WO2003055586A1 - A method and apparatus for optimizing the gas-solid phase catalytic reaction - Google Patents

Abstract

A method and apparatus for optimizing the gas solid-phase catalytic reaction under pressure, wherein a reactor is composed of a self heating reactor and a separately cooling reactor. Such two kinds of reactors are continuous heat exchange reactors, and are associated with each other in succession. Firstly, gases react in the self heating cold pipe reactor at balanced temperature, and catalyst layer is cooled with synthetic gas to transfer heat. Then, in the separately cooling reactor, the catalyst layer is cooled with water to reover heat of the reaction, and to make the temperature of the latter reactor lower than the front reactor. Increased reaction conversion rate, reactant concentration, and productivity are achieved. The present invention has the advantages of optimized reaction temperature, simple structure, good operating performance and reduced investment.

Description

 Method and equipment for optimizing gas-solid phase catalytic reaction

 The invention is a gas-solid phase catalytic reaction method and equipment, which is used for fluid catalytic reaction and heat transfer process, belongs to the field of chemical engineering, is particularly suitable for methanol synthesis reaction process, and can also be used for methyl ether, methylamine, ammonia, methane, Chemical processes such as carbon monoxide transformation. Background of the invention

 For gas-solid phase exothermic catalytic reactions such as methanol synthesis, methylamine, methyl ether, ammonia synthesis, and CO shift under pressure, as the reaction progresses, the continuously released reaction heat increases the temperature of the catalyst layer. In order to improve the efficiency of the reactor, it is necessary to remove the reaction heat to reduce the temperature of the reaction gas. One type that has been widely used in industrial reactors is a multi-stage adiabatic reaction. The raw gas is used to cool the reaction gas between the two stages to reduce the temperature of the reaction gas. This type of reactor reduces the temperature of the reaction gas at the same time as the raw gas is cooled. Reduced the concentration of reactants and affected the synthesis rate. Another type of tubular reactor of the German company Lurgi for methanol synthesis has a plurality of round tubes between the upper and lower tube plates in a pressurized shell. The tubes contain a catalyst, and the raw material gas enters and distributes from the upper air inlet. In each tube, methanol was synthesized in a catalyst layer inside the tube, and water was introduced into the sides between the tubes. The reaction tube is continuously transferred by boiling water outside the tube to generate steam from the side tube and the reaction gas from the bottom outlet tube to the tower. The temperature difference of the tower is small, but the catalyst loading factor is small and the investment is large. The structure of the SPC reactor disclosed by Japanese Mitsubishi Company, such as USP4767791, is to change the tubes in the shell-and-tube reactor into concentric sleeves, and the catalyst is installed between the inner and outer tubes. Heat exchange to reduce the reaction temperature at the end of the catalyst layer and increase the synthesis rate, but the structure is more complicated.

 The task of the present invention is to provide a reactor with reasonable temperature distribution of catalyst layer, high catalyst activity, simple and reliable structure, and good operation performance based on the characteristics of gas-solid phase catalytic exothermic reversible reaction and overcoming the characteristics of the prior art. Meet the best response method. Summary of the invention

The present invention mainly achieves the objective through the following improved methods, that is, the gas-solid phase exothermic catalytic reaction is firstly carried out by self-heating reaction, that is, the raw material gas entering the tower is used to absorb the reaction heat in the catalyst layer outside the tube in the cold pipe, and at the same time the incoming gas reaches the reaction Temperature, and then enter the catalyst layer for reaction. Then it enters the external cooling reactor and uses a coolant (such as water) to indirectly exchange heat to absorb the reaction heat and generate steam. This combination of self-heating and external cooling heat exchange reactions can keep the latter part of the reaction at a lower temperature than the previous one. This pair of exothermic reversible reactions such as methanol synthesis can increase the rate of the synthesis reaction and increase the rate of methanol synthesis. The gas-solid phase catalytic reaction method and equipment of the present invention mainly include a gas-solid phase confirmation method. The exothermic catalytic reactor 1 is composed of two types of continuous heat exchange reactors: self-heating type 1A and external-cooling type 1B. The self-heating type reactor 1A is composed of a pressure-containing shell P and a gas exchange pipe which can flow up and down. The cold tube bladder Cb composed of the heat pipe and the catalyst K are formed. The heat exchange tube has ports, and the inside and outside of the tube communicate with each other. The external cooling reactor 1B is composed of a pressure-containing shell P, a heat exchange tube group Cd, and a catalyst K. Connected, the reactor 1, heat recoverer 2, gas-to-gas heat exchanger 3, reaction product cooling condenser 4, separator 5, gas compression cycler 6 and other pipes are connected to form a continuous industrial production device. The gas first reacts in the reaction. The reactor 1A absorbs the heat of reaction in the cold tube bladder Cb of the self-heating reactor, heats it to the reaction temperature and then reacts in the catalyst layer outside the tube, and then the externally cooled reactor 1B continuously absorbs the reaction heat through the heat exchange tube group Cd with the cooling medium. The hot gas leaving the reactor is recovered by the heat recoverer 2 and the gas-gas heat exchanger 3 exchanges heat with the cold air before entering the reactor. The cooling condenser 4 cools the reaction gas to condense the reaction products. The separator 5 separates the products. The separated gas In addition to emissions one In most cases, most of the decirculation machine 6 is mixed with the raw material gas after increasing the pressure, and is heated into the reactor in the gas-gas heat exchanger 3 for reaction. The heat exchange tube group Cd of the external cooling reactor 1B is composed of one or more groups. Cold tube biliary Cd Cd ₂ … coaxial set, each group of cold tube biliary is composed of coolant inlet pipe _ai , lower ring pipe is shunt pipe and cold pipe b, upper ring pipe is header pipe, outlet pipe, inlet pipe It is connected to the lower ring 瞀 that is the shunt pipe d, the outlet pipe is connected to the upper ring pipe that is the header, the cold pipe b is connected to the upper and lower ring pipes, and the cooling medium enters the inlet pipes _ai , a ₂ and then is divided by the shunt pipes d, C ₂ In each cold pipe b, it flows to the collecting pipe, d ₂ and flows out from the outlet pipe E _{2. The} gas enters through the port on the shell P, reacts through the catalyst layer outside the cold pipe group, and the reaction heat is cooled by the cold pipe b. The medium is absorbed, and the gas is discharged to the bottom gas outlet G _{2. The} upper part of the reactor is equipped with a catalyst P h, and the bottom is provided with a catalyst porous support grid (R). 5〜0. 8。 The amount of catalyst installed in the self-heating internal cooling reactor is the total amount of catalyst installed in the reactor 0. 5 ~ 0. 8.

 The reactor 1B can be the coolant in the tube, and the cold tube of the cold tube group can be a round straight tube, a flat tube, or a serpentine circular tube, a spiral circular tube, a multi-elbow U-shaped tube, or it can be cooled. The catalyst is installed between the tubes and shells, and the catalyst is installed in the tubes. This modification of the existing device can use the original tube and shell reactor. Brief description of the drawings

 Further description will be made below with reference to the drawings.

 Fig. 1 is a simplified flow chart of the present invention.

 Fig. 2 is another rendering of the present invention.

 Fig. 3 is a schematic diagram of an externally cooled by-product steam reactor according to the present invention.

 Fig. 4 is a schematic diagram of an externally cooled by-product steam radial reactor according to the present invention. '

 Fig. 5 is a schematic diagram of an axial flow reactor combining self-heating and external cooling according to the present invention.

Fig. 6 is a schematic diagram of a radial flow reactor combining self-heating and external cooling according to the present invention. Detailed description of the invention

 The present invention is described in detail below by taking methanol synthesis as an example, in which the recovery of reaction heat is achieved by passing a coolant to generate steam. In the following examples, water is used as an example of the coolant, but this example is not limitative, and those skilled in the art can understand that various known coolants can be used in addition to water.

 In FIG. 1, there are an internal cooling type reactor 1A and an external cooling type reactor 1B connected in series before and after, and there are a waste heat boiler 2, a gas-to-gas heat exchanger 3, a water cooler 4, a methanol separator 5, and a circulation compressor 6, which are used in front and rear. The pipes are connected to form a methanol production unit. The raw material gas 7 containing hydrogen and carbon oxide ¾ compressed to 3 to 32 MPa by the compressor enters the methanol synthesis device and is combined with the circulating gas 12 from the cycler 6 to form a mixed gas 8, which is exchanged and heated by the gas-gas heat exchanger 3 and the reaction gas. It enters the reactor 1A at about 100 ° C. The reactor 1A can use, for example, the patent "W00191894" published by the inventor, or other self-heating and cooling tube structure. The gas entering the synthesis tower absorbs the reaction heat in the catalyst layer outside the tube in the cold tube, and the temperature rises to about 200 ° C, exits the cold tube, and enters the catalyst layer outside the tube to react. Due to the continuous heat transfer of the gas in the cooled pipe, the temperature difference of the catalyst layer is kept low. The C 0H in the reaction gas from reactor 1A reaches about 6% and the temperature is about 25.CTC, and then enters the external cooling reactor of reactor 1B to further A methanol synthesis reaction was performed. The reaction heat is continuously removed by the coolant (such as water) through the tube wall. The reaction heat can be used to generate medium pressure steam with a pressure of about 4 MPa. The reaction temperature can be easily adjusted by the pressure of the by-product steam, so that the reactor 1B can be adjusted. The reaction temperature is lower than 1A of the front reactor, for example, about 210 ° C, in order to optimize the reaction temperature process conditions, improve the synthesis rate, and increase the methanol concentration in the reactor to about 10%. The reaction gas 9 from the reactor 1B is recovered by the external heat recovery device 2 to recover the reaction heat, and the low-pressure steam is by-produced, and then the reactor gas 8 is heated in the gas-gas heat exchanger 3, and then the reaction gas enters the water cooler 4 to further After cooling to about 30 ° C, most of the methanol in the reaction gas was condensed. The cold reaction gas enters the methanol separator 5 for gas-liquid separation. The product methanol is sent out from the lower part through the tube 13 and the unreacted gas 10 is sent from the upper outlet. A small part of it is discharged as a relaxation gas from the tube 11 'to maintain inertness in the synthesis system. The gas content will not be too high. Most of the gas 12 is combined with the raw material gas 7 into gas 8 after being boosted by the cycler 6, and once again goes to the reactor to start another cycle. In FIG. 1, the boiler water in the reactor 1B enters through the bottom pipe 14, and the medium-pressure steam generated is led out by the upper pipe 15. The tube 15 communicates with the drum. The boiler water in the heat recovery unit 2 is fed in by the pipe 16, and the low-pressure steam generated is led out by 17, and the cold water in the water cooler is led in by the pipe 18 and discharged by 19.

 Figure 2 is another flowchart. In addition to combining the reactors 1A and 1B in FIG. 1 into one,

1 consists of an upper self-heating type and a lower external cooling type reactor. The lower external cooling type is a heat exchange tube with multiple u-shaped elbows.

Fig. 3 is a schematic diagram of an external cooling reactor. A heat exchange tube group Cd is installed in the pressurized shell P, and a catalyst K is installed between the shell P and the heat exchange tube group Cd. The heat exchange tube group Cd is composed of two groups of cold tube biliary Cd Cd ₂ , each group of cold tube biliary. ^ Composed of shunt pipe (lower ring pipe) c, multi-row cold pipe header (upper ring pipe) connection. Cold pipe b shunt tubes and the connecting manifold, an inlet pipe connected to _AI shunt tube, outlet tube connected to the manifold ₅₁ through the housing and the outer conduit coupling. The outlet tube can be an elastic hose or a corrugated tube, and the cold tube Cd ₂ is also dl. The outlet tubes E _t and E ₂ can be led out of the reactor shell separately, or they can be taken out from the outlet f after converging in the reactor as shown in the figure. . The position of f can be on the side as shown in the figure, or in the middle of the top of the upper head, and the air inlet ^ is set on the side. The reactor has an air inlet G ₁ at the top and an air outlet G ₂ at the bottom. The gas outlet G _{2 is} provided with a porous conical cover ^ to support the catalyst K in the reactor, and a manhole h at the top is also provided for loading the catalyst and serving as an inspection port. When this reactor is used as a by-product steam for methanol synthesis, the boiler water that has been preheated to about 200 由 is introduced from the inlet pipe a _t to the lower stream pipes d and C ₂ and then evenly divided into the cold pipes b. As the water in the cold pipe flows upward, it absorbs the reaction heat outside the pipe, and it is heated to vaporize to generate steam, which is then merged by the upper header, d ₂ , and is led by the outlet pipes Ei, E ₂ and enters the tower at a temperature of 200 ° C or higher. The gas enters through the air inlet G and enters the methanol catalyst layer K to react. The reaction heat is absorbed by the water in the tube, so the temperature difference of the catalyst layer is small.

Fig. 4 is a schematic diagram of an externally cooled radial reactor. The heat exchange tube group in FIG. 4 is similar to the multiple heat exchange tube groups in FIG. 3. Different from FIG. 3, a cylindrical porous shunt wall L is provided on the inner side of the casing P, a circular annular inlet passage is formed between the top end of the shunt wall L and the casing P, and a porous gas collecting pipe m is provided at the center. After entering the reactor, the gas enters the catalyst layer K at the shunt wall L to form a radial flow reaction. After the reaction, the gas enters the gas collecting tube m and enters the gas collecting tube. The gas exits the tower from the outlet G ₂ . The annotation is the same as in Figure 3.

The external-cooled reactors in Figures 3 and 4 can also be used for endothermic reactions, such as methane conversion and hydrocarbon cracking. At this time, the heating agent enters the heat exchange tube group Cd through the inlet pipe _ai , and the heat for the endothermic reaction in the reactor 1B is supplied by the heat agent in the heat exchange tube group Cd.

Figure 5 is a simplified diagram of a reactor with a combination of internal and external cooling. The upper part is a self-heating internal cooling reactor, and the lower part is an external cooling type. The upper and lower reactors have the same pressure-containing shell P, and the upper self-heating reactor housing has an internal cooling cold tube bladder Cb, the cold tube bladder Cb has a gas distribution pipe 0, and the gas distribution pipe Q is connected to multiple sets of cold pipes b, and the cold pipe bi can It is a U-shaped pipe. The other end of the U-shaped pipe is open. The air distribution pipe Q is connected to the air intake pipe S. The air intake pipe S passes through the partition plate J to communicate with the upper and lower gas distribution chambers Q of the partition plate. The air inlet pipe S passes through the opening of the shell P, and the cold pipe can be supported on the cylinder wall P by the support plate T. The lower external cooling reactor has a heat exchange tube group Cd. The heat exchange tube group Cd can be a straight tube as shown in FIG. The difference is that the header in the heat exchange tube group Cd is connected to the outlet pipe E, and the pipe E communicates with the outlet through the upper reactor catalyst and the partition plate J. A catalyst K is installed between the upper and lower cold pipe tubes Cb, the heat exchange tube group Cd and the shell P. The catalyst forms a continuous bed and is supported by a porous grid R at the bottom. There is an air inlet G at the top of the reactor and an air outlet G at the bottom. _2, the synthesis gas into the reactor from the top of the intake port G _1, through an intake pipe separator S through an upper cooling tube J bile duct Cb to the Q points evenly distributed to each of the ϋ-shaped cold-tube, the outer tube in the absorbent catalyst layer The heat of reaction rises to about 200 ° C. From the upper end of the U-shaped cold tube 1 ^, the cold tube exits into the catalyst layer and flows downward. While reacting, heat is transferred to the gas in the cold tube until the internal cold reaction layer is released. The catalyst enters the catalyst in the lower external cooling reaction layer, and continues to flow downward. Here, the reaction heat is transferred to the coolant boiler in the heat exchange tube group Cd to boil water to generate steam to recover heat. Until the bottom, the reaction gas passes through the G ₂ outlet. After being heated to about 20 CTC, the boiler feed water enters the branch pipe C from the inlet pipe a and is divided into the cold pipes b _{2. The} generated steam is collected by the gas collecting pipe d and flows out through the outlet pipe E. The number of the heat exchange tube groups Cd in the above-mentioned FIG. 3 to FIG. 5 can be increased according to the increase of the reactor diameter. ·

 In addition to the reactor with a combination of internal and external cooling formed by a straight tube at the lower external cooling tube as shown in Fig. 5, the heat exchange tube group can also be a coil tube, a spiral tube and a plurality of U-shaped elbows. When there are multiple U-shaped elbows, the structure of this combined internal and external cooling reactor is shown as reactor 1 in Figure 2. The internal cooling self-heating structure of the upper part is similar to that of Figure 5, and the lower part is a U-shape with multiple elbows. The tube group is fed from the lower water inlet pipe 14 and the boiler water enters the stern tube to absorb the reaction heat outside the tube and boil it. The generated steam flows out through the side outlet pipe 15.

Fig. 6 is a radial reactor composed of an external cooling type and an internal cooling type coaxial set. The outer part is a self-heating and internal cooling type, and the inner part is an external cooling type. A porous shunt wall L is provided near the inner wall P of the cylinder. Porous header m. The reactor has the same pressure-containing shell p, and the inner self-heating reactor shell has an internal cooling cold tube bladder Cb, the cold tube bladder Cb has a gas distribution pipe, a gas collecting pipe Q ₂ , and the gas distribution pipe is connected to multiple sets of cold pipes bu cold pipe branch The down-going cold pipe and the up-going cold pipe, the down-going cold pipe is connected to the air distribution pipe and the gas collecting pipe, the end of the up-going cold pipe is connected to the lower loop pipe Q ₂ and one end is open. The shunt pipe is connected to the intake pipe S, and the inner and outer cooling reactors have a heat exchange pipe group Cd, and the header tube in the heat exchange pipe group Cd is connected to the exhaust pipe E, the shunt pipe is connected to the intake pipe, and multiple sets of cold pipes b is connected to the shunt tube ^ and the header. A catalyst K is installed between the shunt wall L, the inner and outer cooling tube Cb of the header, and the heat exchange tube group Cd. There is an air inlet G ₁₅ at the top of the reactor, and an air outlet G ₂ at the bottom. The cold catalyst layer K reacts in a radial flow from L to m.

 The invention can also be applied to a multi-step reaction of raw material gas, for example, synthesis of dimethyl ether from synthesis gas. A methanol catalyst is installed in the former self-heating reactor to make the synthesis gas react to form methanol. A methanol dehydration catalyst is installed in the latter reactor. Then, methanol is formed into dimethyl ether, and for example, gasoline is produced indirectly by using a synthesis gas. In a former self-heating reactor, a bifunctional catalyst is used to react the synthesis gas to produce methanol and dimethyl ether. The latter is charged in an external cooling reactor. For example, a zeolite catalyst methanol dimethyl ether mixture is converted into gasoline. ...

 By adopting the invention, the synthetic reaction gas enters and exits the reactor at one time. The equipment structure is simple and reliable. The catalyst is installed outside the heat exchange tube. The catalyst loading factor is larger than that of the Lurgi shell and tube and the Japanese SPC. The area of the heat exchanger is adjusted flexibly with the inlet coolant temperature of the external cooling reactor and reduces the temperature at the rear of the reaction to increase the synthesis rate. Examples

Methanol is synthesized from hydrogen and carbon oxide raw material gas, and the synthesis pressure is 7 MPa. The combined reactor uses domestic NC306 copper-based methanol catalyst 20M ³ , of which 12M ³ in the internal cooling reactor and 8M ³ in the external cooling reactor. The inlet gas is 982Kmol / h. The composition of the inlet and outlet gas is shown in the table below.

It can be seen from the table that when using the present invention, the composition is shown in No. 1, CH ₃ 0H from the methanol column is 10. 4%, and the output is 600 tons / day. Under the gas volume and composition conditions, the CH ₃ 0H of the methanol column was 8. 26%, and the methanol output was 503 tons / day, and the output of the present invention was increased by 19%.

Claims

Rights request 1. An apparatus for pressurized catalytic reaction, comprising: a reactor (1), a heat exchanger (2, 3, 4), a separator (5), and a compression cycle machine (6);  The reactor (1) includes a connected self-heating internal cooling reactor (1A) and an external cooling reactor (1B). The self-heating internal cooling reactor (1A) is composed of a pressure-containing casing (P) and It consists of a cold tube (Cb) composed of heat exchange tubes (bj) in which the gas in the tube can flow up and down in different directions. A catalyst (K) is placed outside the cold tube (Cb). ;  The external cooling reactor (1B) is composed of a pressure-containing shell (P) and a heat exchange tube group (Cd), and a catalyst (K) is placed outside the heat exchange tube group (Cd), and the inside and outside of the heat exchange tube are not connected;  The gas outlet of the reactor (1) is connected with the heat exchanger (2), the heat exchanger (3), the heat exchanger (4), the separator (5), the compression cycle machine (6), and The air inlets of the heater (3) and the reactor (1) are connected. The device according to claim 1, characterized in that the heat exchange tube group (Cd) of the externally cooled reactor (1B) is composed of one or more groups of cold tube biliary tubes (Cd Cd ₂ ...). The shaft set consists of each set of cold pipe bile ducts (Cd consists of the coolant inlet pipe, the lower ring pipe which is the shunt pipe (d) and the cold pipe (b), the upper ring pipe which is the header pipe ()), the outlet pipe, and the inlet pipe ( ) Is connected to the lower ring pipe (d), the outlet pipe (EJ and the upper ring pipe (d), and the cold pipe (b) is connected to the upper and lower ring pipes (), (d)).  The device according to claim 1 or 2, characterized in that the externally cooled reactor (1B) is near the inner wall (P) of the cylinder and has a porous shunt wall (U, L upper end portion and the outer shell (P)) A circular annular gas inlet channel is formed, with a porous gas collecting tube (m) in the center, and the gas reacts in a radial flow from (L) to (m) in the catalyst layer (K).  4. The device according to claim 1, characterized in that the upper part of the reactor (1) is a self-heating internal cooling reactor (1A), and the lower part is an external cooling reactor (IB). A pressure-containing shell (P); the upper self-heating and internal cooling reactor (1A) has an internal cooling tube (Cb) inside the casing, and a cold tube (Cb) has a gas distribution pipe (Q) and a gas distribution pipe (Q ) Connect multiple sets of cold pipes (bj, cold pipe (b is a U-shaped pipe, the other end of the U-shaped pipe is open, the air distribution pipe (Q) is connected to the air intake pipe (S), and the air intake pipe (S) passes through the partition plate (J ) The air distribution chamber above the partition and the gas distribution tube (Q) below, the tube (S) and the partition (J) are sealed by a stuffing box, and the cold tube can be supported on the wall (P) by the support plate (T). ; The lower external cooling reactor (1B) has a heat exchange tube group (Cd), and the header in the heat exchange tube group (Cd) is connected to the air outlet tube (E), and the shunt tube (C,) is connected to the air inlet tube ( _ai ) Connection, multiple sets of cold pipes (b) are connected to the shunt pipe (d) and the collector pipe (dj, the outlet pipe (E) is connected to the outlet pipe through the upper reactor partition (J), and the upper and lower cold pipes (Cb) The catalyst (K) is installed between the heat exchange tube group (Cd) and the casing (P), The catalyst is formed into a continuous bed from the upper part to the lower part, and is supported by a porous grid plate (R) at the bottom. There is an air inlet (G _t ) at the top of the reactor and an air outlet (G ₂ ) at the bottom.  The device according to claim 4, characterized in that the lower external cooling reactor cold pipe group (Cd) is a plurality of U-shaped elbow cold pipe groups.  6. The device according to claim 1, characterized in that the reactor (1) has a porous shunt wall (L) near the inner wall (P) of the cylinder, and a porous gas collecting pipe (m) at the center, constituting (L ) And (m) radial flow reactors with inner and outer cooling coaxial sets, the outer part is a self-heating inner cooling reactor (1A), the inner part is an outer cooling reactor (1B), the reactor (1A) and (IB) have the same pressure shell (P); The outer autothermal reactor unit (1A) cold inner bladder tube (Cb) inside the housing, cooling tube bile (Cb) took part in the trachea (QJ, manifold (Q _2), sub-tube (connecting a plurality of sets of cold QJ The pipe (bj, the cold pipe (t) is divided into a descending cold pipe and an ascending cold pipe, and the descending cold pipe (bj is connected to the gas distribution pipe (Q and the gas collecting pipe (Q ₂ )), and one end of the ascending cold pipe is connected to the lower loop pipe (Q ₂ ), Opening, the air distribution pipe is connected with the air intake pipe (S); The inner external cooling reactor (IB) has a heat exchange tube group (Cd), and the header (d.) In the heat exchange tube group (Cd) is connected to the air outlet tube (E), and the shunt tube (d) and The air inlet pipe ( _ai ) is connected, and multiple sets of cold pipes (b) are connected to the shunt pipe (d) and the collector pipe (dj), the inner and outer cooling pipe (Cb), the heat exchange pipe group (Cd), and the shell (P) The catalyst (K) is installed in between, the gas inlet (G) at the top of the reactor, and the gas outlet (G ₂ ) at the bottom. The gas passes through the internal and external catalyst layers (K) from (L) to (m) in the radial direction. Flow reaction.  5〜0. 8。 7. The device according to any one of claims 1-4, characterized in that the amount of catalyst installed in the internal cooling reactor accounted for 0.5 to 0.8 of the total amount of catalyst installed in the reactor. - 8. The device according to claim 1, characterized in that the external-cooled reactor (IB) connected after the internal-cooled reactor (1A) is a catalyst in a heat-exchange tube for removing Shell-and-tube reactor in which the reaction heat coolant flows between the shells. 9. The device according to claim 1, characterized in that said self-heating internal cooling type (1A) and external cooling type (1B) use self-heating internal cooling type reactor (1A) as front and external cooling type reactors (1B) via the connecting line in the series manner, externally cooled reactors (1B) the reaction temperature is lower than 10- 70 ° C _o the front portion of the autothermal reactor (1A) of the reaction temperature  10. A method for performing a pressure-catalyzed reaction using the apparatus according to claim 1, comprising, in order, the following steps:  (1) The mixed raw material gas (8) absorbs the reaction heat in the catalyst layer outside the tube in the cold tube of the self-heating internal cooling reactor (1A) and enters the catalyst layer outside the tube to react to form a primary product;  (2) allowing the primary product to enter an external cooling reactor (1B) for further reaction, removing a reaction heat with a coolant during the reaction, adjusting a reaction temperature, and forming a reaction mixture;  (3) isolating a product from the reaction mixture.