is filled into the reaction chamber. Therefore, the shortest distance, that is, the gap size between the outer peripheries of adjacent cooling pipes in the direction perpendicular to the length direction of the cooling pipes, is Merging pipe 17a
By reducing or eliminating the gap between the outer peripheries of each of the adjacent particles, the size can be reduced to several times the diameter or length of the catalyst particles, that is, about 6 to 15 mm. As a result, if the reactor of this invention is used, even if the calorific value per unit volume of the catalyst is very large and it is necessary to install a large number of cooling pipes in the reaction chamber, there will be no problem. It is possible to fill the catalyst without having to use it. This point is explained in the above-mentioned Japanese Patent Application Laid-Open No. 55-149640 and U.S. Pat.
This is an improvement over the reactor proposed in No. 321234. That is, in the reactor proposed last time, since the cooling pipes are installed vertically, when charging and discharging the catalyst, the catalysts are placed adjacent to each other in the secondary branch pipe 16c and the primary merging pipe 1.
It is necessary to be able to freely pass through the gap 7a from top to bottom. When the gap between the lj pipes is shortened to 15 mm and covered, the gap between adjacent secondary flow branch pipes 16c and primary merging pipes 17a becomes 6 pipes or less, and the catalysts are placed next to each other. It becomes difficult to freely pass through the gap of 6 mm or less in the L distribution flow pipe or the merging pipe, making it difficult to charge and discharge the catalyst in a practical sense. Therefore, in the reactor proposed last time, the gap size between adjacent cooling pipes is 15W.
It is difficult to perform the following spells, and as a result, the touch fi
Installation of a heat transfer area of 60 m per "1 m" is approximately the maximum amount of heat transfer area installed. On the other hand, in the case of the reactor according to the present invention, the gap size between adjacent cooling pipes is 6 mm.
Since the reactor of this invention can be shortened to 200 m per 1 Tl'1'' of catalyst,
This makes it suitable for reactions that generate a large amount of heat per unit volume of catalyst. This is the first advantage of the reactor of this invention.

On the other hand, when using this type of reactor and directly recovering the reaction heat as high-pressure vapor of the cooling liquid and effectively utilizing it for purposes such as generating dynamic gas, the pressure on the cooling liquid side generally increases. Since the pressure is higher than the pressure on the reaction gas side, in a reactor in which the catalyst is filled in the duplex and the cooling liquid is passed through the shell side as in the conventional method, as a natural result, the reactor outer shell has a thick wall. However, in the reactor of this invention, the cooling liquid flows inside the cooling tube, so the wall thickness of the reactor outer shell can be reduced, and the weight of the entire reactor can be reduced. It is possible to say 1-. This is the second advantage of the reactor of this invention. In other words, in conventional reactors, in order to reduce the pressure horn on the cooling liquid side, in order to use a thin outer shell,
In cases where it is difficult to use an organic liquid with a high boiling point as the coolant because the reaction is an oxidation reaction and the gas contains oxidizing components such as oxygen, which increases the risk of fire. , the above-mentioned second advantage of the invention is particularly important.

Also, in this reactor, if the baffle plate 24 is not installed and there is only one reaction chamber, the arrangement density of cooling pipes in the reaction chamber should be adjusted as in the case of the reactor proposed last time. By changing and adjusting the temperature along the gas flow direction, the temperature distribution of the catalyst layer along the gas flow direction can be formed into a desired temperature distribution. That is, in FIG. 2A, when the raw material gas flows in from the upper inlet 21 and flows out to the lower produced gas outlet 23, the arrangement density of the cooling pipes on the cross section perpendicular to the central axis in the reaction chamber 8 is In terms of the diameter of the cooling pipes used, for example, a large number of cooling pipes with a small diameter are arranged closely in the upper part, and cooling pipes with a large diameter are arranged loosely in the lower part, or vice versa. , the temperature distribution along the gas flow direction within the catalyst layer can be formed into a desired temperature distribution. Even on this point a3, the reactor of this invention has substantially the same function as the reactor proposed previously. This is the third advantage of the reactor of this invention.

There are many embodiments of this invention, both in the construction and method of use of the reactor, and some of these many embodiments are used below to provide a more detailed description of the inventive reactor and its use. However, the invention is not limited to the embodiments described herein. In the following description of embodiments other than the above, the points that differ from those shown in FIGS. 1 and 2 in terms of structure and usage will be mainly explained. It is possible to use the reaction chamber as just one reaction chamber without installing the baffle plate shown in , or conversely it is also possible to divide it into two or more small reaction chambers, but regarding this point. has already been described. Although the catalyst holding net 7 at the top of the reaction is not absolutely necessary, it is preferable to use it when the reactor is installed not horizontally but in an inclined position.

FIG. 3 shows a branching structure and a merging structure in which a large number of rectangular tube sheets 20a and a cross section perpendicular to the longitudinal direction are semicircular, and the same number of tube sheet covers 20b are sealed at both ends with semicircular plates.
IC partition wall 1 is installed over the entire cross section perpendicular to the central axis of the reactor in the vicinity of both ends of the reactor where these branching structures and merging structures are installed.
1 and 12 separate the header chambers 9 and 10 from the reaction chamber 8, and are further installed in positions close to each other.
The reaction chamber 8 is divided into one small gas passage chamber 33 by the baffle plate 24a that partitions the reaction chamber and the upper gas passage in the direction of the central axis, and the baffle plate 24b that partitions the reaction chamber and the lower gas passage in the direction of the central axis. This is a diagram showing an example in which the reaction chamber is divided into three into two small reaction chambers 8a and 8b.

FIG. 4 is a vertical cross-sectional view taken along line C-7C in FIG. 3 in the direction of the arrow. In FIGS. 3 and 4, the coolant supplied from the coolant inlet pipe 18 is divided into a number of connecting pipes 16b in the primary branch pipe 16a, and then communicated with these connecting pipes 16b to form a rectangular shape. In the space surrounded by the tube sheet 20a and the tube sheet cover 20b, the water is divided into a larger number of cooling pipes 15. The coolant confluence structure in this example is approximately symmetrical with the branch flow structure, and each cooling pipe 15
The coolant flowing out from the reactor passes through the reverse path of the above-mentioned split flow and is forced to flow out of the reactor from the coolant outlet 19. The bulkheads 11 and 12 in this example are perforated plates in the form of tube plates, and one tube in each tube passes through the joint holes in these bulkheads. It is desirable that there be a gap between the side partition wall and each cooling pipe that does not allow catalyst particles to pass through, but allows gas to pass through. Hold at a pressure of I can do it. Conversely, if this contact part becomes an airtight contact through which gas can easily pass, a small pressure equalizing hole is formed in the part of the side partition wall where the side partition partitions and covers the header chamber and the upper gas passage or the lower gas passage. It is preferable to provide approximately the same pressure in both header chambers and the reaction chamber. In this example, the gas-permeable catalyst receiver 6a and the gas-permeable catalyst holder 7a are both installed between the partition walls 11 and 12, and both the upper gas passage 13 and the lower gas passage 14 are connected to the header chamber by the side partition walls. It is divided from 9 and 10. As means for dividing the header chambers 9 and 10 from the upper gas passage 13 and the lower gas passage 14, in addition to the above, partition walls are provided on both extending surfaces of the gas permeable catalyst receiver 5aJ5 and the gas permeable catalyst presser 7a in the central axis direction. A partition parallel to the central axis, similar to the gas-impermeable catalyst receiver 6b and the gas-impermeable catalyst holding plate 7b shown in FIG. There is a way to install the board. In this method, the partition walls 11 and 12 partition the header chamber and the reaction chamber, but the upper and lower gas passages are not partitioned, and both the upper and lower gas passages are extended to the rain jackets 2 and 3. Since it is clear that the structure is possible, it is not shown.

When such a means for dividing the header chamber and the reaction chamber is used, the pressure equalizing small hole is installed in a partition plate parallel to the central axis. As in the examples in Figures 3 and 4,
By separating the header chamber from the reaction chamber, the catalyst particles introduced from the catalyst inlet 25a will not flow into the header chamber at all, and there is no need to consider the lack of heat transfer area in the header chamber d3 as a problem. It disappears. However, even in this case, it is desirable to fill the header chamber with particulate material that does not have a catalytic effect, and this particulate material can be easily filled by providing an inlet 25c and an outlet 26c.

In the examples shown in FIGS. 3 and 4, a baffle plate 24-a, J5J, is located near the center of the reaction chamber 8 in the direction of the center axis, and partitions the upper gas passage and the reaction chamber in the direction of the center axis. Baffle board 2
A baffle plate 24b is installed adjacent to 4a to partition the reaction chamber and the lower gas passage in the direction of the central axis, so that the reaction chamber 8 can be used as a gas passage without being filled with two small reaction chambers F3a, 3b and a catalyst. It is divided into three gas passage small chambers 33.

Also, at the same time as this three-division, the upper gas passage 13 is divided into three parts by the baffle plate 2'.
4a into the two upper gas passages 13a and 131), and similarly, the lower gas passage 14 is connected to the two lower gas passages 14. by the baffle plate 24b. It is divided into a and 14b. This example has the above-mentioned reaction chamber structure.No matter which one of the two small reaction chambers 8a and 8b is located in d''3, it forms a series gas passage that allows gas to flow from top to bottom. In other words, the raw material gas supplied from the gas population 21 is
As shown by the arrow, it passes through the small reaction chamber 8a from top to bottom, flows out into the lower gas passage 14a, and then flows from the lower gas passage 1/4a through the gas passage small chamber 33 to the upper gas passage 1.
31), further passes through the small reaction chamber 8b from top to bottom again, passes through the lower gas passage 14b, and flows out of the reactor from the gas outlet 22. By using the above-mentioned gas passage path, it becomes unnecessary to install the gas permeable catalyst holder 7a when the reactor is installed substantially horizontally. When installing the reactor at an angle of 15 to 45 degrees with respect to the horizontal, it is necessary to install the gas permeable catalyst holder 7a even if the above gas passage path is used. There is no need to firmly fix it. Conversely, when this gas-permeable catalyst holder 7b is firmly fixed to the outer shell or the partition walls 11 and 12, etc., the mutual positional relationship between the two face plates 24a and 24b is adjusted and the gas inlet and gas outlet are connected to the lower part of the outer shell. Even if the reactor is installed on an incline, gas can be made to flow from bottom to top in each small reaction chamber. The example shown in FIGS. 3 and 4 includes one baffle plate 24a that partitions the upper gas passage and the reaction chamber in the central axis direction, and one baffle plate that partitions the reaction chamber and the lower gas passage in the central axis direction. By using one set of baffle plates consisting of one piece of 24b,
This was an example in which the reaction chamber 8 was divided into a 2g small reaction chamber and one gas passage small chamber, but two or more sets of these baffle plate sets were installed inside the outer shell using the same method as above. By doing so,
The reaction chamber 8 is divided into three or more small reaction chambers and two or more small gas passage chambers, and gas is supplied to each small reaction chamber in series, and in any of the small reaction chambers, from top to bottom, or It can be made to flow in the same direction from bottom to top. The existence of such an embodiment can be easily understood from the examples shown in FIGS. 3 and 4, although it is not shown. In addition, 3 in Figure 3
1 has manhole C.

Figure 5 shows the short l1lj shown in Figures 3 and 4 above.
There is an enlarged view Q showing an example of the interconnection method of the tubular plates 20a. That is, the strip-shaped tube sheets 20a adjacent to each other in the vertical direction have a plurality of female threaded holes at approximately the same positions on the vertically opposing surfaces of the tube sheets, and special bolts as shown in the figure are inserted into these female threaded holes. It is screwed in to connect and cover both tube plates. The tube sheets interconnected by this method are fixed to the outer shell 1 by fixing between the tube sheets and the protrusion 35 installed at the relevant position inside the outer shell (Figs. 3 and 4). This is achieved by using a method similar to that described above.

FIG. 6 shows another embodiment of the coolant branching structure and merging structure in J5. In this example, since these branching structures and merging structures are installed symmetrically with respect to the direction of the central axis, only the branching structures are illustrated. In FIG. 6, both ends of a large number of cooling pipes 15 are each connected to one tube plate 20a, and one tube plate is connected to each of the tube plates 20a.
Hemispherical tube sheet covers 20b are attached. In this example, these two tube sheets 20a each correspond to the partition wall 11.
Alternatively, it also serves as 12 and two tube plate covers 20.
b also serves as M2 or M3 at both ends of the outer shell, respectively.

Therefore, the coolant flowing from the coolant pipe 118 flows into the space surrounded by the tube plate cover 20b and the tube plate 20a, and then is directly branched into each cooling pipe 15. In the merging structure, the coolant flows in the reverse order. , flows out of the reactor from the coolant outlet 19. Also, in this example, as mentioned above, both ends of the reactor are
Since there is a single tube sheet cover that also serves as a lid, the internal volume of the space surrounded by the tube sheet cover 20b and the tube sheet 20a is large, and the thickness of the lid is thinner than in the embodiment described above. Although the size is large, the structure of the one-way valve flow section and the confluence section is significantly simpler.
In addition, it has the above-mentioned advantage that the cylindrical portion of the reactor shell has a good wall thickness.

FIG. 7 shows another embodiment in which the branching structure and the merging structure are structurally different. In this example, both the branching structure and the merging structure consist of one tube sheet and a large number of strip-shaped tube sheet covers substantially similar to those described above in their main structure. FIG. 7A is a sectional view taken along the line A-A in FIG. 7, and FIG. 7B is an enlarged view showing the joint of the tube sheet 20a, the cooling pipe 15, and the tube sheet cover 20b. . That is, both ends of one tube 15 are respectively fixed to a tube sheet 20a, and a number of tube sheet covers 20b are attached to this tube sheet 20a as shown in the figure. The tube plate cover 20b covers the connecting pipe 1
6b or 17b communicates with the primary branch pipe 16a or the secondary merging pipe 17G, respectively. The coolant supplied from the coolant inlet 18 is transferred to the primary branch pipe 16
At point a, the water is divided into a large number of connecting pipes 16b, and further into a large number of cooling pipes 15. The coolant flowing out of the cooling pipe first joins the connecting pipe 17b, and then flows into the secondary joining pipe 17c.
The coolant is further merged at , and flows out of the reactor from the coolant outlet 19 . The small hole 30 in the tube sheet 20a is the pressure equalizing hole described above. In this example, since both sides of the tube plate 20a have substantially the same pressure, the tube plate may be relatively thin, and both the branching structure and the merging structure have relatively simple structures. Also in this example, the tube plate 20a has a structure that also serves as the partition walls 11 and 12.

The reactor according to the present invention has a catalyst inlet 25 that passes through the upper part of the outer shell and reaches the upper surface of the reaction chamber, and a catalyst outlet that passes through the lower catalyst receiver 6 of the reaction chamber and the lower part of the outer shell and reaches the outside of the outer shell. 26
, it is possible to charge or discharge the catalyst. When the reaction chamber is divided into a plurality of small reaction chambers, each small reaction chamber requires at least one inlet and one outlet for the catalyst. The cooling tube used in the reactor of this invention can have a large diameter, but when used for a reaction that generates a large amount of heat as described above, it is necessary to In order to arrange a large heat transfer area, the outer diameter is 10 to 50 mm.
It is preferable to use +++n+ later. In the arrangement of the cooling pipes, the distance between the outer peripheries of adjacent cooling pipes, and the distance in the direction perpendicular to the longitudinal direction, is preferably selected between 6 and 50 cylinders. However, it is not necessary to make the outer diameters of these cold fJ tubes or the intervals between the outer circumferences the same, and in order to form a desired temperature distribution in the reaction chamber, cooling tubes with different outer diameters may be used in one reactor. Spacing between the tubes and different circumferences can be employed.

In each of the embodiments described above, in order to ensure that the gas flows uniformly within the reaction chamber, at least one perforated plate is provided between the upper surface of the reaction chamber and the lower catalyst receiver, or the gas As in the case of Fig. 1, a perforated plate that functions as an orifice is installed on the extension of the baffle plate that goes into the gas passage when moving from one small reaction chamber to the next small reaction chamber. It is valid.

In each of the above embodiments, the header chamber J3 and the housing portions of the branching structure and merging structure in the reaction chamber that occur when the header chamber is not partitioned often lead to a lack of heat transfer area. In order to prevent the flow of the raw material gas or the gas during the reaction, it is desirable to fill it with particulate material that does not have a catalytic effect and has strong resistance to the flow of gas (this is also the same as above). In each of the embodiments described above, the structure of the reaction chamber 81S and the gas flow system described above can be applied.

When using the reactor of the present invention, the fluid that should be allowed to flow through the cooling pipe should preferably be one that does not corrode the constituent materials of the reactor, and there are no other special restrictions. However, when carrying out a reaction due to the heat of reaction, the coolant may be water, aliphatic saturated hydrocarbons with a boiling point of 100 to 350°C, chlorinated aromatic hydrocarbons, alkylnaphthalenes, alkylbenzenes, It is preferred to use a mixture of diphenyl oxide and diphenyl, and a mixture or molten salt of at least two selected from these. Also, for the above-mentioned molten salt, those with various known compositions can be used, but two or three types selected from the group consisting of potassium nitrate, sodium nitrate, and sodium nitrite are preferred because they have a low melting point and are easy to use. Mention may be made of mixtures of species. An example of such a molten salt is a mixture consisting of 53% potassium nitrate, 7% sodium nitrate and 40% sodium nitrite (all □□□% by weight).

When using the above coolant, the reaction temperature should be 350-38
If the temperature is 0'C or higher, use a molten salt, and if the temperature is below this temperature, use a substance other than the molten salt listed above, i.e., a substance with a melting point of 12°C or less and which is liquid at room temperature. It is most preferable to use In addition, the above liquid coolants other than molten salt can be boiled under pressureff! ! It is preferable that the liquid is supplied to the coolant inlet as a liquid at a certain temperature and, after absorbing the heat of reaction, is allowed to flow out of the coolant outlet as vapor at the pressure or a mixed phase of vapor and high temperature liquid. Steam and liquid
When the phase substance is obtained from the coolant outlet of the reactor, the vapor and liquid components are separated in a separator installed outside the reactor, and only the liquid valve is obtained as a liquid at the boiling temperature under the pressure. , it is better to be returned to the reactor coolant population. Whether the vapor is separated in the separator mentioned above or obtained from the coolant outlet, it can be used in other processes (for heating purposes). It can be used as a heat source or for power generation.When using a molten salt as a coolant, the molten salt at a relatively low temperature is supplied to the coolant inlet, and after absorbing the reaction heat, it is heated to a higher temperature. It will flow out of the reactor from the coolant outlet as a molten salt at a high temperature.When using the above liquid cooling agent (11) other than the molten salt, use one of these coolants with a high boiling point. As a result, the pressure inside the cold M1 tube can be lowered, allowing the use of thinner cooling tubes, reducing the weight of the reactor, and making it easier to manufacture. In this case, high temperature but low pressure coolant vapor is obtained from the coolant outlet or the separator described above. However, from the viewpoint of effective use of reaction heat, coolant vapor with high temperature but low pressure and high-temperature molten salt are both effective for heating other substances, but they are This is disadvantageous when the occurrence of Therefore, since the reaction temperature is 250°C or higher, a coolant with a boiling point of 150°C or higher was used as a coolant, and a high temperature but low pressure coolant vapor or a mixed phase of vapor and liquid was obtained. In this case, when molten salt is used, heat is exchanged between water and the steam, mixture, or molten salt in a heat exchanger installed separately outside the reactor, and the vapor or molten salt is heated. Thermal energy can be converted into high-temperature, high-pressure water vapor. If the high-temperature, high-pressure steam obtained by this method is introduced into a turbine with or without overheating, the heat of reaction can be efficiently converted into power. When the above-mentioned heat exchanger outside the reactor is used, the cold 7JI liquid produced by condensation of the vapor of the cooling liquid in the heat exchanger outside the reactor or the molten salt after the temperature has been lowered is transferred to this heat exchanger without being further cooled. It may be returned to the coolant inlet of the reactor.

When a substance that is liquid in the state when it is supplied to the coolant inlet is used as the coolant for the reactor of this invention, and the reactor is used at an angle, it is necessary to Preferably, the coolant is directed toward a coolant outlet located at the outlet. In this invention, it is disadvantageous to use molten salt under high pressure, and even when using cold 7iII liquid other than molten salt, the pressure of the cooling liquid is 200 kg/cy#G or more. It is better to avoid this because it makes it difficult to separate the vapor and liquid components in the cooling pipe or in the separator.

When using this reactor, the raw material gas is preferably preheated to the operating temperature of the catalyst used before being introduced into the reaction chamber. As a method for this preheating, it is also possible to use a method of heating one raw gas with another heat source, but the high temperature generated gas flowing out of the reactor and the raw material gas are heated using a heat source installed outside the reactor. A method of exchanging heat in an exchanger is desirable.

As for the material for manufacturing the reactor of this invention, any material can be used as long as it has sufficient performance in terms of strength and corrosion resistance.

Examples of such materials include -C1 carbon steel, low alloy steel, and stainless steel.

The reactor of this invention is useful for gas reactions that generate heat of 150,000 Kcaf/hour or more per catalyst charged in the reaction chamber. Such reactions include (1) oxidation of ethylene with an oxygen-containing gas to produce ethylene oxide; (2) oxidation of ethylene with an oxygen-containing gas to produce ethylene oxide;
- Reaction to produce aldehyde, (3) Reaction to oxidize propylene with oxygen-containing gas to produce acrolein, (4) Reaction to oxidize propylene with oxygen-containing gas to produce noacrylic acid, (5) Reaction to produce noacrylic acid by oxidizing propylene with oxygen-containing gas, (5) Reaction to produce noacrylic acid by oxidizing propylene with oxygen-containing gas. (6) A reaction in which a mixture of propylene and ammonia is oxidized with an oxygen-containing gas to produce acryloni-1. (7) Methanol vapor is oxidized with an oxygen-containing gas to produce acryloni-1. oxidized by
Reaction to produce formaldehyde, (8) Reaction to produce maleic anhydride by oxidizing benzene vapor with oxygen-containing gas, (9) Oxidizing naphthalene or ortho-xylene vapor with oxygen-containing gas to produce phthalic anhydride. Reaction, (10) oxidizing butene-1, butene-2, n-butane or butadiene-1,3 with an oxygen-containing gas,
There are reactions to produce maleic anhydride, etc.

[Brief explanation of the drawing]

Fig. 1 is a vertical sectional view of an example of the reactor of the present invention, Fig. 2A is a vertical sectional view taken in the direction of arrow d51 at the position A-△ of the reactor in Fig. 1, and Fig. 2B is a vertical sectional view of an example of the reactor of the present invention. , FIG. 1 is a vertical sectional view taken in the direction of arrow B-8 of the reactor, FIG. 3 is a vertical sectional view of another example of the reactor of the present invention, and FIG. A vertical cross-sectional view in the direction of arrow t taken at position C, FIG. 5 is an enlarged view of the central part of the tube plate in FIG. 3, and FIG.
FIG. 7 is a vertical sectional view of another example of the reactor of this invention; FIG. 7A is a vertical sectional view of another example of the reactor of this invention; FIG. FIG. 7B is an enlarged view of the central portion of the tube plate in FIG. 7, and both are schematic drawings. Symbol 1・・・・・・・・・Reactor outer shell 2.3・・・・・・Lids on both ends of reactor 4.5・・・
...Reaction chamber side wall 6...Catalyst receiver 6a...Gas permeable catalyst receiver 6b...
......Cast-impermeable catalyst receiver 7...
... Catalyst holding net 7a ... Catalyst holding net 7b ...
......Catalyst holding plate 8...Reaction chambers 8a, 8b...Small reaction chamber 9.10......Herater to 11. 12... Partition walls 13.13a, 13b -- Upper waste passage 14.14
a, 14b - lower gas passage 15...
・Cooling pipe 16......Diversion structure 16a...Primary distribution pipe 16b...
...... Connecting pipe 16c ...... Secondary branch pipe 17 ...
... Merging structure 17a ... Primary joining pipe 17b ...
...... Connecting pipe 17C ...... Secondary confluence pipe 18 ...... Coolant population 19 ...... Coolant outlet 20a...Tube sheet 20b...Tube sheet cover 21 with a circular cross-sectional shape...Gas inlet 22... ...Gas output 1" 23 ...... Dregs outlet 24.24a, 24b -- Baffle plate 25.25a, 25b -- Catalyst inlet 25C125
d...Particulate matter inlet 26.26a, 26b
, --Catalyst outlet 26C, 26d... Particulate matter outlet 27... Orifice porous plate 28
・・・・・・・・・・・・Perforated plate 29・・・・・・・・・Space 30・・・・・・・・・Pressure equalization small hole 31・・・・・・・・・・・・Manhole 32...Special bolt 33...Gas passage manual 34...
... Vibration damping perforated plate 35 ... Protrusion Applicant Toyo Engineering Co., Ltd. Figure 2A Figure 2B Figure 4 Figure 5 Figure 7A Figure 7B

Claims (1)

[Scope of Claims] (1) In a cylindrical shell with lids at both ends and a central axis inclined at an angle of 45 degrees or less with respect to the horizontal direction, wet traces during reaction and raw materials that are gaseous under pressure. A reactor for a catalytic reaction which produces a product which is gaseous under the temperature and pressure during the reaction by contacting a granular catalyst, the reactor comprising: (1) a cross-section perpendicular to the central axis on the inside of the outer shell; A prismatic cylindrical reaction chamber for catalyst filling is installed, which is square or rectangular, and all four vertices of the square or rectangle are in contact with the outer shell; The two opposing faces parallel to the central axis are substantially perpendicular and serve as gas-impermeable side walls, and at least a portion of the prismatic cylindrical reaction bottom surface excluding a portion close to the raincoat is gas-permeable. (1) The space surrounded by the upper surface of the reaction chamber and the upper part of the outer shell is an upper gas passage; (2) The space surrounded by the lower surface of the reaction chamber and the lower part of the outer shell is a lower gas passage; A large number of cooling pipes parallel to the central axis are installed in the reaction chamber to allow the coolant to flow, and one end of each cooling pipe passes through one of the lids to the outside of the outer shell. (1) communicate with the coolant inlet pipe extending from the inlet pipe into the outer shell via a dividing structure for dividing the coolant supplied by the inlet pipe into each of the cooling pipes; The other end is the cold 7J in each cooling pipe.
A coolant outlet pipe that passes through a confluence structure for merging the I agent, passes through another one of the reagents, and reaches the outside of the outer shell, and allows the coolant after the merge to flow out of the outer shell. (1) An inlet for the raw material gas is installed in the outer shell part that contacts a part of one of the gas passages, and an inlet for the raw material gas is installed in the outer shell part that contacts a desired other part of both the waste passages. A reactor characterized in that an outlet for reaction product gas is installed. (2) installed substantially perpendicular to the central axis, dividing the reaction chamber and the lower gas passageway or the reaction chamber and the upper gas passageway into two in the direction of the central axis in a cross section perpendicular to the central axis; The reactor according to claim 1, wherein the reaction chamber is divided into two small reaction chambers by one baffle plate. (3) A baffle plate installed substantially perpendicular to the central axis and partitioning the reaction chamber and the lower gas passage in the direction of the central axis in a cross section perpendicular to the central axis, and a reaction chamber formed in the same cross section. The reaction according to the claims, wherein the reaction chamber is divided into a desired number of small chambers and small reaction chambers by alternately installing at least one baffle plate that partitions the upper gas passage in the direction of the central axis. vessel. (4) The reactor according to claim 1, wherein a portion of the lower surface of the reaction chamber near the raincoat is a gas-impermeable catalyst receiver. (5) The reactor according to claim 1, wherein a catalyst holding plate is installed on the upper surface of the reaction chamber near the rain jacket, and a catalyst holding net is installed on the other upper surface of the reaction chamber. (6) One header chamber each accommodating the branching structure or the merging structure and located at both ends in the outer shell by end partition walls installed near both ends in the outer shell, The reactor according to claim 1, 2, or 3, which is partitioned from the reaction chamber and both gas passages. (7) A portion of the both end partition walls that partitions the header chamber and both gas passages is gas-impermeable and has a small hole that allows communication between one of the gas passages and the header chamber. 6. The reactor (8) according to claim 6, which is made of a flexible material. The reactor (8) according to claim 6, wherein the collective structure and the branch structure are constituted by tubular members having a circular and/or angular cross-sectional shape. A reactor according to scope 1. (9) Of the collective structure and/or the branch structure,
The main structure of the part to be joined to each cooling@end is at least one. 2. The reactor according to claim 1, comprising a tube sheet and at least one plate cover having a semicircular shape in a cross section perpendicular to the longitudinal direction. (10) At least one catalyst supply port that communicates between the upper part of the outside of the outer shell and the upper part of the reaction chamber, and at least one catalyst outlet that allows the lower part of the reaction chamber to communicate with the lower part of the outside of the outer shell. (11) In the arrangement of cold IJ pipes in the reaction chamber, the shortest distance between outer circumferences of adjacent cooling pipes in a cross section perpendicular to the central axis is 6 to 6. The reactor according to claim 1, wherein the reactor is set to a desired value that is not necessarily equal within a range of 50 mm. (12) The outer diameter of the cooling pipe is not necessarily equal.
50n+n+. (13) 11 between the lower surface catalyst receiver of the reaction chamber and the upper surface of the reaction chamber.
2. The reactor according to claim 1, wherein at least one perforated plate is installed parallel to the lower catalyst receiver so that the gas flow is uniformly distributed in a cross section parallel to the lower catalyst receiver. (14) In the upper gas passage and/or lower gas passage corresponding to the passage through which the gas moves from one small reaction chamber to the next small reaction chamber, on the extended surface of the baffle plate that partitions these two-handed reaction chambers. The reactor according to claim 2 or 3, wherein an orifice perforated plate is installed in the reactor. (15) When a tubular structure according to claim 8 is used as the merging structure and/or the dividing structure, in the mutual positional relationship of the tubular members directly connected to the cooling pipe. 9. The reactor according to claim 8, wherein the reactors are arranged alternately at different positions in the direction of the central axis, with the ones closest to each other in the distance between the outer surfaces in the direction perpendicular to the central axis. (16) Particulate matter having no catalytic action and having poor air permeability than the catalyst is filled in a portion of the reaction chamber space where the branching structure and the merging structure are installed. Reactor as described. (17) The reactor according to claim 6, wherein the header chamber is filled with particulate material having no catalytic action. (18) The reactor according to claim 1, wherein a supply port and a discharge port for the non-catalytic particulate material communicating with the outside of the shell are installed in the upper and lower portions of the header chamber, respectively. (19) In a cylindrical shell with lids at both ends and a central axis inclined at 45 degrees or less with respect to the horizontal direction, the raw material, which is gaseous at the temperature and pressure during the reaction, is brought into contact with the granular catalyst. A reactor for a catalytic reaction that produces a product that is gaseous at a temperature and pressure of A rectangular cylindrical reaction chamber for catalyst filling is installed in which the four vertices of the square or rectangle are all in contact with the outer shell; The two opposing faces are substantially perpendicular and serve as gas-impermeable side walls, and at least a portion of the lower surface of the prismatic cylindrical reaction chamber, excluding a portion close to the rain jacket, serves as a gas-permeable catalyst receiver; The space surrounded by the upper surface of the reaction chamber and the upper part of the outer shell is an upper gas passage; (1) the space surrounded by the lower surface of the reaction chamber and the lower part of the outer shell is a lower gas passage; (2) Inside the reaction chamber, A number of cooling pipes are installed parallel to the central axis for circulating the coolant, and one end of each cooling pipe passes through one of the lids from outside the shell into the shell. (1) The other end of each cooling pipe is connected to the coolant inlet pipe through a dividing structure for dividing the coolant supplied by the inlet pipe into each of the cooling pipes; Through a merging structure for merging the coolant in the cooling pipe, passing through another lid to reach the outside of the outer shell, and allowing the coolant after merging to flow out of the outer shell. (1) An inlet for the raw material gas is installed in the outer shell part that contacts a part of one of the two gas passages, and is in contact with another desired part of the two gas passages. In a method of using a reactor in which an outlet for reaction product gas is installed in the outer shell portion, the coolant supplied into the cooling pipe is a molten salt, a substance that is liquid at 12° C. or higher, under a desired pressure. A method of using the reactor, characterized in that the flowing liquid is a mixed phase of vapor of the liquid and the liquid at a high temperature. (20) The method according to claim 19, wherein when the coolant other than the molten salt is supplied to the branching structure, the liquid C at a temperature abbreviated to "a" under the pressure is used. (21) The coolant other than the molten salt is water, and the boiling point is 100
~350°C aliphatic saturated hydrocarbons, chlorinated aromatic hydrocarbons, a mixture of diphenyl oxide and diphenyl, alkylbenzenes, alkylnaphthalenes, or a mixture of at least two compounds selected from these. Scope of Use as described in Item 19. (22) The molten salt is potassium nitrate, puttrium nitrate J5
20. The method according to claim 19, which is a mixture of two or three selected from the group consisting of: and sodium nitrite. (23) When a coolant having a boiling point of 150° C. or higher is used among the coolants set forth in claim 21, and when the molten salt coolant set forth in claim 19 is used, The vapor of the former coolant flowing out from the coolant outlet pipe, the mixed phase product of the former, or the molten salt of the latter are heat exchanged with water under pressure in a heat exchanger separately installed outside the reactor. , water vapor is generated, and the vapor of the former cooling liquid or the vapor in the mixed phase substance is condensed by the heat exchange, and the former cooling liquid or the molten salt after the temperature is lowered is transferred to the cold N1 agent inlet. 20. The method of claim 19, wherein the method is recycled back into the pipe. (24) The method according to claim 21, wherein the pressure of the cooling liquid is 200 Kg/cnrG or less. (25) A baffle plate that is installed substantially perpendicular to the central axis and partitions the reaction chamber and the lower gas passage in the direction of the central axis in a cross section perpendicular to the central axis, and the reaction chamber and the lower gas passage in the same cross section. In the reaction chamber, the reaction chamber is divided into a desired number of small reaction chambers by alternately installing at least one baffle plate that partitions the upper waste passage in the direction of the central axis. 20. The method according to claim 19, wherein the small reaction chambers are made to flow in series. (26) The baffle plate partitions the reaction chamber and the lower gas passage in the direction of the center axis in a cross section perpendicular to the center axis, and the baffle plate partitions the reaction chamber and the upper gas passage in the same cross section in the direction of the center axis. At least one set of baffle plates installed in adjacent positions allows the reaction chamber to be connected to at least one of the small gas passage chambers between the two baffle plates located in close proximity to each other. and divided into at least two small reaction chambers,
The gas is made to flow through the small reaction chambers and the small chambers in alternating series, and in each of the small reaction chambers, it is made to flow in the same direction from top to bottom or from bottom to top. Usage as described in Section 19. (27) The method according to claim 19, wherein the raw material gas is preheated to a desired temperature before flowing into the reaction chamber. (28) The reaction is performed at a pressure of 50 kQ/cnfG or less. The use according to claim 19, which is a reaction for synthesizing ethylene oxide from ethylene and oxygen or a mixed gas of oxygen and nitrogen. Claim 27, wherein the preheating is performed by exchanging heat between the high temperature reaction product gas flowing out of the reaction chamber and the raw material gas that has not reached the preheating temperature in a heat exchanger installed outside the reactor. Usage as described in section.