Gas-liquid separation assembly, gas-liquid separation device and application and dimethyl ethylene ketone preparation method

Abstract

The application discloses a gas-liquid separation assembly, a gas-liquid separation device and application and a preparation method of dimethyl ethylene ketone, and comprises a cooling unit, a gas-liquid separation unit and a gas collecting unit which are arranged in a nested mode from inside to outside; wherein the gas-liquid separation unit and the cooling unit make the gas-liquid mixture to be separated pass through the cooling unit to be cooled and simultaneously perform gas-liquid separation to obtain a gas phase and a liquid phase; the gas collecting unit is used for collecting the gas phase, and the gas-liquid separation unit is provided with a liquid collecting part which is used for collecting the liquid phase. The application has the advantages of in-situ cooling and gas-liquid separation.

Description

Technical Field

[0001] This invention relates to the field of gas-liquid separation technology, specifically to a gas-liquid separation component, a gas-liquid separation device and its application, and a method for preparing dimethyl ketene. Background Technology

[0002] Dimethyl ketone (DMK) is the starting material for the preparation of 2,2,4,4-tetramethyl-1,3-cyclobutanediol (CBDO). CBDO, due to its unique four-membered ring, possesses excellent rigidity. With increasing CBDO monomer content, the glass transition temperature (Tg) of CBDO-modified polyesters significantly increases, making it an excellent member of the high-temperature resistant polyester family. Simultaneously, this copolyester exhibits superior transparency, making it widely used in food packaging, such as drinking water cups. Compared to traditional polycarbonate (PC), CBDO-modified PCTG copolyester does not contain bisphenol A (BPA), greatly improving its food safety. Industrially, DMK is mostly produced through the thermal decomposition of isobutyric acid or isobutyric anhydride, a process with drawbacks such as poor stability and susceptibility to side reactions.

[0003] In traditional chemical processes, cooling and gas-liquid separation are two separate operations. This increases the complexity of the entire process and also increases the investment and floor space required for the equipment. Furthermore, the cascading effect of these two modules increases the time spent on cooling and gas-liquid separation, making it unsuitable for certain heat-sensitive systems requiring rapid separation. Summary of the Invention

[0004] The purpose of this invention is to provide a gas-liquid separation component, a gas-liquid separation device and its application, and a method for preparing dimethyl ketene, which has the advantages of in-situ cooling-gas-liquid separation. Furthermore, using the device of this invention in the production process of dimethyl ketene can significantly improve the process yield.

[0005] During the research process, the applicant of this application discovered that the industrial production of DMK is mostly achieved through the thermal decomposition of isobutyric acid or isobutyric anhydride. This process presents two main challenges: 1) DMK consists of a direct connection between carbon-carbon and carbon-oxygen double bonds, resulting in poor stability at high temperatures; 2) DMK reacts instantaneously upon contact with acidic substances. These factors necessitate rapid cooling and concentration of DMK after the thermal decomposition reaction.

[0006] To address the aforementioned problems, the present invention provides a gas-liquid separation assembly, comprising a cooling unit, a gas-liquid separation unit, and a gas collection unit nested from the inside out; wherein,

[0007] The gas-liquid separation unit and the cooling unit enable the gas-liquid mixture to be separated to be cooled by the cooling unit while the gas-liquid mixture is separated into a gas phase and a liquid phase.

[0008] The gas collection unit is used to collect the gas phase, and the gas-liquid separation unit has a liquid collection section for collecting the liquid phase.

[0009] A second aspect of the present invention provides a gas-liquid separation device, which includes at least one gas-liquid separation component as described in the present invention;

[0010] Preferably, the gas-liquid separation device includes a gas-liquid separation tank, at least one of the gas-liquid separation components is horizontally installed in the gas-liquid separation tank, and the cooling unit has a channel for the flow of heat exchange medium.

[0011] The application of the gas-liquid separation component or gas-liquid separation device of the present invention in the preparation of ketene compounds is preferably applied in the preparation of dimethyl ketene.

[0012] This invention provides a method for preparing dimethyl ketene. The method includes separating a gas-liquid mixture containing dimethyl ketene after reaction using the gas-liquid separation device described in this invention. The gas-liquid mixture is passed into a gas-liquid separation unit, and a heat exchange medium is passed into a cooling unit, so that the gas-liquid mixture is cooled while being separated into a liquid phase and a gas phase containing dimethyl ketene.

[0013] Through the above technical solution, gaseous materials can achieve simultaneous cooling and gas-liquid separation in the device of this invention, which greatly reduces the possibility of contact between gas and liquid materials and realizes the in-situ cooling-gas-liquid separation process. Applying this invention to the industrial production of ketene and dimethyl ketene can greatly improve the process yield and simplify the process. Attached Figure Description

[0014] Figure 1 This is a schematic diagram of the gas-liquid separation component according to a specific embodiment of the present invention;

[0015] Figure 2 yes Figure 1 Radial section view;

[0016] Figure 3 yes Figure 1 Schematic diagram of the cross-sectional structure of the gas-liquid separation layer;

[0017] Figure 4 This is a schematic diagram of the gas-liquid separation device according to a specific embodiment of the present invention;

[0018] Figure 5 This is a diagram of the apparatus for comparison with Example 1;

[0019] Figure 6 This is a diagram of the apparatus for Comparative Example 2.

[0020] Explanation of reference numerals in the attached figures

[0021] 1. Gas-liquid separator; 2. Gas-liquid separation assembly; 21. Cooling medium layer; 22. Gas-liquid separation layer; 23. Gas collection layer; 221. Liquid collection section; 222. Separation section. Detailed Implementation

[0022] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0023] In this invention, unless otherwise stated, directional terms such as "upper," "lower," "top," and "bottom" are generally used to describe the relative positions of components in relation to the directions shown in the accompanying drawings or in relation to the vertical, perpendicular, or gravitational directions; "inner" and "outer" generally refer to the interior or exterior of the cavity relative to the inner chamber or the radial interior or exterior relative to the center of the circle.

[0024] This invention discloses a gas-liquid separation component, such as... Figures 1-3 As shown, the gas-liquid separation assembly includes a cooling unit, a gas-liquid separation unit, and a gas collection unit nested from the inside out.

[0025] The gas-liquid separation unit and the cooling unit enable the gas-liquid mixture to be separated to be cooled by the cooling unit while the gas-liquid mixture is separated into gas phase and liquid phase; the gas collection unit is used to collect the gas phase, and the gas-liquid separation unit has a liquid collection section 221 for collecting the liquid phase.

[0026] In some embodiments of the present invention, such as Figures 1-3 As shown, the cooling unit includes a cooling medium layer 21, the gas-liquid separation unit includes a gas-liquid separation layer 22, and the gas collection unit includes a gas collection layer 23. The cooling medium layer 21 is covered by the gas-liquid separation layer 22, and the gas-liquid separation layer 22 is covered by the gas collection layer 23, forming an auxiliary cooling unit. Figure 2 The concentric enclosure shown in the diagram allows for simultaneous cooling and separation of the gas-liquid mixture to be separated by passing it through the gas-liquid separation layer 22 and cooling it through the heat exchange of the cooling medium layer 21. This configuration is suitable for heat-sensitive systems that require rapid separation.

[0027] In some embodiments of the present invention, the cooling medium layer 21, the gas-liquid separation layer 22, and the gas collecting layer 23 are each cylindrical in shape. The diameter R2:R1 of the gas-liquid separation layer 22 is between 1.2 and 3, preferably 1.5 to 2.5; the diameter R3:R2 of the gas collecting layer 23 is between 1.05 and 2, preferably 1.05 to 1.5. The diameter of the cooling medium layer 21 is denoted as R1, the diameter of the gas-liquid separation layer 22 as R2, and the diameter of the gas collecting layer 23 as R3. This provides the advantage of in-situ cooling and gas-liquid separation.

[0028] In some embodiments of the present invention, such as Figure 3 As shown, the gas-liquid separation unit includes a separator (the separator can be selected from at least one of porous stainless steel plate and porous PTFE plate; in this embodiment, porous PTFE plate is used as an example to illustrate the advantages of the invention, but the invention is not limited thereto). The separator is used to divide the gas-liquid separation layer 22 into a liquid collection section 221 and a separation section 222 for gas-liquid separation. The liquid collection section can be configured as a cavity with a liquid storage function. Preferably, when the gas-liquid separation assembly 2 is placed horizontally, the liquid collection section 221 is located below the separation section 222, and the cross-section (radial section) of the liquid collection section 221 is fan-shaped, wherein the central angle α of the cross-section of the liquid collection section 221 is 90–270°, preferably 90–180°. This provides the advantage of real-time collection of the liquid phase.

[0029] It should be noted that the gas collecting layer 23 can be configured as a cavity formed by a shell with a gas storage function. This shell is connected to the gas-liquid separation layer 22, or it can be fitted over the gas-liquid separation layer 22 to collect the separated gas phase. The separation part 222 of the gas-liquid separation layer 22 can be configured as a support body consisting of upper and lower layers and a gas-liquid separation membrane located between the upper and lower support bodies. The present invention has no special requirements on the shape and material of the support body; its shape only needs to enable cooling and gas-liquid separation simultaneously. For example, [example of such a support body would be inserted here]. Figures 1-3 The layered arrangement shown in the diagram uses materials including, but not limited to, stainless steel perforated plates for the support. In some embodiments of the present invention, the gas-liquid separation membrane of the separation section 222 can be selected as a hydrophilic or oleophilic membrane depending on the properties of the liquid phase system to be separated. In the present invention, there are no special requirements for the hydrophilic or oleophilic membrane; commonly used hydrophilic or oleophilic membranes can be used in the present invention. The following is an illustrative description, but it does not limit the scope of the present invention. The hydrophilic membrane is selected from at least one of glass fiber, molecular sieve, or modified polyacrylonitrile; the oleophilic membrane is selected from at least one of polydimethylsiloxane, polyurethane, or modified polyvinylidene fluoride. For example, in the embodiments of the present invention, a mixture of dimethyl ketone and isobutyric acid / isobutyric anhydride, and a mixture of ketone and acetic acid / water are separated. The advantages of the present invention are illustrated by using an oleophilic polyvinylidene fluoride membrane and a hydrophilic glass fiber membrane, respectively, but the present invention is not limited thereto.

[0030] Based on the aforementioned gas-liquid separation component 2, the present invention discloses a gas-liquid separation device, which includes at least one gas-liquid separation component 2 of the present invention. In the embodiments of the present invention, the installation of three gas-liquid separation components 2 is used as an example to illustrate the advantages of the present invention, but the present invention is not limited thereto.

[0031] Preferably, such as Figures 1-4 As shown, the gas-liquid separation device includes a gas-liquid separation tank 1, at least one gas-liquid separation component 2 is horizontally installed in the gas-liquid separation tank 1, and the cooling medium layer of the cooling unit has a channel for the flow of heat exchange medium, which can achieve indirect heat exchange with the gas-liquid separation layer 22.

[0032] Specifically, in some embodiments of the present invention, such as Figure 4 As shown, multiple gas-liquid separation components 2 are horizontally spaced in a gas-liquid separation tank 1. The gas-liquid separation tank 1 is provided with a heat exchange medium inlet, a heat exchange medium outlet, a gas-liquid mixture inlet, a gas outlet, and a liquid outlet (not shown). The cooling medium layer 21 of each gas-liquid separation component has a channel connecting the heat exchange medium inlet and the heat exchange medium outlet to achieve the inflow and outflow of the heat exchange medium. In this invention, there are no special requirements for the heat exchange medium; commonly used heat exchange media can be used. The following is an illustrative description, but it does not limit the scope of the invention. In some embodiments of this invention, the heat exchange medium can be selected from demineralized water, ethanol, or Freon. The gas-liquid mixture inlet is connected to the separation section 222 of the gas-liquid separation layer 22 of each gas-liquid separation component. The gas outlet is connected to the gas collection layer 23 of each gas-liquid separation component to discharge the separated gas phase, and the liquid outlet is connected to the liquid collection section 221 of the gas-liquid separation layer 22 of each gas-liquid separation component to discharge the separated liquid phase.

[0033] The application of the gas-liquid separation component or gas-liquid separation device of the present invention in the preparation of ketene compounds is preferably applied in the preparation of dimethyl ketene.

[0034] During the research process, the applicant of this application discovered that DMK is mainly produced industrially through the thermal decomposition of isobutyric acid or isobutyric anhydride. The whole process has the following two difficulties: 1) DMK is a direct connection between carbon-carbon double bonds and carbon-oxygen double bonds, and its stability is poor at high temperatures; 2) DMK reacts instantaneously when it comes into contact with acidic substances.

[0035] To address the aforementioned problems, this invention discloses a method for preparing dimethyl ketene, based on the foregoing disclosure. This method includes using the gas-liquid separation device of this invention to separate a gas-liquid mixture containing dimethyl ketene after the reaction. The gas-liquid mixture is passed into a gas-liquid separation unit, and a heat exchange medium is passed into a cooling unit, so that the gas-liquid mixture is cooled while undergoing gas-liquid separation to obtain a liquid phase and a gas phase containing dimethyl ketene. This enables in-situ separation of the gas and liquid phases.

[0036] In some embodiments of the present invention, the reaction includes the thermal decomposition of isobutyric acid or isobutyric anhydride to produce dimethyl ketene, wherein the conditions for thermal decomposition include:

[0037] The temperature of the thermal decomposition process is 300-800℃, preferably 300-700℃;

[0038] The partial pressure of the reactants in the thermal pyrolysis process is 0.1-20 kPa, preferably 2-15 kPa;

[0039] The residence time during the thermal pyrolysis process is 0.01–10 s, preferably 0.1–2 s. It should be noted that the conditions for the thermal pyrolysis of isobutyric anhydride to produce dimethyl ketene in this embodiment of the invention are illustrated by a thermal pyrolysis temperature of 450°C, a partial pressure of isobutyric anhydride feedstock of 10 kPa, nitrogen as the remaining gas, and a residence time of 0.5 s, as examples to illustrate the advantages of the invention, but the invention is not limited thereto.

[0040] The present invention does not have any special requirements for the reaction device. A conventional reaction device that can thermally decompose isobutyric acid or isobutyric anhydride to generate dimethyl ketene can be used. The outlet of the reaction device is connected to the gas-liquid mixture inlet of the gas-liquid separator to pass the gas-liquid mixture containing dimethyl ketene into the gas-liquid separator to achieve real-time cooling and gas-liquid separation of DMK.

[0041] In some embodiments of the present invention, the residence time of the gas-liquid mixture containing dimethyl ketene after the reaction in the gas-liquid separator 1 is 0.01-10s, preferably 0.1-2s.

[0042] In some embodiments of the present invention, the final cooling temperature is -10 to 180°C, preferably -10 to 100°C.

[0043] The advantages of the present invention will be illustrated by the following examples, but the present invention is not limited thereto.

[0044] The following examples show a gas-liquid mixture containing the target product after the reaction. Figures 1-4 The gas-liquid separator 1 shown is used for separation. The gas-liquid separator 1 has a heat exchange medium inlet, a heat exchange medium outlet, a gas-liquid mixture inlet, a gas outlet, and a liquid outlet (not shown) on its body. The gas-liquid separator 1 is equipped with three gas-liquid separation components 2. The axes of the three gas-liquid separation components 2 are parallel to the axis of the gas-liquid separator 1 and are distributed at intervals.

[0045] like Figures 1-3 As shown, each gas-liquid separation assembly 2 includes a cylindrical cooling medium layer 21, a gas-liquid separation layer 22, and a gas collection layer 23 arranged from the inside out; wherein,

[0046] The cooling medium layer 21 is configured as a pipe, with each end of the pipe connected to a heat exchange medium inlet and a heat exchange medium outlet, respectively. The gas-liquid separation layer 22 is divided into a liquid collection section 221 and a separation section 222 by a separator. The separation section 222 is connected to the gas-liquid mixture inlet and is configured as a support (support frame) comprising upper and lower arc-shaped stainless steel perforated plates and a gas-liquid separation membrane located between the upper and lower support layers. The liquid collection section is configured as a cavity structure connected to the liquid outlet. Figure 3 As shown, the cavity structure and the support body are combined to form a cylindrical gas-liquid separation layer 22 that is fitted outside the cooling medium layer; the gas collection layer 23 is configured as a cavity formed by the shell, which covers the gas-liquid separation layer 22 and is connected to the gas outlet.

[0047] The method in the following embodiments includes: passing a gas-liquid mixture containing the target product into a gas-liquid mixture inlet, and passing a heat exchange medium Freon into a heat exchange medium inlet.

[0048] Example 1

[0049] The parameters of the gas-liquid separation components used in this embodiment are as follows: R2:R1 = 1.5, R3:R2 = 1.3, the central angle α of the cross-section of the liquid collection section 221 is 120°, the gas-liquid separation unit separator is a porous PTFE plate, and the gas-liquid separation membrane of the separation section 222 is a polyvinylidene fluoride membrane. Three of the above-mentioned gas-liquid separation components are installed in the gas-liquid separation device of this embodiment.

[0050] In this embodiment, the conditions for the thermal decomposition of isobutyric anhydride to produce dimethyl ketene are: thermal decomposition temperature of 450°C, partial pressure of isobutyric anhydride feedstock of 10 kPa, nitrogen as the remaining gas, and thermal decomposition residence time of 0.5 s.

[0051] In this embodiment, the final temperature of the cooling-gas-liquid separation is 30°C. After cooling-gas-liquid separation, the removal rate of AIB in the system reaches 99.31%, the removal rate of ANIB reaches 99.57%, and the recovery rate of DMK reaches 90.37%.

[0052] Example 2

[0053] The parameters of the gas-liquid separation components used in this embodiment are as follows: R2:R1 = 2, R3:R2 = 1.5, the central angle α of the cross-section of the liquid collection section (221) is 180°, the gas-liquid separation unit separator is a porous PTFE plate, and the gas-liquid separation membrane of the separation section 222 is a polyvinylidene fluoride membrane. Three of the above-mentioned gas-liquid separation components are installed in the gas-liquid separation device of this embodiment.

[0054] In this embodiment, the conditions for the thermal decomposition of isobutyric anhydride to produce dimethyl ketene are: thermal decomposition temperature of 450°C, partial pressure of isobutyric anhydride feedstock of 10 kPa, nitrogen as the remaining gas, and thermal decomposition residence time of 0.5 s.

[0055] In this embodiment, the cooling-gas-liquid separation endpoint temperature is 30°C. After cooling-gas-liquid separation, the removal rate of AIB in the system reaches 99.55%, the removal rate of ANIB reaches 99.83%, and the recovery rate of DMK reaches 85.12%.

[0056] Example 3

[0057] The parameters of the gas-liquid separation components used in this embodiment are as follows: R2:R1 = 2.5, R3:R2 = 1.1, the central angle α of the cross-section of the liquid collection section 221 is 90°, the gas-liquid separation unit separator is a porous PTFE plate, and the gas-liquid separation membrane of the separation section 222 is a polyvinylidene fluoride membrane. Three of the above-mentioned gas-liquid separation components are installed in the gas-liquid separation device of this embodiment.

[0058] In this embodiment, the conditions for the thermal decomposition of isobutyric anhydride to produce dimethyl ketene are: thermal decomposition temperature of 450°C, partial pressure of isobutyric anhydride feedstock of 10 kPa, nitrogen as the remaining gas, and thermal decomposition residence time of 0.5 s.

[0059] In this embodiment, the final temperature of the cooling-gas-liquid separation is 30°C. After cooling-gas-liquid separation, the removal rate of AIB in the system reaches 99.49%, the removal rate of ANIB reaches 99.91%, and the recovery rate of DMK reaches 92.37%.

[0060] Example 4

[0061] The parameters of the gas-liquid separation components used in this embodiment are as follows: R2:R1 = 1.2, R3:R2 = 1.8, the central angle α of the cross-section of the liquid collection section 221 is 90°, the gas-liquid separation unit separator is a porous PTFE plate, and the gas-liquid separation membrane of the separation section 222 is a polyvinylidene fluoride membrane. Three of the above-mentioned gas-liquid separation components are installed in the gas-liquid separation device of this embodiment.

[0062] In this embodiment, the conditions for the thermal decomposition of isobutyric anhydride to produce dimethyl ketene are: thermal decomposition temperature of 450°C, partial pressure of isobutyric anhydride feedstock of 10 kPa, nitrogen as the remaining gas, and thermal decomposition residence time of 0.5 s.

[0063] In this embodiment, the final temperature of the cooling-gas-liquid separation is 30°C. After cooling-gas-liquid separation, the removal rate of AIB in the system reaches 98.53%, the removal rate of ANIB reaches 98.92%, and the recovery rate of DMK reaches 80.17%.

[0064] Example 5

[0065] The parameters of the gas-liquid separation components used in this embodiment are as follows: R2:R1 = 1.2, R3:R2 = 1.8, the central angle α of the cross-section of the liquid collection section 221 is 250°, the gas-liquid separation unit separator is a porous PTFE plate, and the gas-liquid separation membrane of the separation section 222 is a polyvinylidene fluoride membrane. Three of the above-mentioned gas-liquid separation components are installed in the gas-liquid separation device of this embodiment.

[0066] In this embodiment, the conditions for the thermal decomposition of isobutyric anhydride to produce dimethyl ketene are: thermal decomposition temperature of 450°C, partial pressure of isobutyric anhydride feedstock of 10 kPa, nitrogen as the remaining gas, and thermal decomposition residence time of 0.5 s.

[0067] In this embodiment, the cooling-gas-liquid separation endpoint temperature is 30°C. After cooling-gas-liquid separation, the removal rate of AIB in the system reaches 99.25%, the removal rate of ANIB reaches 99.69%, and the recovery rate of DMK reaches 75.32%.

[0068] Example 6

[0069] The parameters of the gas-liquid separation components used in this embodiment are as follows: R2:R1 = 1.8, R3:R2 = 1.1, the central angle α of the cross-section of the liquid collection section 221 is 120°, the gas-liquid separation unit separator is a porous PTFE plate, and the gas-liquid separation membrane of the separation section 222 is a glass fiber membrane. Three of the above-mentioned gas-liquid separation components are installed in the gas-liquid separation device of this embodiment.

[0070] In this embodiment, the conditions for the thermal decomposition of acetic acid to produce ketene are: thermal decomposition temperature of 750°C, partial pressure of acetic acid feedstock of 10 kPa, nitrogen as the remaining gas, and thermal decomposition residence time of 0.7 s.

[0071] In this embodiment, the cooling-gas-liquid separation endpoint temperature is 10°C. After cooling-gas-liquid separation, the removal rate of acetic acid in the system reaches 99.72%, the removal rate of water reaches 99.84%, and the recovery rate of ketene reaches 97.31%.

[0072] Comparative Example 1

[0073] The conditions for the thermal decomposition of isobutyric anhydride to produce dimethyl ketene in this comparative example are: thermal decomposition temperature of 450℃, partial pressure of isobutyric anhydride feedstock of 10 kPa, nitrogen as the remaining gas, and thermal decomposition residence time of 0.5 s.

[0074] The reaction products were processed as follows Figure 5 The shell-and-tube heat exchanger shown is cooled to 30°C. The gas-liquid mixture at the outlet of the shell-and-tube heat exchanger is separated into gas and liquid by a cyclone separator. The removal rate of AIB in the system is 95.73%, the removal rate of ANIB is 95.29%, and the recovery rate of DMK is 36.19%.

[0075] Comparative Example 2

[0076] In this embodiment, the conditions for the thermal decomposition of acetic acid to produce ketene are: thermal decomposition temperature of 750°C, partial pressure of acetic acid feedstock of 10 kPa, nitrogen as the remaining gas, and thermal decomposition residence time of 0.7 s.

[0077] The reaction products were processed as follows Figure 6 The three-section shell-and-tube heat exchanger shown is cooled to 10°C. Each heat exchanger is followed by a gas-liquid separator. The system achieves a 98.13% removal rate for acetic acid, a 98.52% removal rate for water, and a 93.28% recovery rate for ketene.

[0078] The preferred embodiments of the present invention have been described in detail above; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various technical features in any other suitable manner. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. A gas-liquid separation component, characterized in that, The gas-liquid separation assembly (2) includes a cooling unit, a gas-liquid separation unit, and a gas collection unit nested from the inside out; wherein, The gas-liquid separation unit and the cooling unit enable the gas-liquid mixture to be separated to be cooled by the cooling unit while the gas-liquid mixture is separated into a gas phase and a liquid phase. The gas collection unit is used to collect the gas phase, and the gas-liquid separation unit has a liquid collection section (221) for collecting the liquid phase; The cooling unit includes a cooling medium layer (21), the gas-liquid separation unit includes a gas-liquid separation layer (22), and the gas collection unit includes a gas collection layer (23). The cooling medium layer (21) is covered by the gas-liquid separation layer (22), and the gas-liquid separation layer (22) is covered by the gas collection layer (23). The gas-liquid separation unit includes a separator for dividing the gas-liquid separation layer (22) into a liquid collection section (221) and a separation section (222) for gas-liquid separation. When the gas-liquid separation component (2) is placed horizontally, the liquid collection part (221) is located below the separation part (222), and the cross-section of the liquid collection part (221) is fan-shaped, wherein the central angle α of the cross-section of the liquid collection part (221) is 90~270°.

2. The gas-liquid separation assembly according to claim 1, wherein, The central angle α of the cross-section of the liquid collecting part (221) is 90~180°.

3. The gas-liquid separation component according to claim 1, characterized in that, The cooling medium layer (21), the gas-liquid separation layer (22), and the gas collecting layer (23) are each cylindrical in shape. The diameter of the cooling medium layer (21) is denoted as R1, the diameter of the gas-liquid separation layer (22) is denoted as R2, and the diameter of the gas collection layer (23) is denoted as R3; The diameter R2:R1 of the gas-liquid separation layer (22) is between 1.2 and 3; and / or The diameter of the gas collecting layer (23) R3:R2 is between 1.05 and 2.

4. The gas-liquid separation component according to claim 3, wherein, The diameter R2:R1 of the gas-liquid separation layer (22) is between 1.5 and 2.5; and / or The diameter of the gas collecting layer (23) R3:R2 is between 1.05 and 1.

5.

5. The gas-liquid separation assembly according to claim 1, characterized in that, The separation section (222) includes a hydrophilic membrane or an oleophilic membrane.

6. The gas-liquid separation assembly according to claim 5, wherein, The hydrophilic membrane is selected from at least one of glass fiber, molecular sieve, and modified polyacrylonitrile; and / or The oleophilic film is selected from at least one of polydimethylsiloxane, polyurethane, and modified polyvinylidene fluoride.

7. A gas-liquid separation device, characterized in that, The gas-liquid separation device includes at least one gas-liquid separation component (2) as described in any one of claims 1-6.

8. The gas-liquid separation device according to claim 7, wherein the gas-liquid separation device includes a gas-liquid separation tank (1), at least one of the gas-liquid separation components (2) is horizontally installed in the gas-liquid separation tank (1), and the cooling unit has a channel for the flow of heat exchange medium.

9. The application of the gas-liquid separation device according to claim 7 or 8 in the preparation of ketene compounds.

10. The application according to claim 9, wherein, This application is in the preparation of dimethyl ketene.

11. A method for preparing dimethyl ketene, characterized in that, The preparation method includes using the gas-liquid separation device as described in claim 7 or 8 to separate the gas-liquid mixture containing dimethyl ketene after the reaction, wherein the gas-liquid mixture is passed into the gas-liquid separation unit and the heat exchange medium is passed into the cooling unit, so that the gas-liquid mixture is cooled and gas-liquid separation is performed to obtain a liquid phase and a gas phase containing dimethyl ketene.

12. The preparation method according to claim 11, wherein, The resulting gas-liquid mixture containing dimethyl ketene originates from the thermal cracking reaction of isobutyric acid or isobutyric anhydride, wherein the conditions for the thermal cracking reaction include: The temperature during the thermal decomposition process is 300-800℃; The partial pressure of the reactants in the thermal pyrolysis process is 0.1-20 kPa; The residence time during the thermal decomposition process is 0.01~10s.

13. The preparation method according to claim 12, wherein, The conditions for the pyrolysis reaction include: The temperature during the thermal decomposition process is 300-700℃; The partial pressure of the reactants in the thermal pyrolysis process is 2~15 kPa; The residence time during the thermal decomposition process is 0.1~2s.

14. The preparation method according to claim 13, wherein, The residence time of the gas-liquid mixture containing dimethyl ketene after the reaction in the gas-liquid separator (1) is 0.01-10 s; and / or The final cooling temperature is -10~180℃.

15. The preparation method according to claim 14, wherein, The residence time of the gas-liquid mixture containing dimethyl ketene after the reaction in the gas-liquid separator (1) is 0.1-2 s; and / or The final cooling temperature is -10~100℃.

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