A synthesis device and synthesis method for synthesizing butyraldehyde by hydroformylation of propylene

Abstract

The present invention discloses a synthesis device and a synthesis method for synthesizing butyraldehyde by hydroformylation of propylene, which relates to the technical field of organic chemical industry. It includes a propylene pipeline, a synthesis gas pipeline, a hydrogen pipeline, a first reaction kettle, a second reaction kettle, a flash evaporator, an absorption tower, a stripping tower, a rectifying tower, a separator and a compressor. The propylene pipeline is communicated with the first reaction kettle, the hydrogen pipeline is connected to the synthesis gas pipeline, the synthesis gas pipeline is communicated with the first reaction kettle and the second reaction kettle. The first reaction kettle includes a first gas distributor arranged at the bottom, and the second reaction kettle includes a second gas distributor arranged at the bottom. In the present invention, a circulation pump and a cooler are arranged outside the reaction kettle for synthesizing butyraldehyde by hydroformylation of propylene, the traditional mechanical stirring is changed to fluid stirring, the vent tail gas is separated and recovered, the operation cycle of the reaction kettle is prolonged, and the shutdown maintenance cost is reduced; and the utilization rate of propane and propylene resources is improved, and the production cost is reduced.

Description

Technical Field

[0001] The present invention relates to the technical field of organic chemical industry, and specifically to a synthesis device and a synthesis method for synthesizing butyraldehyde by hydroformylation of propylene. Background Art

[0002] Butyraldehyde is an important chemical raw material, mainly used as an intermediate for resins, plasticizers, vulcanization accelerators, pesticides, etc. Butyraldehyde is mainly synthesized by hydroformylation of propylene. The traditional process for synthesizing butyraldehyde by hydroformylation of propylene (see the appendix Figure 1 ) uses mechanical stirring, and a mechanical seal must be installed on the stirrer. Due to the large volume of the stirrer, problems such as eccentricity, dynamic balance imbalance, and short service life of the mechanical seal are likely to occur, and frequent inspection and maintenance are required. On the other hand, the vent gas from the synthesis of butyraldehyde by hydroformylation of propylene contains a certain amount of propylene and propane. The traditional process is to directly discharge it to the flare system for incineration after cooling, resulting in serious waste of resources and high production costs. Summary of the Invention

[0003] In order to solve the above technical problems, the present invention provides a method and a synthesis device for synthesizing butyraldehyde by hydroformylation of propylene. Fluid stirring is used instead of mechanical stirring, which can extend the operation cycle of the reactor and reduce the cost of shutdown inspection and maintenance; the vent gas is recycled to improve the resource utilization efficiency of propane and propylene and reduce the production cost.

[0004] To achieve the above object, the present invention provides the following technical solution: A synthesis device and a synthesis method for synthesizing butyraldehyde by hydroformylation of propylene, including:

[0005] A propylene pipeline, a synthesis gas pipeline, a hydrogen pipeline, a first reaction kettle, a second reaction kettle, a flash evaporator, an absorption tower, a stripping tower, a rectification tower, a separator, and a compressor;

[0006] The propylene pipeline is connected to the first reaction kettle, the hydrogen pipeline is connected to the synthesis gas pipeline, and the synthesis gas pipeline is connected to the first reaction kettle and the second reaction kettle;

[0007] The first reaction kettle includes a first gas distributor provided at the bottom, the second reaction kettle includes a second gas distributor provided at the bottom, the top and bottom of the first reaction kettle are respectively provided with a feed inlet N3 and a feed inlet N1, and the top and bottom of the second reaction kettle are respectively provided with a feed inlet N4 and N5;

[0008] An outlet N2 is provided in the upper middle part of the first reaction kettle, and a first cooler is connected to the outlet N2 through a first circulation pump. An outlet N7 is provided in the upper middle part of the second reaction kettle, and a second cooler is connected to the outlet N7 through a second circulation pump;

[0009] An outlet N6 is provided at the top of the second reaction kettle, and the outlet N6 is connected to a flash evaporator, and the flash evaporator is also connected to a separator.

[0010] Regarding this solution, further, both the first gas distributor and the second gas distributor are three - layer gas distributors, and the opening size, quantity, and direction of the distributors are optimized to make the syngas more evenly distributed in the reaction kettle.

[0011] Regarding this solution, further, a second reaction kettle outlet gas pipeline is provided at the top of the second reaction kettle, and a compressor is also provided on the pipeline of the second reaction kettle outlet gas pipeline. The compressor is connected to the separator and the second reaction kettle.

[0012] Regarding this solution, further, the separator is provided with a pipeline connected to the absorption tower, a pipeline is provided for communication between the absorption tower and the stripping tower, a pipeline is provided for flow between the stripping tower and the rectification tower, a pipeline is provided for flow between the separator and the stripping tower, and a pipeline is also provided at the rectification tower to be connected to the propylene pipeline.

[0013] A synthesis method for synthesizing butyraldehyde by hydroformylation of propylene, and the above - mentioned synthesis device for synthesizing butyraldehyde by hydroformylation of propylene includes the following steps:

[0014] Step 1: Propylene enters the first reaction kettle through the feed port N1 via the propylene pipeline, syngas and hydrogen enter the first reaction kettle through the first gas distributor via the syngas pipeline, and the flashed circulating mother liquor enters the first reaction kettle through the feed port N3.

[0015] Step 2: After the reaction of propylene, syngas, and hydrogen in the first reaction kettle, they enter the first cooler through the discharge port N2 by the first circulation pump.

[0016] Step 3: After heat exchange in the first cooler, propylene, syngas, and hydrogen return to the first reaction kettle through the feed port N3.

[0017] Step 4: The gas is discharged from the top gas outlet of the first reaction kettle and enters the second reaction kettle through the second gas distributor.

[0018] Step 5: The liquid in the first reaction kettle enters the second reaction kettle from the bottom feed port N5 of the second reaction kettle after passing through the first circulation pump.

[0019] Step 6: The reaction liquid in the second reaction kettle enters the second cooler through the discharge port N7 by the second circulation pump.

[0020] Step 7: After heat exchange, the reaction liquid returns to the second reaction kettle through the feed port N4 provided at the top of the second reaction kettle.

[0021] Step 8: The gas in the second reaction kettle is discharged through the top gas outlet and enters the absorption tower for treatment through the second reaction kettle outlet gas pipeline.

[0022] Step 9: The reaction liquid in the second reactor enters the flash evaporator through the discharge port N6 set in the upper middle part of the second reactor. The liquid after being processed by the flash evaporator returns to the first reactor through the feed port N1, and the gas enters the separator;

[0023] Step 10: The gas discharged from the second reactor enters the absorption tower and is absorbed with mixed butyraldehyde. The gas is discharged through the outlet pipeline of the absorption tower, and the mixed liquid enters the stripping tower from the bottom of the absorption tower;

[0024] Step 11: The mixed liquid enters the stripping tower for separation. The separated propylene and propane mixture enters the distillation tower, and butyraldehyde is discharged from the bottom of the stripping tower;

[0025] Step 12: After being processed by the distillation tower, propane is discharged from the bottom discharge port, and propylene is discharged from the upper part of the distillation tower and enters the propylene pipeline;

[0026] Step 13: After being processed by the separator, the gas is compressed by a compressor and then enters the outlet pipeline of the second reactor. Part of the butyraldehyde enters the absorption tower, and part is discharged from the bottom of the separator.

[0027] Furthermore, regarding this solution, the flow rate of propylene entering the first reactor in Step 1 is controlled to be 10m - 15m / s, the flow rate of the synthesis gas and hydrogen entering the first reactor through the synthesis gas pipeline via the first gas distributor is controlled to be 20m - 50m / s, and the flow rate of propylene, synthesis gas, and hydrogen returning to the first reactor through the feed port N3 in Step 4 is controlled to be 10m - 15m / s.

[0028] Furthermore, regarding this solution, the included angle between the fluid injection angle of the feed port N1 and the feed port N3 towards the inside of the first reactor and the horizontal line is set to be 0° - 45°, and the included angles between the discharge port N2 and the feed port N3 and the horizontal plane are set to be 90° - 180°.

[0029] Furthermore, regarding this solution, a bypass line is provided on the first cooler, and flow rate adjustment control is increased. The temperature of the first reactor is controlled by adjusting the flow rate of the reaction liquid in the first cooler and the flow rate of the reaction liquid in the bypass line of the first cooler.

[0030] Compared with the prior art, the beneficial effects of the present invention are:

[0031] In the present invention, a circulation pump and a cooler are provided outside the propylene hydroformylation synthesis butyraldehyde reactor. The traditional mechanical stirring is changed to fluid stirring, the vent tail gas is separated and recovered, the operation cycle of the reactor is extended, and the shutdown maintenance cost is reduced; and the utilization rate of propane and propylene resources is improved, and the production cost is reduced;

[0032] Meanwhile, adjust the material flow rate of the inlet pipeline of propylene hydroformylation to synthesize butyraldehyde into the reactor to 10-15 m / s. The orientation of the pipe orifice of the inlet pipeline of the reactor is distributed at a certain angle. The synthesis gas enters the reactor and is distributed by a three-layer distributor. The orientation of the pipe orifice of the outlet pipeline of the reactor forms a certain angle with the orientation of the pipe orifice of the pipeline entering the reactor after circulating cooling. Change the traditional mechanical stirring to fluid stirring, and separate and recover the vented tail gas to extend the operation cycle of the reactor and reduce the shutdown and maintenance cost; and improve the utilization rate of propane and propylene resources and reduce the production cost. BRIEF DESCRIPTION OF THE DRAWINGS

[0033] Figure 1 It is a schematic structural diagram of the improved process flow of the present invention;

[0034] Figure 2 It is a schematic structural diagram of the distributor of the present invention;

[0035] Figure 3 It is a schematic structural diagram of the nozzle head in the distributor of the present invention;

[0036] Figure 4 It is a schematic cross-sectional structural diagram of the nozzle head of the present invention.

[0037] In the figure: 1. First reactor; 11. First circulation pump; 12. First cooler; 13. First gas distributor; 2. Second reactor; 21. Second circulation pump; 22. Second cooler; 23. Second gas distributor; 24. Outlet gas pipeline of the second reactor; 3. Flash evaporator; 4. Absorption tower; 41. Outlet gas pipeline of the absorption tower; 5. Desorption tower; 6. Rectification tower; 7. Separator; 8. Compressor; 9. Synthesis gas pipeline; 91. Hydrogen pipeline; 10. Propylene pipeline;

[0038] 14. Annular pipe; 15. Nozzle head; 151. Horizontal pipe; 152. Damping bearing; 153. Nozzle pipe; 154. Side plate; 155. Nut sleeve; 156. Fork-shaped opening; 157. Sleeve; 158. Outlet; 159. Plug; 160. Spring; 161. Cover plate; 162. Partition; 163. Tapered opening; 164. Hanging rod; 16. Connecting pipeline. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0039] Next, the technical solutions in the embodiments of the present invention will be clearly and completely described in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, rather than all the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative efforts shall fall within the protection scope of the present invention.

[0040] See Figure 1, an embodiment of the present invention provides a synthesis device and a synthesis method for the hydroformylation of propylene to synthesize butyraldehyde, including a first reaction kettle 1, a second reaction kettle 2, a flash evaporator 3 and an absorption tower 4. A feed inlet N1 is provided at the bottom of the first reaction kettle 1, and the feed inlet N1 is connected to a propylene pipeline 10.

[0041] A first gas distributor 13 is provided at the lower part of the first reaction kettle 1. The first gas distributor 13 is a three-layer gas distributor, and the opening size, quantity and direction are more reasonable, making the gas distribution in the reaction kettle more uniform. The gas distributor is three-layer, and the opening form of the distributor adopts an X-shaped distribution. The opening size is determined according to the liquid layer height requirement of the reaction kettle, and the opening quantity is determined according to the gas flow rate of the synthesis gas required by the production capacity. The design of the change in the production capacity of each set of devices will also change. The first gas distributor 13 is connected to a synthesis gas pipeline 9 and a hydrogen pipeline 91.

[0042] As Figure 2 shown, specifically, the first gas distributor 13 includes an annular pipe 14, a spray head 15 and a connecting pipeline 16. The connecting pipeline 16 is connected to the propylene pipeline 10;

[0043] As Figure 2 and Figure 3 shown, the spray head 15 includes a horizontal pipe 151. A nozzle pipe 153 is fixed on the surface of the horizontal pipe 151. The nozzle pipe 153 is a copper pipe and the fork-shaped opening 156 is far from the horizontal pipe 151. The fork-shaped opening 156 is in an expanding setting. Threads are provided on the surface of the nozzle pipe 153 at the fork-shaped opening 156, and a nut sleeve 155 is screwed on the threads. That is to say, the diameter at the fork-shaped opening 156 can be changed. When the nut sleeve 155 is screwed tightly towards the fork-shaped opening 156, the diameter of the opening becomes narrower. In this way, the dissipation mode of the air flow can be controlled;

[0044] As Figure 3 and Figure 4 shown, wherein, two side plates 154 are also fixed on the horizontal pipe 151. A sleeve 157 is fixed between the two side plates 154. An outlet 158 for gas dissipation is provided on the sleeve 157. The length of the sleeve 157 is between 5 cm and 30 cm. A partition 162 is provided on the inner wall of the end of the sleeve 157 close to the nozzle pipe 153. The partition 162 is used to separate both sides of the partition 162. A hole is provided in the middle of the partition 162. Among them, a plug 159 is provided in the sleeve 157. A protrusion is provided in the middle of the plug 159 and the protrusion is inserted into the hole. A cover plate 161 is provided at the end of the sleeve 157 far from the nozzle pipe 153. A hanging rod 164 is fixed at the bottom of the cover plate 161 and the hanging rod 164 slides on the inner wall of the sleeve 157. A spring 160 is provided between the cover plate 161 and the plug 159. Conical openings 163 are also provided on both sides of the partition 162 for guiding the air flow.

[0045] The first gas distributor 13 can achieve a proper mixing effect by adjusting the gas flow rate. When the liquid level in the kettle is relatively low, the opening of the first gas distributor 13 is relatively large, allowing the gas flow to directly eject from the nozzle tube 153. The force of the gas flow is not sufficient to push open the plug 159. That is to say, the gas flow will directly diffuse at the nozzle tube 153. With the cooperation of multiple nozzles 15, the gas can be evenly diffused in the liquid.

[0046] When the liquid level in the kettle is relatively high, the opening of the first gas distributor 13 is adjusted to the minimum to increase the gas flow rate. The gas ejected from the nozzle tube 153 will rapidly impact on the plug 159. Due to the high-speed impact, the plug 159 is pushed open, and the spring 160 can prevent gas from flowing back. In this case, the gas will impact upward and quickly reach the liquid surface at the top of the kettle, improving the mixing effect.

[0047] Regarding the above embodiments, it should be noted that the horizontal pipes 151 are connected by the ring pipe 14, and the horizontal pipes 151 and the ring pipe 14 are connected by damping bearings 152. This can adjust the angle of the nozzles 15 while enabling the nozzles 15 to stably output gas flow.

[0048] An outlet N2 is provided in the upper middle part of the first reaction kettle 1. The outlet N2 is connected to a first circulation pump 11. The first circulation pump 11 is connected to a first cooler 12. The first cooler 12 is connected to a feed inlet N3 provided at the top of the first reaction kettle 1. The included angle between the feed inlet N1 and the feed inlet N3 is 0° - 45°; the included angle between the outlet N2 and the feed inlet N3 is 90° - 180°. This way can form a turbulent flow at the outlet N2 and the feed inlet N3 to achieve a better stirring effect and make the material mixing more uniform. A gas outlet is provided at the top of the first reaction kettle 1; a by-pass line is provided on the first cooler 12, and the flow regulation control is increased. The temperature of the first reaction kettle 1 is controlled by adjusting the flow rate of the reaction liquid in the first cooler 12 and the flow rate of the reaction liquid in the by-pass line of the first cooler 12.

[0049] As Figure 1As shown in the figure, a feed inlet N5 is provided at the bottom of the second reactor 2. The feed inlet N5 is connected to the outlet of the first circulation pump 11. A second gas distributor 23 is provided at the lower part of the second reactor 2. The second gas distributor 23 has the same structural form as the first gas distributor 13. The second gas distributor 23 is connected to the gas outlet at the top of the first reactor 1, the synthesis gas pipeline 9 and the hydrogen pipeline 91. An outlet N7 is provided in the upper middle part of the second reactor 2. The outlet N7 is connected to a second circulation pump 21. The second circulation pump 21 is connected to a second cooler 22. The second cooler 22 is connected to the feed inlet N4 provided at the top of the second reactor 2. The included angle between the feed inlet N4 and the feed inlet N5 is 0° - 45°. A by-pass line is provided on the second cooler 22 and flow regulation and control are added. The temperature of the second reactor 2 is controlled by adjusting the flow rate of the reaction liquid in the second cooler 22 and the flow rate of the reaction liquid in the by-pass line of the second cooler 22. An outlet N6 is also provided in the upper middle part of the second reactor 2. The included angle between the outlet N6 and the feed inlet N5 is 90° - 180°. The outlet N6 is connected to a flash evaporator 3. The bottom outlet of the flash evaporator 3 is connected to the feed inlet N1 of the first reactor 1. The top outlet of the flash evaporator 3 is connected to a separator 7.

[0050] As Figure 1 shown in the figure, a gas outlet is provided at the top of the second reactor 2. The gas outlet is connected to a second reactor gas outlet pipeline 24. The second reactor gas outlet pipeline 24 is connected to an absorption tower 4. An absorption tower gas outlet pipeline 41 is provided at the top of the absorption tower 4. The absorption tower gas outlet pipeline 41 can be directly discharged to the fuel gas network for use as external supplied fuel gas, or can be returned to the hydroformylation reactor after compression treatment. The bottom outlet of the absorption tower 4 is connected to a stripping tower 5. A bottom outlet is provided at the bottom of the stripping tower 5. The upper outlet of the stripping tower 5 is connected to a rectification tower 6. A bottom outlet is provided at the bottom of the rectification tower 6. The upper outlet of the rectification tower 6 is connected to a propylene pipeline 10. The upper outlet of the separator 7 is connected to a compressor 8. The compressor 8 is connected to the second reactor gas outlet pipeline 24. The bottom outlet of the separator 7 is connected to the absorption tower 4.

[0051] An embodiment of the present invention provides a method for synthesizing butyraldehyde by propylene hydroformylation, comprising the following steps:

[0052] S1: Propylene enters the first reaction kettle 1 through the propylene pipeline 10 via the feed inlet N1. Syngas and hydrogen enter the first reaction kettle 1 through the syngas pipeline 9 via the first gas distributor 13. The flashed circulating mother liquor enters the reaction kettle through the feed inlet N3. (It should be noted that the circulating mother liquor is separated from butyraldehyde and the reaction solution by flashing after the hydroformylation synthesis of butyraldehyde. That is to say, at the start-up stage of the equipment, there is no circulating mother liquor in the first reaction kettle 1). The flow rate of propylene entering the first reaction kettle 1 is controlled at 10 m - 15 m / s, and the gas flow rate of syngas and hydrogen entering the first reaction kettle 1 through the syngas pipeline 9 via the first gas distributor 13 is controlled at 20 m - 50 m / s;

[0053] S2: After the reaction of propylene, syngas and hydrogen in the first reaction kettle 1, they enter the first cooler 12 through the discharge port N2 by the first circulation pump 11. The temperature of the first reaction kettle 1 is controlled by adjusting the flow rate of the reaction solution in the first cooler 12 and the flow rate of the reaction solution in the bypass of the first cooler 12.

[0054] S3: After heat exchange in the first cooler 12, propylene, syngas and hydrogen return to the first reaction kettle 1 through the feed inlet N3. The flow rate of propylene, syngas and hydrogen returning to the first reaction kettle 1 through the feed inlet N3 is controlled at 10 m - 15 m / s;

[0055] S4: The gas (the gas phase coming out of the top of the first reaction kettle 1 directly enters the second gas distributor 23 at the lower part of the second reaction kettle 2 as the gas feed of the second reaction kettle 2) is discharged from the gas outlet at the top of the first reaction kettle 1 and enters the second reaction kettle 2 through the second gas distributor 23;

[0056] S5: The liquid in the first reaction kettle 1 enters the second reaction kettle 2 from the bottom feed inlet N5 after passing through the first circulation pump 11. The flow rate of the liquid entering the second reaction kettle 2 from the feed inlet N5 is controlled at 10 m - 15 m / s;

[0057] S6: The reaction solution in the second reaction kettle 2 enters the second cooler 22 through the second circulation pump 21 at the discharge port N7;

[0058] S7: After heat exchange, the reaction solution returns to the second reaction kettle 2 through the feed inlet N4 provided at the top of the second reaction kettle 2. The flow rate of the heat-exchanged liquid entering the second reaction kettle 2 from the feed inlet N4 is controlled at 10 m - 15 m / s. The temperature of the second reaction kettle 2 is controlled by adjusting the flow rate of the reaction solution in the second cooler 22 and the flow rate of the reaction solution in the bypass of the second cooler 22;

[0059] S8: The gas in the second reaction kettle 2 is discharged through the top gas outlet and enters the absorption tower 4 through the second reaction kettle outlet pipeline 24 for treatment;

[0060] S9: The reaction liquid in the second reactor 2 enters the flash evaporator 3 through the discharge port N6 provided in the upper middle part of the second reactor 2. The liquid (flash mother liquor) after being processed by the flash evaporator 3 returns to the first reactor 1 through the feed port N1, and the gas enters the separator 7 from the top of the second reactor 2;

[0061] S10: The gas discharged from the second reactor 2 enters the absorption tower 4 and is subjected to absorption treatment with mixed butyraldehyde. The gas is discharged from the gas outlet pipeline 41 of the absorption tower, and the mixed liquid enters the stripping tower 5 from the bottom of the absorption tower 4;

[0062] S11: The mixed liquid enters the stripping tower 5 for separation. The separated propylene and propane mixture enters the rectification tower 6, and butyraldehyde is discharged from the bottom of the stripping tower 5;

[0063] S12: After being processed by the rectification tower 6, propane is discharged from the bottom discharge port, and propylene is discharged from the upper part of the rectification tower 6 and enters the propylene pipeline 10;

[0064] S13: After being processed by the separator 7, the gas is compressed by the compressor 8 and then enters the gas outlet pipeline 24 of the second reactor. A part of the butyraldehyde enters the absorption tower 4, and a part is discharged from the bottom of the separator 7.

[0065] Although the embodiments of the present invention have been shown and described, it will be understood by those of ordinary skill in the art that various changes, modifications, substitutions, and variations can be made to these embodiments without departing from the principles and spirit of the present invention. The scope of the present invention is defined by the appended embodiments and their equivalents.

Claims

1. A synthesis device for synthesizing butyraldehyde by hydroformylation of propylene, characterized in that, Including: Propylene pipeline (10), synthesis gas pipeline (9), hydrogen pipeline (91), first reactor (1), second reactor (2), flash evaporator (3), absorption tower (4), stripping tower (5), rectifying tower (6), separator (7) and compressor (8); The propylene pipeline (10) is communicated with the first reactor (1), the hydrogen pipeline (91) is connected to the synthesis gas pipeline (9), and the synthesis gas pipeline (9) is communicated with the first reactor (1) and the second reactor (2); The first reactor (1) includes a first gas distributor (13) arranged at the bottom, the second reactor (2) includes a second gas distributor (23) arranged at the bottom, a feed inlet N3 and a feed inlet N1 are respectively arranged at the top and the bottom of the first reactor (1), and a feed inlet N4 and N5 are respectively arranged at the top and the bottom of the second reactor (2); An outlet N2 is arranged in the upper middle part of the first reactor (1), and a first cooler (12) is connected at the outlet N2 through a first circulation pump (11). An outlet N7 is arranged in the upper middle part of the second reactor (2), and a second cooler (22) is connected at the outlet N7 through a second circulation pump (21); An outlet N6 is arranged at the top of the second reactor (2), and a flash evaporator (3) is connected at the outlet N6. The flash evaporator (3) is also connected to the separator (7); When the liquid level in the reactor is low, the opening of the first gas distributor (13) is large, allowing the gas flow to directly spray out from the nozzle pipe (153), and the gas flow will directly diffuse at the nozzle pipe (153); When the liquid level in the reactor is high, the opening of the first gas distributor (13) is adjusted to the minimum to increase the gas flow velocity. The gas impacts upward and quickly reaches the liquid level at the top surface of the reactor, improving the mixing effect; The spray head (15) includes a horizontal pipe (151). A nozzle pipe (153) is fixed on the surface of the horizontal pipe (151). The end of the nozzle pipe (153) away from the horizontal pipe (151) is a fork-shaped opening (156). The fork-shaped opening (156) is arranged in an expanded manner. Threads are arranged on the surface of the nozzle pipe (153) starting from the fork-shaped opening (156) and extending to near the horizontal pipe (151). A nut sleeve (155) is screwed on the threads; There are also two side plates (154) fixed on the horizontal pipe (151). A sleeve (157) is fixed between the two side plates (154). An outlet (158) is provided on the sleeve (157) for gas escape. A partition (162) is provided on the inner wall of one end of the sleeve (157) close to the nozzle pipe (153). The partition (162) is used to separate both sides of the partition (162). A hole is provided in the middle of the partition (162). Among them, a plug (159) is provided in the sleeve (157). A protrusion is provided in the middle of the plug (159) and the protrusion is inserted into the hole. A cover plate (161) is provided at one end of the sleeve (157) away from the nozzle pipe (153). A hanging rod (164) is fixed at the bottom of the cover plate (161) and the hanging rod (164) slides on the inner wall of the sleeve (157). A spring (160) is provided between the cover plate (161) and the plug (159). Conical openings (163) are also provided on both sides of the partition (162) for guiding the airflow.

2. The synthesis device for synthesizing butyraldehyde by hydroformylation of propylene according to claim 1, wherein: Both the first gas distributor (13) and the second gas distributor (23) are three-layer gas distributors, and the opening size, quantity, and direction of the distributors are optimized to make the syngas more evenly distributed in the reaction kettle.

3. The synthesis device for synthesizing butyraldehyde by hydroformylation of propylene according to claim 1, characterized in that: A second reaction kettle outlet gas pipeline (24) is provided at the top of the second reaction kettle (2). A compressor (8) is also provided on the pipeline of the second reaction kettle outlet gas pipeline (24). The compressor (8) is connected to the separator (7) and the second reaction kettle (2).

4. A synthesis device for synthesizing butyraldehyde by propylene hydroformylation according to claim 1, characterized in that: The separator (7) is provided with a pipeline connected to the absorption tower (4). A pipeline is provided for communication between the absorption tower (4) and the stripping tower (5). A pipeline is provided for circulation between the stripping tower (5) and the rectification tower (6). A pipeline is provided for circulation between the separator (7) and the stripping tower (5). A pipeline is also provided at the rectification tower (6) and is connected to the propylene pipeline (10).

5. A method for synthesizing butyraldehyde by hydroformylation of propylene, which uses the synthesis device for synthesizing butyraldehyde by hydroformylation of propylene according to any one of claims 1-4, characterized in that, It includes the following steps: Step 1: Propylene enters the first reaction kettle (1) through the propylene pipeline (10) via the feed inlet N1. Syngas and hydrogen enter the first reaction kettle (1) through the syngas pipeline (9) via the first gas distributor (13). The flashed circulating mother liquor enters the first reaction kettle (1) through the feed inlet N3. Step 2: After the reaction of propylene, syngas, and hydrogen in the first reaction kettle (1), they enter the first cooler (12) from the discharge port N2 through the first circulation pump (11). Step 3: After being heat-exchanged in the first cooler (12), propylene, syngas, and hydrogen return to the first reaction kettle (1) through the feed inlet N3. Step 4: The gas is discharged from the top gas outlet of the first reaction kettle (1) and enters the second reaction kettle (2) through the second gas distributor (23). Step 5: The liquid in the first reaction kettle (1) enters the second reaction kettle (2) from the bottom feed inlet N5 of the second reaction kettle (2) after passing through the first circulation pump (11). Step 6: The reaction liquid in the second reaction kettle (2) enters the second cooler (22) from the discharge port N7 through the second circulation pump (21). Step 7: After being heat-exchanged, the reaction liquid returns to the second reaction kettle (2) again from the feed inlet N4 provided at the top of the second reaction kettle (2). Step 8: The gas in the second reactor (2) is discharged through the top gas outlet and enters the absorption tower (4) through the second reactor outlet pipeline (24) for treatment; Step 9: The reaction liquid in the second reactor (2) enters the flash evaporator (3) from the discharge port N6 provided in the upper middle part of the second reactor (2). The liquid after being treated by the flash evaporator (3) returns to the first reactor (1) from the feed port N1, and the gas enters the separator (7); Step 10: The gas discharged from the second reactor (2) enters the absorption tower (4), is absorbed with mixed butyraldehyde, the gas is discharged through the absorption tower outlet pipeline (41), and the mixed liquid enters the stripping tower (5) from the bottom of the absorption tower (4); Step 11: The mixed liquid enters the stripping tower (5) for separation. The separated propylene and propane mixture enters the distillation column (6), and butyraldehyde is discharged from the bottom of the stripping tower (5); Step 12: After being treated by the distillation column (6), propane is discharged from the bottom discharge port, and propylene is discharged from the upper part of the distillation column (6) and enters the propylene pipeline (10); Step 13: After being treated by the separator (7), the gas is compressed by the compressor (8) and then enters the second reactor outlet pipeline (24). A part of the butyraldehyde enters the absorption tower (4), and a part is discharged from the bottom of the separator (7).

6. The synthesis method of synthesizing butyraldehyde by propylene hydroformylation according to claim 5, characterized in that: In the said Step 1, the flow rate of propylene entering the first reactor (1) is controlled to be 10m - 15m / s, the flow rate of the synthesis gas and hydrogen entering the first reactor (1) through the synthesis gas pipeline (9) via the first gas distributor (13) is controlled to be 20m - 50m / s, and in the said Step 4, the flow rate of propylene, synthesis gas and hydrogen returning to the first reactor (1) through the feed port N3 is controlled to be 10m - 15m / s.

7. A synthesis method for synthesizing butyraldehyde by propylene hydroformylation according to claim 5, characterized in that: The included angle between the fluid injection angle of the feed port N1 and the feed port N3 towards the inside of the first reactor (1) and the horizontal line is set to be 0° - 45°, and the included angles of the discharge port N2 and the feed port N3 with the horizontal plane are set to be 90° - 180°.

8. A method for synthesizing butyraldehyde by hydroformylation of propylene according to claim 5, characterized in that: A by - pass is provided on the said first cooler (12), and flow rate adjustment control is added. The temperature of the first reactor (1) is controlled by adjusting the flow rate of the reaction liquid of the first cooler (12) and the flow rate of the reaction liquid of the by - pass of the first cooler (12).

9. A method for synthesizing butyraldehyde by hydroformylation of propylene according to claim 5, characterized in that: In the said Step 5, the flow rate of the liquid entering the second reactor (2) from the feed port N5 is controlled to be 10m - 15m / s, and in the said Step 7, the flow rate of the heat - exchanged liquid entering the second reactor (2) from the feed port N4 is controlled to be 10m - 15m / s.

10. The synthesis method of synthesizing butyraldehyde by propylene hydroformylation according to claim 5, characterized in that: A by - pass is provided on the said second cooler (22), and flow rate adjustment control is added. The temperature of the second reactor (2) is controlled by adjusting the flow rate of the reaction liquid of the second cooler (22) and the flow rate of the reaction liquid of the by - pass of the second cooler (22).

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