JPS5876134A - Spherical reactor having plural cylindrical reaction chambers and use thereof - Google Patents

Abstract

PURPOSE:To reduce the wall thickness of a pressure resistant outer shell and the height of a reactor, by constituting a container for catalytic reaction of a stock gas under high pressure from a spherical or a long spherical pressure resistant outer shell capable of possessing a specific cylindrical protruded part and two or more reaction chambers formed therein in columnar, cylindrical and a truncated cone shapes. CONSTITUTION:A stock gas entering the reactor of a pressure resistant outer shell 3 from a pipe 1 reaches a space 11 and the inner space 12 of a cylindrical protruded part of the shell 3 and the temp. rise of the shell 3 is prevented. The stock gas is subsequently passed through plural tubes of a heat exchanger 4 to be indirectly heat exchanged with a high temp. reaction product gas issued from a reaction chamber 33 and reaches a cylindrical reaction chamber 31 having a center vertical shaft in a sphere through a preheated space 13 and a pipe 14. Herein, partial catalytic reaction is generated and a high temp. gas reaches a reaction chamber 32 while cooled by cooling pipe 63 between the space 15 and the space 17. In this chamber 32, reaction is further advanced and the high temp. gas enters the reaction chamber 33 while cooled by a cooling pipe 53 to complete the reaction and a high temp. reaction product gas is discharged out of the reactor from a pipe 2 through a tubular space 23 and the shell side of the heat exchanger 4. In addition, in case of a long spherical shell, the length of a central cylindrical part is adjusted to 3/4 or less of the diameter thereof.

Description

DETAILED DESCRIPTION OF THE INVENTION This invention uses a granular fixed bed catalyst under high pressure to
This relates to the improvement of reactors that perform chemical reactions on raw materials to obtain gaseous products.The main purpose of this project is to reduce the thickness of the pressure-resistant outer shell, reduce the weight of the reactor, and reduce the weight of the reactor. By lowering the height of the reactor, the length of the incidental piping can be shortened, and the frame and foundation for installing the reactor can also be made smaller, thereby reducing construction costs.

Production of ammonia by bringing gas under high pressure into contact with a granular fixed bed catalyst bed (hereinafter simply referred to as catalyst) at the operating temperature of the catalyst to carry out a chemical reaction to produce a gaseous product;
There are already many operational examples, with methanol production being a typical example.

Further, a large number of examples of reactors for carrying out such chemical reactions have already been disclosed. In these disclosed examples, the same reactor was divided into seven or more units filled with sb and catalyst in order to cool the catalyst and gas whose temperature rose as a result of the exothermic reaction.

An opening for directly supplying low-temperature raw material gas at a desired location within the reaction chamber or between different reaction chambers, and a heat transfer surface for indirect heat exchange with low-temperature raw material gas or other coolant other than raw material gas are provided. There are many things that are true.

In addition, in these conventional reactors, the shape of the reaction chamber installed inside the reactor and used to fill the catalyst is cylindrical, mainly from the viewpoint of the need for uniform gas distribution within the catalyst layer and ease of manufacturing. or cylindrical shapes are used. Further, as the direction of gas flow in these reaction chambers, axial flow in which gas flows in the axial direction of a column or cylinder, and radial flow in which gas flows in the radial direction are known. Therefore, in conventional reactors, a cylindrical shell with lids at both ends is used as a pressure-resistant shell to accommodate a cylindrical or cylindrical reaction chamber, and examples of pressure-resistant shells other than this cylindrical shape are disclosed. can not see.

The present invention relates to a reactor having a spherical or nearly spherical pressure-resistant shell. When the internal volume is the same and the internal gas pressure is the same, a spherical pressure vessel has a smaller surface area than a cylindrical pressure vessel, and the steel used for the pressure shell is thinner. It is well known that the weight of the pressure-resistant outer shell itself is reduced (about 10 is sufficient in the case of the same inner diameter and the same pressure).

Taking advantage of this fact, spherical tanks are often used as storage tanks for, for example, liquefied petroleum gas.

However, when a spherical shell is used as the outer shell of a pressure-resistant reactor, nothing is known about the manner in which the internal space of the spherical pressure-resistant shell is utilized.

The inventors of this invention arrived at this invention as a result of their studies regarding the use of the internal space of a spherical pressure-resistant shell as a reactor. The content of this invention will be explained in detail below.

The basic feature for using the internal space of the spherical pressure-resistant shell as a reactor in this invention is that at least two cylindrical cylinders are provided in this internal space.

The object of the present invention is to provide a reaction chamber having a truncated conical shape or/and an annular shape formed by a part or all of the outer surface of the truncated cone and a part of the spherical inner surface. This basic feature allows the interior space of the spherical pressure-resistant shell to be used effectively for the reactor, and the weight of the reactor can be reduced compared to conventional cylindrical reactors. First, the basic contents of this invention will be explained with reference to FIG.

FIG. 1 is a schematic sectional view for comparing the surface areas of the spherical outer shell A and the cylindrical outer shell B when three reaction chambers having the same horizontal cross-sectional area are provided. C is a cylindrical reaction chamber for charging a catalyst that is in contact with the inner surface of the spherical reactor A, and is illustrated so as to be common to both outer shells. D is a cylindrical reaction chamber that is in contact with the inner surface of the spherical reactor A on the outside of C, and is provided so that its horizontal cross-sectional area is equal to C.

Dl is a diagram showing a state in which a cylindrical reaction chamber whose internal volume and horizontal cross-sectional area are equal to D is stacked on a reaction chamber C in a cylindrical reactor B. The internal volumes of D and Dl are smaller than C. E is a cylindrical reaction chamber provided outside D so as to be in contact with the inner surface of the spherical reactor A so that its horizontal cross-sectional area is equal to C and D. El shows a state in which a cylindrical reaction chamber whose internal volume and horizontal cross-sectional area are equal to E is stacked on top of the reaction chamber D1 in the cylindrical reactor B.

The volumes of E and El are smaller than D and Dl.

The above-mentioned spherical reactor A and cylindrical reactor B can be filled with the same volume of catalyst, and in the spherical reactor, the raw material gas is axially oriented O-+D→E or g-+D→C.
If the gas passes through the reactors C2D and E, the linear velocity when the gas passes through the cylindrical reactor B is equal to the linear velocity when the gas passes through the cylindrical reactor B in the axial direction. That is, it has remarkable performance both in terms of catalyst amount and pressure loss during gas passage. Attach well-known lids to the top and bottom ends of cylindrical reactor B (hemispherical in Figure 1), and calculate the surface areas of both reactors using a well-known method.The surface area of spherical reactor A is then The surface area of cylindrical reactor B is significantly smaller. When high-pressure gas at the same pressure exists in both reactors, the weight of the pressure-resistant outer shell of both reactors is the same as that of the outer shell of the spherical reactor, even when considering the installation of a cooling device described below between the reaction chambers. can be made smaller than the outer shell of a cylindrical reactor by about 1/θ to 2θ or more. This weight reduction of the pressure-resistant shell is achieved by reducing the wall thickness required for the pressure-resistant shell, but in large reactors, the size of the reactor makes it difficult to manufacture the steel material used for the shell. May be limited by upper wall thickness,
A reduction in wall thickness means that such limitations can be avoided.

The above is a detailed explanation of this invention. In the present invention, a truncated conical or annular truncated conical reaction chamber, which is not used in conventional cylindrical reactors, can also be used, but this will be described later. In addition, there are two types of chemical reactions that can be carried out in this reactor: an exothermic reaction and an endothermic reaction. There is no fundamental difference in the reactions, and the following explanation can also be applied to endothermic reactions by reversing the temperature relationships other than the preheating of the raw material gas, such as replacing cooling in exothermic reactions with heating in endothermic reactions. Usually, inside the reactor, there is a chamber other than the above-mentioned reaction chamber to cool the catalyst or gas whose temperature has increased as a result of the reaction to the desired temperature, and to preheat the raw material gas supplied to the reactor to the operating temperature of the catalyst. equipment is required to do so.

The first method for cooling the catalyst and high-temperature gas inside these reactors is to supply the low-temperature raw material gas to a desired location within the catalyst layer or upstream of the partitioned catalyst layer (i.e., reaction chamber). There is a method of supplying the gas directly to the intermediate gas path with the subsequent downstream one. The first method for achieving the same purpose is to install a heat transfer surface for indirect heat exchange in the space between the upstream side of the catalyst bed or the partitioned reaction chamber and the downstream side of the row wall. However, there is a method of exchanging heat between a catalyst or gas at a high temperature and a raw material gas at a low temperature.

This first method can also be used to preheat the raw material gas. Furthermore, as a third method for the same purpose, instead of the raw material gas, which is the fluid on the cold side of the heat exchanger in the second method, another cooling fluid, such as another gaseous body or a desired temperature under pressure, is substituted. There is a method that uses a liquid that has reached boiling temperature or a multiphase fluid of liquid and its vapor. Methods for preheating the raw material gas include the second method described above and a method of indirectly exchanging heat between the high temperature gas flowing out from the most downstream of the reaction chambers and the raw material gas introduced into the reactor. If there is no problem in maintaining the strength of the pressure-resistant shell and preventing corrosion and embrittlement even if the pressure-resistant shell of the reactor rises to the operating temperature of the catalyst, heat exchange outside the reactor can be used as a raw material gas preheating method. It is also possible to heat the raw material gas using a reactor and introduce the raw material gas into the reactor after reaching the operating temperature of the catalyst. However, if it is necessary to maintain the temperature of the pressure-resistant shell below the operating temperature of the catalyst, it is necessary to install the indirect heat exchanger for preheating the raw material gas in the reactor.

The interior of the spherical pressure-resistant outer shell according to the present invention is used as a space for accommodating functional equipment such as the reaction chamber and catalyst, gas cooling, and raw material gas preheating as described above, but the volume required for each of these functional equipment is It varies significantly depending on the type of reaction that occurs in the reaction chamber, the type of catalyst used, the amount of heat generated during the reaction, the reaction temperature, the reaction pressure, etc. Therefore, there are many advantages to the present invention other than the reduction in reactor weight and wall thickness.

First, things common to many embodiments will be explained.

In general, in reactions where the reaction pressure is less than j kg/d (same as cage pressure or less), there is a pressure resistance difference between the weight of a cylindrical reactor using the same amount of catalyst and the weight of the spherical reactor according to the present invention. The difference in the amount of steel material required for the outer shell is small, and the advantages of the present invention are not noticeable. Reaction pressure/θkg/
The advantage of this invention is particularly when the weight is 3 kg/d or more. Regarding the reaction chamber, even when using a spherical reactor, in order to maintain an even flow of gas within the cross section perpendicular to the direction of gas passage in the reaction chamber and increase the effective utilization rate of the catalyst, The preference for a cylindrical or cylindrical reaction chamber is similar to that for a cylindrical reactor. However, if only one cylindrical or cylindrical reaction chamber is provided in a spherical reactor, the internal space other than the reaction chamber will be large, and in this internal space there will be equipment for cooling the catalyst and gas, or equipment for cooling the raw material gas. Even if equipment for preheating the reactor is accommodated, there will still be surplus space, and the advantage of using a spherical reactor will not be realized. Therefore, in order to effectively utilize the internal space of the spherical reactor, it is necessary to install at least two cylindrical or cylindrical reaction chambers. In addition, in a spherical reactor, unlike a cylindrical reactor, there is a truncated conical reaction chamber in addition to the cylindrical 2 cylindrical reaction chambers, and a cylindrical 1 part or all of the cylindrical or truncated conical outer surface and the inner surface of the pressure-resistant outer shell. Using the annular space formed between the two parts as a reaction chamber is an easy and advantageous method of effectively using the space within the reactor. This fact shows that spherical reactors are so-called “
Therefore, at least one reaction chamber according to the present invention includes a shape other than the above-mentioned cylindrical shape.Advantages of reaction chambers other than the cylindrical shape and two cylindrical shapes. will be explained in the section on specific examples.Two or more reaction chambers with these shapes have a common center axis, that is, they are coaxial, and the one with the smaller outer diameter is inside the one with the inner diameter. Installation is important for effective use of internal space.

The first structural advantage of the spherical reactor having the above structure is that the outer shell has a smaller wall thickness and weight than a cylindrical reactor having the same catalyst filling volume. One of the reasons for this is the general policy already described. The second structural advantage of the spherical reactor is that it is relatively easy to provide connections for gas, coolant, or catalyst at desired positions on the spherical surface of the spherical pressure-resistant shell. It is. In other words, in the case of a conventional elongated cylindrical reactor, it is possible to provide a space for gas and coolant to enter and exit at a location away from the end plates at both ends, but this requires a considerable increase in the length of the pressure-resistant shell. No. In particular, when an inner cylinder is required for a reaction chamber, a large expansion/contraction difference occurs between the outer shell and the inner cylinder due to the temperature difference during operation, and the side wall of the cylindrical pressure-resistant outer shell and the inner cylinder side wall. It would be impractical to install a pipe that penetrates the two to let gas or coolant in and out, as the structure would be complicated. On the other hand, in the case of the present invention, the annular space between the partition wall in the reactor and the inner surface of the spherical part of the pressure-resistant shell is used to
It is possible to install the tube for introducing and discharging the coolant etc. as a curved tube or coil along the inner surface of the pressure-resistant shell, and the structure is simple and the thermal stress due to thermal expansion of the reactor is not large. . In this respect, a large-sized reactor is advantageous in manufacturing because the annular space is large enough for an operator to work in this space.

In the explanation of the principle using FIG. 1, a case where the side surfaces of each reaction chamber in a spherical reactor are in contact with each other is illustrated for ease of explanation. It is desirable to install the reaction chambers in such a way that the reaction chambers are in contact with each other on some or most of their surfaces, since much of the space within the spherical reactor can be used as the reaction chamber. However, regardless of the shape of the reactor, the reaction that occurs in the reaction chamber has a large calorific value, the heat resistance of the catalyst is low, and the performance deteriorates due to an excessive rise in temperature, or the temperature of the gas and catalyst rises to a chemical equilibrium. If there is a property that makes the progress of the reaction unfavorable, a space is required in the reactor to provide the above-mentioned cooling equipment. In conventional cylindrical reactors, these cooling facilities are used, i.e., supply pipes or openings thereof to the reaction chambers of the low-temperature raw gas or gas passages between the reaction chambers, or the hot gas is connected indirectly to the low-temperature raw gas or other coolant. If a space is provided for installing a tubular heat transfer surface for heat exchange, it is necessary to increase the diameter or length of the cylindrical reactor for the same amount of catalyst. ``On the other hand, in a spherical reactor having two or more reaction chambers, an annular space remains between the reaction chamber and the outer shell of the spherical reactor, and this remaining space can be used directly or as a passage for the reaction gas. It can be used as a place to install a reservoir tube through which reactant gas, raw material gas, and coolant circulate while exchanging heat, thereby increasing the utilization rate of the internal space without increasing the internal volume of the spherical reactor.

As is clear from the above description, the entire surface of the spherical reactor does not need to be spherical in order to obtain the advantages of the present invention; any surface that is close to spherical can realize the advantages of the present invention. Even if a part of the spherical shell protrudes outward, the advantages of the present invention are not impaired as long as this protrusion is cylindrical and the diameter of the cylinder is relatively small compared to the diameter of the sphere. . For example, in the case where there are seven or more cylindrical protrusions that communicate with the internal space of the spherical part, the inventors have investigated the case and found that the part exhibiting a spherical surface with the boundary between the cylindrical protrusions and the spherical surface as a boundary. Even in a spherical reactor in which the surface area of the nuclear sphere occupies more than the total surface area of the core sphere in the absence of a cylindrical protrusion, almost the same advantages as in a spherical reactor without a protrusion can be realized. In this case, even if the protruding length of the protruding portion is considerably large, the above-mentioned advantages can be achieved in substantially the same way as compared to the case where the same volume as the internal space surrounded by the spherical surface is accommodated in the cylinder. Further, the number of these protrusions is not limited to seven, and it is also possible to provide a large number of small protrusions at desired locations on the surface of the spherical reactor.

Similarly, another example of a case in which the advantages of the present invention can be realized and the entire surface of the spherical reactor does not exhibit a spherical shape is that a cylinder with a length and a diameter under the clod has a hemispherical shape at each end with the same diameter as the cylinder. Some have a long spheroidal shape with mirror plates. This elongated spheroidal reactor is a preferred shape when the reaction heat generated is large and the reaction chamber needs to flow at high speed into the reaction chamber, and the reaction chamber must have a large heat transfer area for indirect cooling. becomes. Also in this elongated spherical reactor, the presence of at least seven cylindrical protrusions as described above does not hinder realization of the advantages of the present invention. In the following description, both the above-mentioned spherical and elongated spheroidal reactors with and without cylindrical protrusions are simply referred to as spherical reactors. In this case, it is often preferable for the common axis of each reaction chamber to be vertical as shown in Figure 1 for assembly and maintenance inspection purposes, but since both the raw material gas and the produced gas are gaseous, this common axis may be tilted even if it is horizontal. There is no problem in functionality even if it is.

Next, a method of using the spherical reactor according to the present invention will be explained. The shape of the cross section perpendicular to the gas flow direction inside the reactor of the present invention is the same in any cross section,
Moreover, it is possible to install two or more reaction chambers having the same length in the gas flow direction. If two or more reaction chambers are filled with the same catalyst, the raw material gas can be
It is also possible to pass the reaction through more than one reaction chamber in parallel. However, in such a method of passing gas in parallel, the gas flow rate to each reaction chamber may not be equal, resulting in uneven flow. If gas is allowed to flow in parallel through reaction chambers with different cross-sectional shapes and lengths, the risk of uneven flow increases. In order to prevent this uneven flow, it is necessary to add some kind of equipment to maintain an equal gas flow rate to each reaction chamber. In addition, the shape of the cross section perpendicular to the gas flow direction in a spherical reactor is the same in all cross sections, and it is not necessarily possible to install one or more reaction chambers having the same length in the gas flow direction. This cannot be said to be the most effective way to utilize the internal space of the vessel. For these reasons, it is a desirable method of utilizing the reactor of this invention to pass the gas in series through at least two reaction chambers in the spherical reactor of this invention, and according to this method of passing gas in series, A large amount of catalyst can be packed inside the spherical reactor almost regardless of the cross-sectional shape and length of each reaction chamber, so that the catalyst can be used effectively and the effective utilization rate of the internal space of the spherical reactor can be increased. The first advantage obtained by flowing raw material gas in series through two or more reaction chambers is that it becomes easier to prevent the temperature of the catalyst on the upstream side (especially the most upstream) of the raw material gas from rising too much. At the point. In other words, in order to make effective use of the catalyst, it is necessary to first bring the raw material gas, which has been preheated to the operating temperature of the catalyst, into contact with the most upstream catalyst; at this time, the raw material gas does not contain any reaction products. None or only a few. Therefore, a violent reaction occurs in the most upstream catalyst layer, and both the gas temperature and the catalyst temperature rise sharply. It is well known that such excessive rise in catalyst temperature has adverse effects on many catalysts, such as reduced performance or increased production of undesirable by-products. This problem can be solved by using a reaction chamber with a small cross-sectional area perpendicular to the gas flow direction and a small length on the upstream side, and by keeping the gas flow rate in this reaction chamber high. This can be easily prevented by limiting the generation of a large amount of reaction heat and by cooling the gas ' leaving the reaction chamber by one of the cooling means described above. Subsequently, as the concentration of reaction products in the gas increases, by passing the gas at a low flow rate through a reaction chamber with a dog cross-sectional area, it is possible to obtain reaction products in exactly the same way as in a conventional cylindrical reactor. At the same time, the effect of extending the life of the catalyst or reducing the amount of by-products produced can be obtained. In order to obtain the above effects in a conventional cylindrical reactor, the internal volume of the reactor must be increased as a necessary result.

In this invention, the second advantage obtained by allowing the gas to pass through each reaction chamber in series is to take advantage of the second structural advantage described above and to use piping for the high-temperature gas that has passed through the catalyst layer. The advantage is that it is relatively easy to take the gas out of the pressure-resistant shell and reintroduce it into the pressure-resistant shell from another position on the surface of the pressure-resistant shell. The advantage of this is that when the raw material gas contains trace amounts of substances toxic to the catalyst, a reaction chamber is provided in the spherical reactor that is completely separated from other reaction chambers, and this reaction chamber is used for the most upstream reaction in the reactor. The catalyst in this reaction chamber absorbs catalyst poisons, causing performance deterioration, but the catalysts in other downstream reaction chambers are protected from toxic substances, and only the most upstream catalyst is removed without replacing the downstream catalysts. replace it with a new one,
It can be used to extend the average life of all catalysts. This second advantage also allows two or more chemical reactions using different catalysts to be carried out in series in the same reactor, as will be described below with specific examples.

'The gas flow direction in each reaction chamber in the spherical reactor according to the present invention can be either the axial direction or the radial direction of the reaction chamber. For axial flow, top to bottom, right to left, or vice versa, and for radial flow, inside to outside or vice versa can be used. In addition, it is also possible to use a mixture of the above-mentioned flow directions on the reaction chamber side as desired, such as axial flow in some of the reaction chambers and radial/direction flow in other reaction chambers. .

As described above, the internal space of the spherical reactor according to the present invention is used as a reaction chamber, a gas passage, a space for mixing high-temperature gas and low-temperature raw material gas, and a space for installing a heat transfer surface for indirect heat exchange. These design requirements include the type of reaction that will occur in the raw material gas, reaction conditions such as temperature and pressure, and the type of catalyst.

It varies depending on many factors such as the amount of raw material gas supplied and the method for removing reaction heat. Hence these factors.

There are countless implementations depending on the combination of requirements. Several examples of these embodiments will be specifically explained below using the drawings, but the present invention is not limited to the illustrated embodiments.

Figure 2 shows a cylindrical or cylindrical shape filled with catalyst.
5 reaction chambers 3/, 32.33 are arranged vertically and coaxially.
This is an example in which a cylindrical protrusion is provided at the top of the reactor, and a shell-and-cheap heat exchanger for preheating the raw material gas is disposed within the protrusion to carry out an exothermic reaction. The raw material gas that has not been sufficiently preheated enters the reactor from the bottom of the pressure-resistant outer shell 3 through the tube, and enters the space in contact with the inner surface of the spherical part of the pressure-resistant outer shell 30.
It then passes through the space in contact with the inner surface of the cylindrical projection of the pressure-resistant shell 3 to reach the upper space 7.2 of the heat exchanger.

This raw material gas path can prevent the temperature of the pressure-resistant shell from rising. The raw material gas then passes through a large number of chambers in the heat exchanger group, where it performs indirect heat exchange with the high temperature reaction product gas exiting the reaction chamber 33, is preheated to a desired temperature, and reaches space /3. The raw material gas further passes through the space within the tube/g and enters the reaction chamber 3/, where a chemical reaction is partially caused, and the temperature of the gas increases due to the heat of reaction. This reaction chamber 3/ is cylindrical with an axis passing perpendicularly through the center of the sphere. The high-temperature gas that has partially undergone a reaction in the reaction chamber 3/ exits into the space /S, and then flows through this space and the reaction chamber 3.
While passing through the cylindrical space between / and 3, it comes into contact with the cooling pipe A3 provided in these rain spaces, through which coolant flows, and is cooled to a desired temperature, returning to space /7. reach. Next, the gas enters the three reaction chambers from space /7, where the reaction continues and the temperature rises again before exiting from space /9. The reaction chamber 32 is a cylindrical reaction chamber with a vertical axis passing through the center of the sphere, is coaxial with the reaction chamber 3/, and has an inner diameter of 3.
Although it is small, the horizontal cross-sectional area and reaction chamber height can be set to 3/3. Gas is in space/9 and reaction chamber 3
．． While passing through the cylindrical space -0 provided between 2 and 33, it comes into contact with a cooling pipe S3 through which a coolant flows, is cooled to a desired temperature, and enters the reaction chamber 33 via space 2/. ``The reaction chamber 33 is a cylindrical reaction chamber having a vertical axis passing through the center of the sphere, and a tubular space 3 serving as a gas passage provided at the position of this axis. The gas completes the chemical reaction within the reaction chamber 33,
It becomes high temperature again and enters the shell side of the heat exchanger G through the gas passage opening 2g through the space jJ, 23, where it preheats the above-mentioned passed raw material gas, and its own temperature decreases and enters the gas passage opening 2j. The gas leaves the reactor through the outlet pipe.

On the other hand, the pressure of the refrigerant is adjusted to the desired boiling temperature, and the refrigerant is treated as a liquid at approximately the boiling temperature in the refrigerant distribution pipe J/
, % or Otsu/ is introduced into the reactor interior through pipe 5.2 or Otsu2, and then through cooling pipe s3, respectively.
Alternatively, the gas enters Otsu 3, and while passing through these, heat exchanges with the gas exiting the reaction chamber 3.2 or 3/ as described above to cool the gas, and the gas itself becomes a gas phase or a gas in which a part of the liquid has evaporated. A mixture of phase and liquid is formed and flows into the gas-liquid separator 7θ via the pipe 3'1 or the pipe, respectively. Gas-liquid separator 7θ
At the refrigerant is separated into its vapor and liquid, the vapor is used for the desired purpose and the liquid is returned by gravity or pump to the refrigerant distribution pipes S/ and O/ (this part is not shown). ).

Although cooling tubes S3 and 63 are both shown as coiled heat transfer surfaces in this example embodiment, they could both be coils of seven tubes or two. However, the number of tube rows in this case is also 7.
The number of heat transfer areas may be two or more, and the key is to provide the necessary heat transfer area according to the desired amount of heat to be exchanged.

Further, the cooling tubes may be coil-shaped or may be a group of many substantially vertical tubes arranged concentrically as described later.

FIG. 3 shows an example in which one truncated conical reaction chamber is provided in which an exothermic reaction takes place, and the gas is cooled by adding and mixing low-temperature raw material gas into the reaction chamber. This figure is simplified for the purpose of showing the arrangement and shape of the reaction chamber.

In Fig. 3, 3/ is a reaction chamber, which has a vertical central axis passing through the center of the spherical pressure-resistant outer shell 3, and is a hollow truncated conical reaction chamber with a catalyst layer only at the periphery of this central axis. be. 3 is a truncated conical reaction chamber having a vertical axis passing through the center of the spherical pressure-resistant outer shell 3. In this embodiment, the feed gas preheated to the operating temperature of the catalyst enters the reactor from the upper feed gas port and reaches the annular space via one or more radially arranged gas passages. C,
Enter reaction chamber 3/ from this space. By contacting the catalyst in this reaction chamber, the reaction partially proceeds and the temperature of the gas increases. This reaction chamber is connected to the outside of the reactor through a pipe 7, and there is a gas cooling equipment with a diameter of θ in the disperser for uniformly distributing low-temperature raw material gas to a desired horizontal section within this reaction chamber. Equipped. By supplying and mixing the desired amount of low-temperature raw material gas with this equipment, an excessive rise in the temperature of the gas and catalyst is prevented, the reaction proceeds further, the gas is heated again, and exits from the reaction chamber 3/space/3. In space /3, the gas is again supplied with low-temperature raw material gas from the gas cooling equipment such as the pipe 7 leading outside the reactor and the distributor connected thereto, and the gas temperature after mixing is maintained at the desired temperature. descend. Next, the gas enters the reaction chamber 3.2 via the hollow truncated conical space /g and the space /j, where the reaction proceeds further. As a result of the progress of the reaction in the reaction chamber 32, the gas whose temperature has increased is the same as in the case of the reaction chamber 3/3. After being mixed twice and subjected to a cooling effect, the reaction is completed and the reaction gas exits from the reactor via the space 6 and the reaction gas outlet. Heat can be recovered from the high-temperature gas discharged from the reactor by, for example, a waste heat boiler, but this part is not shown. In this embodiment, since the additional supply of low-temperature raw material gas for cooling is performed within the reaction chamber or between the reaction chambers, the amount of gas in the downstream reaction chamber 32 tends to increase. However, by using a truncated cone-shaped reaction chamber and causing the gas to flow from the top to the bottom of the truncated cone, the cross-sectional area of the gas increases as the gas flows, and the gas flow rate within the reaction chamber increases. This makes it possible to prevent the pressure loss due to the gas flow from increasing, and to make the pressure loss due to the gas flow relatively small, and to prevent the reaction rate from decreasing due to the increase in the space velocity.

Similarly, by increasing the cross-sectional area of passage of downstream reaction base gas, the gas flow velocity can be reduced, and the effect of reducing pressure loss can be obtained. Furthermore, by increasing the filling amount in the downstream reaction chamber 32, the space velocity can be maintained at an appropriate value.

FIG. 9 shows one cylindrical reaction chamber 3/ for carrying out an exothermic reaction, and a reaction chamber 3.2 having the same central axis as the cylindrical reaction chamber 3/ and utilizing an annular space formed by the cylinder and the spherical surface of the pressure-resistant outer shell.
The gas is cooled by mixing low-temperature raw material gases using gravity, as in the case shown in Figure 3, but the preheating of the raw material gases and the cooling of the gas during the reaction are performed using a shell-and-cheap type heat source installed at the top of the spherical shell. This is done by indirectly exchanging heat between both gases in an exchanger.

This figure is simplified for the purpose of showing the arrangement and shape of the reaction chamber. In FIG. 9, 3/ is a cylindrical reaction chamber having a vertical central axis passing through the center of the spherical pressure-resistant outer shell 3;
is an annular reaction chamber having a vertical central axis passing through the center of the pressure-resistant outer shell 3 and formed by a spherical surface and a part of the outer surface of the reaction chamber 3/. In this embodiment, the feed gas which has not been sufficiently preheated enters the tube/' and passes through the upper space of the heat exchanger// into the multiple tubes of the heat exchanger group, where it passes through the reaction chamber 3/'.
It is preheated to a desired temperature by indirect heat exchange with the high temperature reaction product gas exiting from the reaction chamber 3.
/to go into. In this reaction chamber, the reaction partially proceeds due to contact with the catalyst, and the temperature of the gas increases. Inside this reaction chamber, there is a gas cooling equipment that is connected to the outside of the reactor through pipe 7 and has a disperser gap θ for uniformly distributing low-temperature raw material gas to a desired horizontal section within this reaction chamber. Equipped. By feeding and mixing the desired amount of low-temperature raw material gas in this equipment, an excessive rise in the temperature of the gas and the catalyst is prevented, and the reaction proceeds further, and the gas temperature rises again, but in the same way as in the pipe 7.
2.73, each of which communicates with the two distributors θ
It is mixed twice with the low-temperature raw material gas supplied from the reactor chamber 3/, which is cooled, and exits the reaction chamber 3/, into the space/3. It enters the shell side of the heat exchanger from the gas passage opening /j through /'I. Here, the raw material gas is preheated as described above, and its own temperature drops to the desired temperature, and the space /A, /7°7g is After that, it enters three reaction chambers. The gas that has completed the reaction in the reaction chamber 3.2 leaves the reactor via the space /9 through the outlet 2. In FIG. 9, the cross sections of the gas passages in reaction chamber 3/ and reaction chamber 3- are the same, but in this structure, the shape of the reaction chamber may be made into a truncated cone as in the case of FIG. Furthermore, by making the gas passage into a multi-stage columnar shape and changing the cross-sectional area of the gas passage, pressure loss can be reduced and reaction conditions can be optimized.

FIG. S shows an example of an embodiment in which gas flows in the radial direction of the cylindrical reaction chamber 3 and the cylindrical reaction chamber 32 located inside the cylindrical reaction chamber 3, and an exothermic reaction occurs. Cylindrical reaction chamber 3. !
The inside thereof is provided with seven or more multi-jointed cooling pipes S3 arranged vertically on concentric circles for circulating coolant. The unpreheated raw material gas enters the reactor from the lower gas inlet//, passes through the space// along the inner surface of the spherical pressure-resistant shell, and then enters the central space of the reaction chamber 3.2. Upper chamber 3 of shell and cheap heat exchanger
The heat exchanger passes through the upper chamber 7.2 of the L&Cheve type heat exchanger installed in the central space of the heat exchanger, and passes through a large number of chambers for this heat exchanger. After being preheated to the desired temperature, the lower chamber/3 of this heat exchanger
flows into. Next, this preheated raw material gas enters the peripheral pressure equalization space /j through the space /g in the radially provided connecting pipe, and from there it travels inside the reaction chamber 3/in a radial direction almost horizontally. That is, it flows from the outer circumferential portion of this cylindrical reaction chamber toward the cylindrical axis direction passing through the center of the spherical portion of the pressure-resistant outer shell. When the raw material gas comes into contact with the catalyst inside this reaction chamber 3, an exothermic reaction occurs and the temperature of the gas rises. Into this reaction chamber 3/, the pipe 7/ is introduced from outside the reactor as in the case of FIG. A cooling facility may be provided to uniformly disperse and add the low-temperature raw material gas and to prevent the temperature of the gas from rising excessively during the reaction. After the gas from the reaction chamber 3 once flows into the cylindrical pressure equalizing space /6 provided between this reaction chamber and the cylindrical reaction chamber 32 located inside it, the gas is then perpendicular to the reaction chamber 3/. The liquid flows into the cylindrical reaction chamber 32, which has a long direction, almost horizontally and radially, that is, in the direction of the central axis. The reaction proceeds again, but inside the three reaction chambers there are many cooling pipes s3 arranged concentrically as described above.
The reaction heat generated in this reaction chamber is removed by the coolant flowing through these cooling pipes j3, and an excessive rise in temperature is prevented. The reason why the above-mentioned cooling equipment is used in the reaction chamber 32 in this embodiment is that the cooling equipment allows the cooling liquid exhibiting a desired boiling temperature to flow through the cooling pipe j3 while being boiled under an appropriate pressure. It is possible to impart a very large cooling power to the cooling pipes, and it is also possible to adjust the arrangement density of these many cooling pipes in the three reaction chambers. This is because it becomes possible to match the temperature distribution of the catalyst layer and the gas flow along the flow direction (that is, the radial direction) to a desired preset temperature distribution. Appropriate setting of the temperature distribution along the flow direction of the gas in the catalyst layer is important because the reaction limit decreases due to chemical equilibrium reasons as the gas temperature rises, which is often seen in exothermic reactions. This is important in order to prevent the concentration and yield from becoming small, or to obtain a constant amount of product with the minimum amount of catalyst. After passing through the reaction chamber 32 in the radial direction, the still hot gas that has completed the reaction flows out into the cylindrical space /7 between the heat exchanger 3.2 and the reaction chamber 3.2, and then flows into the shell of the heat exchanger The raw material gas flows into the side from the bottom, indirectly preheats the raw material gas as described above, and then exits from the reactor through the gas outlet.

On the other hand, the coolant is introduced into the reactor as a liquid at a high boiling temperature under the desired pressure from outside the reactor through pipe j/, and is then introduced into the reactor through seven or more annular coolant distribution pipes communicating with pipe j/. j
The gas and liquid are distributed to a large number of cooling pipes S3 by the cooling pipes S3, and while boiling in these cooling pipes, the gas flows upward and collects in seven or more annular collecting pipes S4t, passing through pipes jj to the gas and liquid outside the reactor. It flows into the separator 7θ.

The liquid and vapor of the coolant are separated in the gas-liquid separator 7θ,
The steam is delivered to the desired use through pipe SA, and the liquid is returned to pipe j/ without being cooled, either by gravity or by means of a pump, but this part is not shown. In addition, this reactor uses a turnbuckle at the top,
Although the structure is such that the weight of the reaction chamber is suspended, this structure is more advantageous than supporting the reaction chamber from below in terms of thermal stress and strength.

FIG. 6 is an example of using a heat exchanger located outside the reactor.

In this example, the reactor has one cylindrical reaction chamber 3/ and 3.2 and seven cylindrical reaction chambers 33 whose axis is a straight line passing through the center of the sphere, three of which are 3/, 32 and 33. The reaction chambers 3/a and 3/b are independent reaction chambers 3/a and 3/b; 32a and 3.2b, 33a and 33b
It is divided into two equal parts, and between 3/a and 31b there is an annular space /3 that serves as a gas passage, 3,! There is an annular space /7 between a and 32b that serves as a gas passage, and between 33a and JJb
There is a disc-shaped space -〇 between them. The preheated raw material gas is introduced into the reactor from the single-pipe inlet//, and first flows into the space//. From this space //, the raw material gas flow is divided into two equal parts, one of which is the reaction chamber 37B.
and the inner surface of the spherical pressure-resistant outer shell as shown by the arrow, and flows into the reaction chamber J/a via the annular space /2a.

The other flow b passes through the gap between the reaction chamber 31b and the inner surface of the spherical pressure-resistant shell as indicated by the arrow, and flows into the reaction chamber 31b via the annular space 7.2b. Reaction chambers 3/a and 31b
The raw material gas flowing into the chamber causes a chemical reaction in both reaction chambers,
When this chemical reaction is an exothermic reaction, the temperature increases, and when this chemical reaction is an endothermic reaction, the temperature decreases, and both flow into the space /3 and merge. This combined gas flows through the space /lI into an indirect heat exchanger located outside the reactor, exchanges heat with the fluid at the desired temperature flowing into the tube from /a and flows out from g/b, and undergoes temperature adjustment. . That is, if the gas temperature after merging in space /3 is higher than the proper temperature of the adjacent downstream catalyst layer, it is cooled, and if it is too low, it is heated and adjusted to the desired temperature. The temperature-adjusted gas flow is divided into approximately equal parts again, with one flow a passing through the tube /3a and entering the annular space /A.
a to the reaction chamber 3. ! a, and the other flow b passes through the pipe/jb and the annular space/6b to the reaction chamber 32b.
respectively. A chemical reaction occurs again in the reaction chambers 3.2a and 3.2b, and the temperature of the gas increases if this chemical reaction is exothermic or decreases if it is endothermic. The gases that have passed through the reaction chambers 3.2a and J2'b each flow into the annular space /7, where they join together again,
Flows into the heat exchange via space/g. In this heat exchanger, the gas is subjected to temperature adjustment in the same manner as described above, and is further divided into approximately equal parts, each of which flows into the reaction chamber 33a or 33b via the pipe /9a or /9b, respectively. The gases that have flowed into the reaction chambers 33a and 33b undergo a reaction again to cause a temperature change, and after completing the chemical reaction in both chambers, they join together again in the space -〇 and exit the reactor from the produced gas outlet -〇. leave. This generated gas outlet is provided to penetrate the pressure-resistant outer shell 3 perpendicularly to the plane of the paper. The gas exiting the reactor from the produced gas outlet - is still at a high temperature, and heat can be recovered from this gas, but this is not shown.

In this example, pressure loss is reduced by dividing the cylindrical and cylindrical reaction chambers into one and using them in parallel. At the same time, in the case of an exothermic reaction, the pressure-resistant shell can be kept at a relatively low temperature.

In this embodiment, the common axis of each reaction chamber is vertical, but the common axis can be horizontal or inclined to adjust the position of the gas permeable catalyst receiver. It can be used without any problems. Further, as described above, the chemical reaction may be an endothermic reaction, an exothermic reaction, or an exothermic reaction. Furthermore, reaction chamber 3/, 3.
The catalyst filled in 2 or 33 may be the same catalyst that causes the same chemical reaction, but the temperature characteristics are required to cause the same chemical reaction.

Different types of catalysts differing in optimum space velocity etc. may also be used.

Furthermore, this embodiment is characterized in that the reaction chambers 3/, 32 and 33 are filled with different types of catalysts for causing different chemical reactions;
By passing a gas adjusted to an appropriate temperature for each of these different types of catalyst in series through each catalyst layer, it is possible to perform multiple stages using one or three reactors instead of using a conventional reactor. Alternatively, in cases where it is necessary to carry out a three-stage chemical reaction, it becomes possible to carry out the process as a substantially one-stage reaction using a method such as this example. The different chemical reactions at this time may include endothermic reactions and exothermic reactions. If there is a large difference in temperature between the reaction chambers when such different chemical reactions occur, it is preferable to use a partition wall interposed between adjacent reaction chambers that has heat insulating properties. Also, if desired, for example, an additional raw material supply port/
It is also possible to additionally supply a raw material gas of a different type from the raw material gas supplied from θ to the gas population /g to cause a chemical reaction different from that in the other two reaction chambers to occur in the -reaction chamber 33, or conversely, a chemical reaction different from that in the other two reaction chambers can be performed. Means for separating and removing some of the products produced in the reaction chambers 3/32 can also be interposed between the heat exchanger 2 and the reaction chambers 3/32.

An example of such different chemical reactions is the synthesis of methanol from hydrogen and carbon oxide, and the subsequent synthesis of hydrocarbons from methanol. That is, a high-pressure gas rich in hydrogen and carbon oxide is supplied from the raw material gas source /, and a well-known methanol synthesis catalyst (for example, containing chromium, copper-zinc, etc.) is used in the reaction chambers 3 and 32, and the pressure /θθ( A mixed gas of methanol, hydrogen, and carbon oxide is produced at a temperature of about 30θ℃, and as soon as this mixed gas is separated, the temperature is reduced to 35θ℃ using a heat exchanger.
Reaction chamber 3 in which zeolite catalyst is used after adjusting to about ℃
Dimethatol can be converted to hydrocarbons by passing it through 3. At this time, the hydrogen and carbon oxides that were not converted to methanol are recycled to the raw material gas after separating the methanol and hydrocarbons, and the methanol that was to be converted to hydrocarbons is separated from the hydrocarbons and then supplied as an additional raw material as steam or liquid. It can be returned to the port n and reintroduced into the reaction chamber 33.

The advantages of the reactor according to the invention and its method of use are numerous, as already mentioned, but to summarize, the first advantage relates to the reactor, and as mentioned above, the advantages of the reactor and its method of use are numerous. The thickness of the pressure-resistant outer shell is small, and the weight of the reactor is also small. This advantage makes it possible to save on steel materials for reactor manufacturing, and the reactor itself can be manufactured at low cost, and the foundation, frame, piping, etc. for installing this reactor can also be made smaller, making it possible to reduce the overall cost. This advantage is especially great in large-scale high-pressure reactors, since construction costs can be reduced.

The second advantage relates to the reaction method, and the reactor has one or more reaction chambers as described above, each having a cylindrical shape, a cylindrical shape, or a truncated conical shape, which differ in cross-sectional area perpendicular to the direction of gas passage and catalyst loading. Therefore, reaction chambers of different shapes can be designed and used as desired depending on the nature of the chemical reaction and the characteristics of the catalyst. In other words, if the same chemical reaction is carried out at the same space velocity (especially in large reactors), a cylindrical reactor must be very elongated, and if the gas is allowed to flow in the axial direction of the cylinder, Although the uneven flow of gas in the catalyst layer is small, the flow velocity increases and the pressure loss increases.Conversely, if the gas flows in the radial direction to reduce the pressure loss, it will flow in each cross section perpendicular to the long axis. However, when a spherical reactor is used as in this invention, the shape of each internal reaction chamber is so-called a square shape with a small ratio of diameter to height, so drifting does not occur. Moreover, it can be used as a reactor with little pressure loss.

This advantage also has the effect of extending the life of the catalyst. The catalyst life extension is achieved for two reasons with different principles. The first reason is in the case of highly exothermic reactions, such as methanol synthesis from hydrogen and carbon oxide. In general, in this type of reaction, if gas is passed through each catalyst layer at an average flow rate suitable for all catalysts, as mentioned above, the catalyst that first comes into contact with the raw material gas will have a small concentration of products, so a violent reaction will occur. This causes thermal deterioration of catalyst performance due to excessive rise in catalyst temperature. This phenomenon can be prevented by flowing gas through the catalyst at high speed. In order to prevent this phenomenon when using a cylindrical reactor for this type of reaction, if the gas is made to flow axially, it becomes necessary to increase the length of the reactor and the pressure loss is reduced. When flowing in the radial direction, it becomes necessary to create wasted space within the reactor, which is not practical. On the other hand, in the case of the present invention, the above-mentioned phenomenon can also be prevented since it is easy to provide a small, square-shaped reaction chamber without increasing wasted space in the reactor. The second effect of extending the life of the catalyst is, as mentioned above, when the raw material gas contains a trace amount of a substance that is toxic to the catalyst.
Small catalyst layer space (reaction chamber) that first comes into contact with this raw material gas
If the structure is sufficiently isolated from the other reaction chambers, heat exchangers, and cooling equipment space in the spherical reactor, and these are connected with a pipe with a nozzle running outside the spherical reactor, the raw material can be If the catalyst that comes into contact with the gas first becomes poisoned, it is possible to isolate only the reaction chamber containing this catalyst from other reaction chambers using a valve and replace the internal catalyst with a new one. The life of most catalysts can be extended.

The third advantage of this invention relates to the method of using this reactor, as described in the explanation of the embodiment shown in FIG. This reactor can be used for reactions.

In this case, two or more different reactions can be used as a reactor to carry out chemical reactions that are completely unrelated to each other in parallel, but generally one or more chemical reactions are carried out step by step from a certain raw material. By using this reactor, it is possible to perform a substantially staged reaction when the final product is obtained by conducting the reaction in series, and this is a preferred method of use as a means of reducing the number of reactors. It is.

The reactor according to the invention is suitable as a reactor for obtaining gaseous products from gaseous raw materials under pressures above S (example), the above-mentioned advantages being that the reaction pressure is increased and the The internal volume of the reactor increases as the volume increases.Furthermore, preferred chemical reactions for using the reactor according to the present invention include the following: Synthesis reaction of ammonia from a gas containing hydrogen and nitrogen: hydrogen and oxidation Synthesis reaction of aliphatic/hydric alcohols such as methanol, ethanol, propatools, butanols, etc. from gas containing carbon: Direct synthesis reaction of hydrocarbons from gas containing hydrogen and carbon oxide (so-called Fischer-Tropsey synthesis): Hydrogen A hydrocarbon synthesis method in which a fatty alcohol/hydric alcohol is synthesized from a gas containing water vapor and carbon oxide, and the fatty alcohol/hydric alcohol is subsequently converted into a hydrocarbon: A gas containing water vapor and carbon monoxide is converted into a gas containing hydrogen and carbon dioxide. Conversion reaction: A reaction that converts a gas containing hydrocarbons and water vapor, such as methane or naphtha, into a gas containing hydrogen and carbon oxide: A reactor that synthesizes saturated hydrocarbons from unsaturated hydrocarbon gas and hydrogen-containing gas. The main thing.

Conditions such as temperature and pressure space velocity when carrying out these chemical reactions vary depending on the type of reaction and the characteristics of the catalyst used, but are well known when using a conventional cylindrical reactor. Conditions approximately equivalent to the conditions can be used.

Furthermore, well-known devices can be used for the disperser for the low-temperature raw material gas supplied when cooling the catalyst and gas inside the reactor according to the present invention, various heat exchangers, gas-permeable catalyst supports, etc. can. Further, in the present invention, water whose pressure is adjusted so that it boils at a desired temperature is used as a coolant for cooling the catalyst and the gas during the reaction by the indirect heat exchange method.

Preferred examples include a mixture of seven or at least two hydrocarbons that are liquid at room temperature, and a heat medium such as Dowtherm. However, gaseous or other liquid cooling media may also be used satisfactorily.

[Brief explanation of drawings]

FIG. 1 is a schematic cross-sectional view of a cylindrical reactor and a spherical reactor illustrating the principle of the present invention. Second. Third. Figures G, J, and 6 are examples of embodiments of the present invention, respectively. A Spherical pressure-resistant outer shell B Cylindrical pressure-resistant outer shell C, D, E, D', E' Reaction chamber/ Raw material gas inlet Reaction product gas outlet 3 Pressure-resistant outer shell Heat exchanger S for preheating raw material gas
Catalyst filling port 6 Catalyst extraction port A Gas-permeable catalyst receiving area constituting at least a part of the outer surface of the reaction chamber, 9 Heat exchanger/θ Additional raw material supply port//~29 Space for gas passage, with a number of The order indicates the order of gas passage. 37 to 39 Reaction chambers; the order of gas passage into the reaction chambers is shown. j/~S9 A coolant path, where the order of numbers indicates the order of the coolant path. 67-69 Coolant passage according to the above, S/~
j shows a different passage than wa. 70 Coolant gas-liquid separators 77 to 79 Injection pipes for gas and low-temperature raw material gas for catalyst cooling, and the larger the number, the more downstream. θ For a disperser of low-temperature raw material gas for cooling/
Fluid inlet 2 Fluid outlet? / Turnno (Tukuru Figure 1 Figure 1 Figure 3 Figure V Figure J

Claims (1)

[Scope of Claims] ■ A reactor for producing a reaction product gas by bringing a gaseous raw material into contact with a fixed bed granular catalyst under high pressure to cause a chemical reaction in the raw material gas, the pressure-resistant outer shell being (I) ) It is a sphere or a cylinder whose length is less than 10 times the diameter and has hemispherical end plates at both ends with the same diameter as the diameter of the cylinder (b) Or the spherical or long spheroidal pressure-resistant outer shell is at least 7 times the length of the cylinder cylindrical protrusions, in which case the surface area of the pressure-resistant outer shell excluding the protrusions occupies 10 or more of the total surface area of the nuclear sphere or the prolate sphere; 2 cylinders inside. At least seven reaction chambers selected from a group of at least seven reaction chambers each having a truncated cone shape or an annular shape formed between a part or all of the outer surface of the truncated cone and a part of the inner surface of the sphere. A spherical reactor characterized in that two reaction chambers are provided in a mutually arranged relationship such that the smaller outer diameter of the reaction chambers is inside the inner diameter dog. (2) Using the reactor according to claim 1 in a method of bringing a gaseous raw material into contact with a fixed bed granular catalyst under high pressure to cause a chemical reaction in the raw material gas to obtain a reaction product gas; A reaction method characterized in that the gas is passed in series through at least one reaction chamber in the reactor. ■ Penetrate from the outside of the pressure-resistant shell through the spherical part of the pressure-resistant shell or the elongated spherical part and the partition wall for partitioning the internal space of the reactor to connect the partitioned space inside the reactor to the outside of the reactor. A curved pipe is provided between the pressure-resistant outer shell penetrating part and the inner partition wall penetrating part of the pipe for communicating with the pipe in a space close to the inner surface of the spherical part or the elongated spherical part of the pressure-resistant outer shell. A reactor according to claim 1. ■■ Each of the reaction chambers is cylindrical, and the axis of the cylinder is arranged vertically. @ An equal pressure space is provided between the adjacent reaction chambers, and θ source gas is distributed between each of the reaction chambers. flowing in series and radially; ■ At least seven of the reaction chambers are parallel to the axis;
Claim 1 or 3, wherein a large number of cooling pipes are arranged in at least two concentric circles through which a gas-liquid mixed-phase coolant that is boiling at a desired pressure flows upward. reactor. ■ In the internal spaces of at least seven of the cylindrical protrusions of the pressure-resistant shell, there is indirect heat exchange for preheating the low-temperature raw material gas with the high-temperature gas that is in the middle of the reaction or has completed the reaction. Claim 1, in which the device is installed;
The reactor according to item 3 or 9.