A method and device for improving HCl conversion rate in cracking of high-boiling-point mixture of organic silicon

Abstract

The present invention provides a method and device for improving the conversion rate of HCl in the cracking of a high-boiling-point mixture of organic silicon. A reaction structure is added during the cracking process, and an external circulation of liquid materials is formed between reaction containers, so as to improve the conversion rate of HCl in the cracking of a high-boiling-point mixture of organic silicon.

Description

Technical Field

[0001] The invention relates to a method and a device for preparing an organosilicon product, in particular to a method and a device for cracking an organosilicon high-boiling-point mixture. Technical Background

[0002] High-boiling-point organic silicon mixture is one of the main by-products of upstream organic silicon monomer production, accounting for about 3% of monomer production capacity. It has a complex composition, mainly Si-Si, Si-C-Si, Si-O-Si and other bond energy structures, a normal pressure density of about 1.13g / ml, a boiling range of 100-240℃, and occasionally carries a small amount of solid particles such as silicon and copper. It is a brown or yellow liquid, which easily reacts with moisture in the air to generate corrosive hydrogen chloride gas. It cannot be treated by simple methods and belongs to the category of hazardous chemical waste. If it is not treated in time, it will inevitably cause extremely serious impacts on the environment, and further affect the normal production of organic silicon monomer enterprises. One of the traditional methods for treating high-boiling organic silicon is that the high-boiling-point organic silicon mixture undergoes a cracking reaction with HCl under the action of a catalyst under pressure and temperature to produce valuable organic silicon monomers.

[0003] In the prior art, in order to ensure that the high-boiling-point mixture of organic silicon reacts completely, excessive HCl is usually introduced during the reaction, and the unreacted HCl is discharged into the waste gas water washing absorption treatment system to produce acidic wastewater. This will lead to problems such as high cost and difficulty of wastewater treatment for enterprises. Summary of the invention

[0004] The present invention relates to a method and a device for improving the conversion rate of HCl in the cracking of a high-boiling-point mixture of organic silicon. A reaction structure is added during the cracking process, and an external circulation of liquid materials is formed between reaction containers, so as to improve the conversion rate of HCl in the cracking of a high-boiling-point mixture of organic silicon.

[0005] The invention provides a cracking method for a high-boiling-point organic silicon mixture, comprising: the high-boiling-point organic silicon mixture is cracked in a first reaction container in the presence of a catalyst and a cracking agent, after the cracking, the un-cracked high-boiling-point organic silicon mixture and the catalyst and HCl dissolved therein in the first reaction container are sent from the lower part of the first reaction container to a second reaction structure in the form of liquid; the cracking product and the unreacted HCl gas in the first reaction container are sent from the upper part of the first reaction container to the second reaction structure in the form of gas, and the un-cracked high-boiling-point organic silicon mixture undergoes a secondary cracking reaction in the second reaction structure; after the secondary cracking reaction, the liquid material in the second reaction structure is returned to the first reaction container, and an external circulation of the liquid material is formed between the second reaction structure and the first reaction container.

[0006] According to the present invention, the method further comprises the step of separating the products after the two cracking steps into a distillation or rectification device to obtain an organosilicon monomer.

[0007] In one embodiment of the present invention, the second reaction structure is a reaction device independent of the distillation or rectification device. In one embodiment of the present invention, the second reaction structure is a reaction structure located below the inside of the distillation or rectification device. Regardless of whether the second reaction structure is independent or embedded, in a specific embodiment of the present invention, the second reaction structure includes a liquid accumulation tray, a downcomer, a distributor, a redistributor and a packing layer arranged in sequence from top to bottom. The liquid accumulation tray, downcomer, distributor, redistributor and packing can all use structures or devices known in the art.

[0008] When the second reaction structure is an independent reaction device, it is also referred to as the second reaction device herein, which may have various appearance structures known in the art, such as a cylindrical reaction device of various sizes or specifications, in which a liquid accumulation tray, a downcomer, a distributor, a redistributor and a packing layer are arranged in sequence from top to bottom. The bottom of the second reaction device is provided with a liquid material outlet, the lower part is provided with a gas material inlet, and the upper part is provided with a gas product outlet and a liquid material inlet. The cracking product and the unreacted HCl gas in the first reaction vessel are discharged from the upper part of the first reaction vessel and enter the second reaction device through the gas material inlet at the lower part of the second reaction device; the uncracked high-boiling-point mixture of organic silicon and the catalyst and the HCl dissolved therein in the first reaction vessel are discharged from the lower part of the first reaction vessel in liquid form, enter the second reaction device through the liquid material inlet at the upper part of the second reaction device, and a secondary cracking reaction is carried out in the second reaction device. The cracking product produced by the two crackings is discharged in a gaseous state from the gas product outlet at the upper part of the second reaction device and enters a subsequent distillation or rectification device. The material that is still in liquid form after two crackings is discharged through the liquid material outlet at the bottom of the second reaction device and returns to the first reaction container, thereby forming an external circulation of the liquid material between the second reaction device and the first reaction container.

[0009] When the second reaction structure is a structure embedded in the lower part of the distillation or rectification device, the liquid accumulation tray, downcomer, distributor, redistributor and packing layer in the structure form a group of components that are relatively independent of other components in the distillation or rectification device. There is a spacing space between the component group formed by the second reaction structure and other components in the distillation or rectification device, and there is also a space between the component group formed by the second reaction structure and the bottom of the distillation or rectification device. The distillation or rectification device is provided with a liquid material outlet at the bottom, a gas material inlet at the bottom, a liquid material inlet at the middle, and a gas product outlet at the top. The gas material inlet is located below the second reaction structure, and the liquid material inlet is located above the second reaction structure. The cracking product and unreacted HCl gas in the first reaction container are discharged from the upper part of the first reaction container and enter the second reaction structure through the gas material inlet at the lower part of the distillation or rectification device; the uncracked high-boiling-point mixture of organosilicon and the catalyst and the HCl dissolved therein in the first reaction container are discharged from the lower part of the first reaction container in the form of liquid, enter the second reaction structure through the liquid material inlet at the middle part of the distillation or rectification device, and a secondary cracking reaction is carried out in the second reaction structure. The cracking products produced by the two crackings pass through the second reaction structure in a gaseous state, enter the packing layer above the inside of the distillation or rectification device, and are discharged through the gas product outlet at the top of the distillation or rectification device. The material that is still in a liquid state after the two crackings is discharged through the liquid material outlet at the bottom of the distillation or rectification device and returns to the first reaction container, thereby forming an external circulation of the liquid material between the second reaction structure and the first reaction container.

[0010] According to the present invention, the operating pressure of the cracking reaction is 0-500 KPa g, and the temperature is 110-180°C; preferably, the pressure is 300-450 KPa g, and the temperature is 140-170°C.

[0011] According to the present invention, the catalyst is an amine substance, including but not limited to: tri-n-butylamine, tri-isobutylamine, N,N-dimethylaniline, tri-n-octylamine and the like.

[0012] According to the present invention, the cleavage agent is selected from HCl.

[0013] In a preferred embodiment of the present invention, the external circulation volume of the liquid material is 5 to 10 t / h, and the height of the packing layer in the second reaction structure is 900 to 2000 mm; more preferably, the external circulation volume of the liquid material is 6 to 8 t / h, and the height of the packing layer in the second reaction structure is 1200 to 1500 mm.

[0014] In some embodiments of the present invention, the high boiling point organic silicon mixture is (CH 3 ) n Cl 3-n -Si-Si-(CH3 ) n Cl 3-n , (CH 3 ) n Cl 3-n -Si-CH 2 -Si-(CH 3 ) n Cl 3-n A mixture of substances.

[0015] In some embodiments of the present invention, the pyrolysis product is 25-40% CH 3 SiCl 3 , 20-40% (CH 3 ) 2 SiCl 2 , 0~1%(CH 3 ) 3 SiCl, 15-30% CH 3 HSiCl 2 Methylchlorosilane monomers.

[0016] According to the present invention, the method further comprises condensing the distilled or rectified organosilicon monomer and collecting it in a storage device.

[0017] In one embodiment of the present invention, a portion of the condensed organosilicon monomers is returned to the upper part of the distillation or rectification device to maintain the composition of the upper liquid of the distillation or rectification device stable.

[0018] During the reaction process of the method of the present invention, the liquid material in the lower part of the first reaction container includes the unreacted high-boiling-point organic silicon mixture, HCl dissolved therein, and the catalyst, which is discharged from the lower part of the first reaction container and sent to the second reaction structure. After the secondary cracking reaction in the second reaction structure, it flows back to the first reaction container through the pipeline, forming an external circulation of the liquid material between the first reaction container and the second reaction structure. The product of the cracking reaction in the first reaction container, the methylchlorosilane organic silicon monomer, is entrained with the unreacted HCl gas and sent to the second reaction structure to undergo the secondary reaction with the externally circulated material.

[0019] The present invention also provides a cracking device for cracking the high-boiling-point mixture of organic silicon, comprising: a first reaction container and a second reaction structure; the first reaction container is used for cracking the high-boiling-point mixture of organic silicon in the presence of a catalyst and a cracking agent; the second reaction structure is used for performing a secondary cracking reaction on the high-boiling-point mixture of organic silicon that has not been cracked after the cracking reaction in the first reaction container; the top of the first reaction container is connected to the bottom of the second reaction structure through a gas-phase conveying pipeline, the bottom of the first reaction container is connected to the top of the second reaction structure through a first liquid-phase conveying pipeline, and the bottom of the second reaction structure is connected to the top of the first reaction container through a second liquid-phase conveying pipeline; the first reaction container, the second reaction structure and the two liquid-phase conveying pipelines form an external circulation structure for liquid materials.

[0020] According to the present invention, the device further comprises a distillation or rectification device, which is used to separate the cracking products.

[0021] In one embodiment of the present invention, the second reaction structure is a reaction device independent of the distillation or rectification device. In one embodiment of the present invention, the second reaction structure is a reaction structure located at the lower part of the distillation or rectification device. Regardless of whether the second reaction structure is independent or embedded, in a specific embodiment of the present invention, the second reaction structure includes a liquid accumulation tray, a downcomer, a distributor, a redistributor and a packing layer arranged in sequence from top to bottom. The liquid accumulation tray, downcomer, distributor, redistributor and packing can all use structures or devices known in the art.

[0022] When the second reaction structure is an independent reaction device, it is also referred to as the second reaction device herein, and it can have various appearance structures known in the art, such as a cylindrical reaction device of various sizes or specifications, in which a liquid accumulation tray, a downcomer, a distributor, a redistributor and a packing layer are arranged in sequence from top to bottom. The bottom of the second reaction device is provided with a liquid material outlet, the lower part is provided with a gas material inlet, and the upper part is provided with a gas product outlet and a liquid material inlet. The gas material inlet is connected to the aforementioned gas phase conveying pipeline, the liquid material inlet is connected to the aforementioned first liquid phase conveying pipeline, and the liquid material outlet is connected to the aforementioned second liquid phase conveying pipeline.

[0023] When the second reaction structure is a structure embedded in the lower part of the distillation or rectification device, the liquid accumulation plate, downcomer, distributor, redistributor and packing layer in the structure form a group of components that are relatively independent of other components in the distillation or rectification device. There is a spacing space between the component group formed by the second reaction structure and other components in the distillation or rectification device, and there is also a space between the second reaction structure and the bottom of the distillation or rectification device. The bottom of the distillation or rectification device is provided with a liquid material outlet, the lower part is provided with a gas material inlet, the middle part is provided with a liquid material inlet, and the upper part is provided with a gas product outlet. The gas material inlet is located below the second reaction structure, and the liquid material inlet is located above the second reaction structure. The gas material inlet is connected to the aforementioned gas phase conveying pipeline, the liquid material inlet is connected to the aforementioned first liquid phase conveying pipeline, and the liquid material outlet is connected to the aforementioned second liquid phase conveying pipeline.

[0024] According to the present invention, the device further comprises a condenser, which is connected to the top of the distillation or rectification device.

[0025] According to the present invention, the device further comprises a storage device for the organosilicon monomer, the storage device being connected to the condenser to receive the organosilicon monomer condensed after distillation or rectification separation. In one embodiment of the present invention, the storage device is connected to the upper part of the distillation or rectification device, and a part of the organosilicon monomer in the storage device is delivered to the distillation or rectification device by a pumping device.

[0026] In the present invention, unless otherwise specified, the pressure is gauge pressure.

[0027] The technical effects of the present invention are:

[0028] 1. The present invention increases the time-space yield by providing a second reaction structure, forming an external circulation of liquid material between the first reaction structure and the second reaction structure, and further forming a secondary reaction space.

[0029] 2. A secondary reaction is formed through the second reaction structure, so that the high-boiling-point organic silicon mixture reacts again with the unreacted HCl in the first reaction container, thereby improving the HCl conversion rate. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] Figure 1 It is a schematic diagram of the structure of the present invention, wherein: 1. high boiling point mixture feed; 2. reactor; 3. distillation tower; 4. top condenser; 5. reflux tank; 6. reflux pump; 7. reaction circulation pump; 8. output discharge; 9. cracking reaction layer; 10. reactor gas phase pipe; 11. reactor liquid phase pipe (i.e., second liquid phase transport pipe).

[0031] Figure 2 for Figure 1A partial enlarged view of the device in the figure is used to show the structural schematic diagram of the cracking reaction layer 9; wherein: 7, reaction circulation pump; 12, first liquid phase delivery pipe; 13, liquid accumulation tray; 14, downcomer; 15, distributor; 16, redistributor; 17, packing layer. DETAILED DESCRIPTION

[0032] Attached Figure 1 and attached Figure 2 This is an example of a specific embodiment of the method and device of the present invention, in which the second reaction structure is a structure embedded in the distillation device.

[0033] The top of the reactor 2 (i.e., the first reaction vessel) is provided with a high boiling point mixture feed 1, a feed inlet for hydrochloric acid and a catalyst, and an outlet for cracking products and HCl gas, which is connected to the lower part of the distillation tower 3 (i.e., the distillation device) through a reactor gas phase pipe 10.

[0034] A cracking reaction layer 9 (i.e., a second reaction structure) is provided at the lower part of the distillation tower 3, and the cracking reaction layer 9 includes a liquid accumulation tray 13, a downcomer 14, a distributor 15, a redistributor 16, and a packing layer 17 arranged in sequence from top to bottom. A liquid material inlet is provided in the middle of the distillation tower above the cracking reaction layer 9, and the first liquid phase delivery pipe 12 delivers the liquid material discharged from the bottom of the reactor 2 to the cracking reaction layer 9 via the inlet. A distillation product outlet is provided at the top of the distillation tower 3, and the outlet is connected to the top condenser 4 through a pipeline, and the top condenser 4 is connected to the reflux tank 5, and the reflux pump 6 connects the reflux tank 5 and the upper part of the distillation tower 3.

[0035] The reaction circulation pump 7 is connected to the bottom of the reactor 2 and the liquid material inlet above the cracking reaction layer 9. The bottom of the distillation tower 3 and the top of the reactor 2 are connected through the reactor liquid phase pipe 11.

[0036] Organic silicon high boiling point mixture feed 1 (a high boiling point mixture (CH 3 ) n Cl 3-n -Si-Si-(CH 3 ) n Cl 3-n , (CH 3 ) n Cl 3-n -Si-CH 2 -Si-(CH 3 ) n Cl 3-nThe pyrolysis product and HCl gas are sent to the distillation tower 3 through the gas phase pipe 10 of the reactor to be separated. The distillation product is sent from the top of the distillation tower 3 to the top condenser 4 for condensation. The obtained top condensate is sent to the reflux tank 5 for storage. A part of the top condensate is discharged as the output 8 (the main component is methylchlorosilane monomer, containing 25-40% CH 3 SiCl 3 , 20-40% (CH 3 ) 2 SiCl 2 , 0~1%(CH 3 ) 3 SiCl, 15-30% CH 3 HSiCl 2 The other part is refluxed to the upper part of the distillation tower 3 through the reflux pump 6 as reflux liquid, so that the liquid composition on the distillation tower plate remains stable.

[0037] The lower part of the reactor 2 contains unreacted materials, including un-cracked high-boiling-point organic silicon mixture, HCl and catalyst. The materials are discharged from the bottom of the reactor 2 in liquid form and transported to the cracking reaction layer 9 through the reaction circulation pump 7. A secondary reaction occurs in the cracking reaction layer 9. The unreacted high-boiling-point organic silicon mixture flows back to the reactor 2 through the reactor liquid phase pipe 11, forming an external circulation of liquid materials. The cracking product methylchlorosilane carries unreacted HCl gas from the reactor gas phase pipe 10 to the cracking reaction layer for secondary reaction with the external circulating materials. As the reaction proceeds, the un-cracked high-boiling-point mixture in the reactor 2 gradually accumulates. When the cracking operating pressure rises, the reaction is determined to be over. The reaction time for one batch is 96 to 168 hours.

[0038] In actual implementation, the external circulation of liquid materials prevents the high-boiling-point mixture in the reactor from reacting in dead corners; the unreacted HCl reacts again in the cracking reaction layer to increase the HCl conversion rate. The following is the data of the actual production of the cracking process of this application:

[0039]

[0040] After multiple implementations and verifications, the cracking effects are basically the same and stable when the cracking pressure is 0-500KPa and the temperature is 110-180℃. Considering the operating cost and HCl conversion rate, the best operation is achieved when the liquid material external circulation volume is 6-8t / h and the packing layer height is 1200-1500mm.

Claims

1. A method for cracking a high-boiling-point mixture of organosilicon, characterized in that: The high-boiling-point organic silicon mixture undergoes a cracking reaction in the first reaction vessel in the presence of a catalyst and a cracking agent. After the cracking, the uncracked high-boiling-point organic silicon mixture and the catalyst and HCl dissolved therein in the first reaction vessel are sent from the lower part of the first reaction vessel to the second reaction structure in the form of liquid; the cracking product and the unreacted HCl gas in the first reaction vessel are sent from the upper part of the first reaction vessel to the second reaction structure in the form of gas, and the uncracked high-boiling-point organic silicon mixture undergoes a secondary cracking reaction in the second reaction structure; after the secondary cracking reaction, the liquid substance in the second reaction structure is returned to the first reaction vessel, and an external circulation of the liquid material is formed between the second reaction structure and the first reaction vessel.

2. The cracking method according to claim 1, characterized in that: The method also includes the step of separating the products after the two cracking steps into a distillation or rectification device to obtain an organosilicon monomer.

3. The cracking method according to claim 2, characterized in that: The second reaction structure is a reaction device independent of the distillation or rectification device; or, the second reaction structure is a reaction structure located at the lower part of the distillation or rectification device.

4. The cracking method according to claim 3, characterized in that: The second reaction structure includes a liquid accumulation tray, a downcomer, a distributor, a redistributor and a packing layer which are arranged in sequence from top to bottom.

5. The cracking method according to claim 3, characterized in that: The second reaction structure is an independent reaction device, called the second reaction device, wherein a liquid accumulation tray, a downcomer, a distributor, a redistributor and a packing layer are arranged in sequence from top to bottom inside the second reaction device, a liquid material outlet is arranged at the bottom, a gas material inlet is arranged at the lower part, and a gas product outlet and a liquid material inlet are arranged at the upper part; The cracked product and unreacted HCl gas in the first reaction vessel are discharged from the upper part of the first reaction vessel and enter the second reaction device through the gas material inlet at the lower part of the second reaction device; the uncracked high-boiling-point mixture of organic silicon and the catalyst and the HCl dissolved therein in the first reaction vessel are discharged from the lower part of the first reaction vessel in the form of liquid and enter the second reaction device through the liquid material inlet at the upper part of the second reaction device, and a secondary cracking reaction is carried out in the second reaction device; the cracked product produced by the two crackings is discharged in the form of gas from the gas product outlet at the upper part of the second reaction device; the material that is still in liquid form after the two crackings is discharged through the liquid material outlet at the bottom of the second reaction device and returns to the first reaction vessel, thereby forming an external circulation of liquid material between the second reaction device and the first reaction vessel.

6. The cracking method according to claim 3, characterized in that: The second reaction structure is a structure embedded in the lower part of the distillation or rectification device. The liquid accumulation tray, downcomer, distributor, redistributor and packing layer in the second reaction structure form a group of components that are relatively independent of other components in the distillation or rectification device. There is a spacing space between the component group and other components in the distillation or rectification device, and there is also a space between the component group and the bottom of the distillation or rectification device. The distillation or rectification device is provided with a liquid material outlet at the bottom, a gas material inlet at the lower part, a liquid material inlet at the middle part, and a gas product outlet at the upper part, wherein the gas material inlet is located below the second reaction structure, and the liquid material inlet is located above the second reaction structure; The cracking products and unreacted HCl gas in the first reaction container are discharged from the upper part of the first reaction container and enter the second reaction structure through the gas material inlet at the lower part of the distillation or rectification device; the uncracked high-boiling-point mixture of organic silicon and the catalyst and the HCl dissolved therein in the first reaction container are discharged from the lower part of the first reaction container in the form of liquid and enter the second reaction structure through the liquid material inlet in the middle part of the distillation or rectification device, and a secondary cracking reaction is carried out in the second reaction structure; the cracking products produced by the two crackings pass through the second reaction structure in the gaseous state, enter the packing layer above the inside of the distillation or rectification device, and are discharged through the gas product outlet at the upper part of the distillation or rectification device; the material that is still in liquid state after the two crackings is discharged through the liquid material outlet at the bottom of the distillation or rectification device and returns to the first reaction container, thereby forming an external circulation of liquid material between the second reaction structure and the first reaction container.

7. The lysis method according to any one of claims 1 to 6, characterized in that: The operating pressure of the cracking reaction is 0-500 KPa g, and the temperature is 110-180° C.; the catalyst is an amine substance; and the cracking agent is HCl.

8. The lysis method according to claim 7, characterized in that: The catalyst is tri-n-butylamine.

9. The lysis method according to any one of claims 1 to 6, characterized in that: The external circulation volume of the liquid material is 5-10 t / h, and the height of the packing layer in the second reaction structure is 900-2000 mm.

10. The lysis method according to claim 9, characterized in that: The external circulation volume of the liquid material is 6-8 t / h, and the height of the packing layer in the second reaction structure is 1200-1500 mm.

11. The lysis method according to claim 2, characterized in that: The method further comprises condensing the distilled or rectified organosilicon monomer and collecting it in a storage device.

12. The lysis method according to claim 11, characterized in that: A portion of the condensed organosilicon monomers is returned to the upper portion of the distillation or rectification device to maintain a stable composition of the upper layer liquid of the distillation or rectification device.

13. A cracking device for the cracking method of the high-boiling-point organic silicon mixture according to any one of claims 1 to 12, characterized in that include: A first reaction container and a second reaction structure; the first reaction container is used for performing a cracking reaction of the high-boiling-point organic silicon mixture in the presence of a catalyst and a cracking agent; The second reaction structure is used for performing a secondary cracking reaction on the organic silicon high-boiling-point mixture that has not been cracked after the cracking reaction in the first reaction container; the top of the first reaction container is connected to the bottom of the second reaction structure through a gas-phase conveying pipeline, the bottom of the first reaction container is connected to the top of the second reaction structure through a first liquid-phase conveying pipeline, and the bottom of the second reaction structure is connected to the top of the first reaction container through a second liquid-phase conveying pipeline. The first reaction container, the second reaction structure and the two liquid-phase conveying pipelines form an external circulation structure for liquid materials; The cracking device also contains a distillation or rectification device, which is used to separate the cracking products; The second reaction structure is a reaction device independent of the distillation or rectification device, or the second reaction structure is a reaction structure located below the inside of the distillation or rectification device; The second reaction structure includes a liquid accumulation tray, a downcomer, a distributor, a redistributor and a packing layer which are arranged in sequence from top to bottom.

14. The cracking device according to claim 13, characterized in that The cracking device further comprises a condenser, which is connected to the top of the distillation or rectification device.

15. The cracking device according to claim 14, characterized in that The cracking device also contains a storage device for the organic silicon monomer, which is connected to the condenser to receive the organic silicon monomer condensed after distillation or rectification separation.

16. The cracking device according to claim 15, characterized in that The storage device is connected to the upper part of the distillation or rectification device, and a part of the organosilicon monomer in the storage device is sent to the distillation or rectification device through the pumping device.

17. The cracking device according to any one of claims 13 to 16, characterized in that: The second reaction structure is an independent reaction device, called the second reaction device, wherein a liquid accumulation tray, a downcomer, a distributor, a redistributor and a packing layer are arranged in sequence from top to bottom inside the second reaction device, a liquid material outlet is arranged at the bottom, a gas material inlet is arranged at the lower part, and a gas product outlet and a liquid material inlet are arranged at the upper part; the gas material inlet is connected to the pipeline for conveying the gas phase, the liquid material inlet is connected to the first pipeline for conveying the liquid phase, and the liquid material outlet is connected to the second pipeline for conveying the liquid phase; Alternatively, the second reaction structure is a structure embedded in the lower part of the distillation or rectification device, and the liquid accumulation plate, downcomer, distributor, redistributor and packing layer in the structure form a component group that is relatively independent of other components in the distillation or rectification device. There is a spacing space between the component group and other components in the distillation or rectification device, and there is also a space between the component group and the bottom of the distillation or rectification device; a liquid material outlet is arranged at the bottom of the distillation or rectification device, a gas material inlet is arranged at the lower part, a liquid material inlet is arranged at the middle part, and a gas product outlet is arranged at the upper part, the gas material inlet is located below the second reaction structure, and the liquid material inlet is located above the second reaction structure; the gas material inlet is connected to the pipeline for conveying the gas phase, the liquid material inlet is connected to the first pipeline for conveying the liquid phase, and the liquid material outlet is connected to the second pipeline for conveying the liquid phase.

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