Continuous production process for perfluoropentanone

Abstract

This invention belongs to the field of perfluoropentanone preparation technology, specifically relating to a continuous production process for perfluoropentanone. The continuous production process for perfluoropentanone includes the following steps: a fluorination catalyst is loaded into a reaction tube, purged with nitrogen, and a preheated mixture of hexafluoropropylene and trifluoroacetyl fluoride is introduced into the reaction tube for continuous reaction. Part of the reacted gas is condensed to obtain the target product, perfluoropentanone, while the other part is recycled back to the mixing and preheating stage. This continuous production process for perfluoropentanone uses hexafluoropropylene and trifluoroacetyl fluoride as raw materials, and employs a one-step gas-phase continuous flow method to rapidly synthesize perfluoropentanone under the action of a MgF2-based fluorination catalyst. No solvent is required, and the trifluoroacetyl fluoride raw material is a byproduct of the preparation of hexafluoropropylene oxide, making the raw materials readily available. The process route is simple, with high conversion rate and high selectivity, facilitating large-scale industrial production.

Description

Technical Field

[0001] This invention belongs to the field of perfluoropentanone preparation technology, specifically relating to a continuous production process for perfluoropentanone. Background Technology

[0002] Perfluoropentanone, also known as perfluoro-3-methyl-2-butanone, is a new type of perfluoroketone compound. At room temperature, it is a colorless, odorless, non-flammable, easily liquefied gas / liquid. It has the characteristics of low GWP, short atmospheric lifetime, high dielectric strength, low toxicity, and good material compatibility. It is an important environmentally friendly medium to replace high GWP greenhouse gases and has broad application prospects in fields such as power insulation, clean fire extinguishing, and electronic cleaning.

[0003] The synthesis of perfluoropentanone mainly uses perfluoroolefins and acyl fluoride / perfluoroepoxy intermediates as raw materials, and is prepared by liquid-phase addition or gas-solid phase reaction. The synthesis technology of perfluoropentanone has gone through several development stages. The early laboratory stage of electrochemical fluorination and direct fluorination methods have inherent defects such as poor fluorination selectivity, frequent side reactions, low product yield, and severe corrosion to production equipment, and have never been able to achieve industrial application.

[0004] Existing synthetic techniques mainly focus on liquid-phase addition or gas-solid phase reaction preparation. CN109704935A discloses a method for preparing perfluoro-3-methyl-2-butanone, using hexafluoropropylene and trifluoroacetyl fluoride as raw materials. The reaction is carried out under the action of a liquid-phase composite catalyst consisting of a main catalyst of metal fluoride / hydrfluoride, a co-catalyst of C6-C9 perfluoroolefin, an auxiliary agent of crown ether / crown-like ether, and a polar aprotic solvent. The reaction rate is fast and the product yield is high. However, the liquid-phase batch method has the problems of complex catalyst system and non-renewable catalyst. At the same time, it requires the use of organic solvents, which leads to complicated post-processing.

[0005] CN109896936A discloses a method for preparing perfluoropentanone, which uses hexafluoropropylene and trifluoroacetyl fluoride as raw materials, adds an aprotic solvent, and reacts in the presence of alkali metal fluorides KF and / or NaF to obtain perfluoropentanone. This method is a one-pot synthesis, which eliminates the need for stepwise processing of intermediate products, reduces process steps and equipment investment, and simplifies the operation process. However, it uses KF homogeneous catalysis, the catalyst cannot be recovered and regenerated, and it requires the use of organic solvent acetonitrile, resulting in cumbersome post-processing and high energy consumption. The reaction is an intermittent high-pressure operation with a long cycle, and unreacted raw materials are difficult to recycle.

[0006] CN116037118A discloses a method for preparing perfluoro-3-methyl-2-butanone, using CXY=CH2 and 2,2-dichloro-1,1,1,3,3,3-hexafluoropropane as starting materials. The method involves multiple steps including telomerization, fluorine-chlorine exchange, isomerization, and oxidation, ultimately yielding the target product, perfluoro-3-methyl-2-butanone, via ethylene oxide isomerization. 3 methyl 2 Butanone (MEK) is produced using a gas-phase reaction mode, which is conducive to continuous production. It also features three dedicated catalytic systems: initiator, fluorination catalyst, and isomerization catalyst, which are designed to be suitable for different reaction stages such as telomerization, fluorine-chlorine exchange, and isomerization. The catalytic selectivity is high, which helps to ensure the purity of the target product. However, this method involves a multi-step reaction route, which is lengthy and involves complex raw material structures. Although it achieves continuous reaction, it is difficult to control continuously in industrial applications.

[0007] In summary, existing technologies have developed routes for the synthesis of perfluoropentanone, including one-step liquid-phase method, one-pot method, and multi-step gas-phase method, and have made some progress in terms of raw material compatibility, catalytic activity, or process simplification. However, problems still exist, such as over-reliance on aprotic solvents, low catalyst selectivity, and difficulty in achieving continuous production. Summary of the Invention

[0008] To address the shortcomings of existing technologies, the present invention aims to provide a continuous production process for perfluoropentanone. Using hexafluoropropylene and trifluoroacetyl fluoride as raw materials, perfluoropentanone is rapidly synthesized in a one-step gas-phase continuous flow under the action of a MgF2-based fluorination catalyst. No solvent is required, and the raw material trifluoroacetyl fluoride is obtained as a byproduct from the production of hexafluoropropylene oxide. The raw materials are readily available, the process route is simple, the conversion rate is high, the selectivity is high, and it is easy to scale up for industrial production.

[0009] The technical solution adopted in this invention is as follows:

[0010] A continuous production process for perfluoropentanone, the continuous production process being carried out in a tubular reactor, includes the following steps:

[0011] The fluorinated catalyst is packed into the reaction tube. After purging with nitrogen, a mixture of preheated hexafluoropropylene and trifluoroacetyl fluoride gas is introduced into the reaction tube for continuous reaction. Part of the gas after reaction is condensed to obtain the target product perfluoropentanone, and the other part is recycled back to the mixing and preheating stage.

[0012] The fluorination catalyst is a MgF2-based fluorination catalyst, which is prepared by solid-phase grinding, molding, calcination fluorination and activation treatment using anhydrous MgCl2, anhydrous Fe(NO3)3, La2O3, NH4HF2 and graphite powder as effective components.

[0013] In the tubular reactor, the bulk density of the fluorination catalyst is 0.25-0.80 g / cm³. 3 .

[0014] The continuous reaction is carried out at a pressure of 0.05-0.1 MPa and a temperature of 200-300℃.

[0015] The molar ratio of hexafluoropropylene to trifluoroacetyl fluoride is 1:(1-2), and the inlet flow rate of the mixed gas is 100-500 mL / min, preferably 120-360 mL / min.

[0016] The preparation method of the MgF2-based fluorination catalyst includes the following steps:

[0017] (1) The effective components anhydrous MgCl2, anhydrous Fe(NO3)3, La2O3, NH4HF2 and graphite powder are mixed and ground at room temperature for 4-5 hours. The mixture is then pressed into cylindrical wet particles using a mold with a pore size of 1-3 mm.

[0018] (2) The wet particles are placed in a muffle furnace and roasted under a nitrogen atmosphere. The roasting exhaust gas is absorbed by an alkaline absorbent and cooled naturally to obtain catalyst particles.

[0019] (3) Before use, the catalyst particles are transferred into a fixed bed reactor and HF / N2 mixed gas is introduced. After activation treatment, the finished MgF2-based fluorinated catalyst is obtained.

[0020] In step (1), the mass ratio of anhydrous MgCl2, anhydrous Fe(NO3)3, La2O3, NH4HF2 and graphite powder is (8-10):(0.8-0.9):(0.3-0.5):(7-9):(0.7-0.9).

[0021] In step (2), the calcination process is as follows: in the first stage, the temperature is raised to 200-250℃ at a heating rate of 2-5℃ / min and held for 1-2 hours; in the second stage, the temperature is raised to 400-500℃ at a heating rate of 2-5℃ / min and held for 6-8 hours.

[0022] In step (2), the alkaline absorbent is a sodium hydroxide aqueous solution with a concentration of 10-15 wt.%.

[0023] In step (3), the volume fraction of HF in the HF / N2 mixed gas is 5-8%, the inlet flow rate of the HF / N2 mixed gas is 30-60 mL / min, the activation temperature is 250-300℃, and the activation time is 2-4 h.

[0024] Preferably, the continuous production process of the perfluoropentanone, which is carried out in a tubular reactor, includes the following steps:

[0025] The fluorinated catalyst was loaded into DN50. In a 1000 reaction tube, the bulk density of the fluorination catalyst was controlled to be 0.25-0.80 g / cm³. 3Nitrogen gas is introduced for purging, maintaining a pressure of 0.01-0.05 MPa, and purging at 200-250℃ for 2-5 hours. The moisture content is measured to be <50 ppm. After purging, the control valves for hexafluoropropylene and trifluoroacetyl fluoride are opened, and they are mixed and preheated to 150-200℃ in a static mixer at a molar ratio of 1:(1-2). Subsequently, the inlet flow rate of the mixed gas is controlled at 120-360 mL / min, and it is introduced into the reaction tube for continuous reaction at a pressure of 0.05-0.1 MPa and a reaction temperature of 200-300℃. Part of the gas after reaction is condensed and transported to a storage tank with a back pressure of 0.3 MPa to obtain the target product perfluoropentanone. The other part is recycled back to the static mixer for mixing and preheating, with a recycling ratio of 12% of the total mass of the reaction liquid.

[0026] Preferably, the fluorination catalyst is a MgF2-based fluorination catalyst, which includes the following preparation steps:

[0027] (1) The effective components anhydrous MgCl2, anhydrous Fe(NO3)3, La2O3, NH4HF2 and graphite powder are mixed in a mass ratio of (8-10):(0.8-0.9):(0.3-0.5):(7-9):(0.7-0.9), ground at room temperature for 4-5 hours, and then pressed into cylindrical wet particles using a mold with a pore size of 2 mm.

[0028] (2) The wet particles were placed in a muffle furnace and roasted under a nitrogen atmosphere. In the first stage, the temperature was raised to 200°C at a rate of 3°C / min and held for 1 hour. In the second stage, the temperature was raised to 480°C at a rate of 5°C / min and held for 6 hours. The tail gas generated during the roasting process was absorbed by a 10wt.% sodium hydroxide aqueous solution. After the roasting was completed, the temperature was naturally cooled down to obtain catalyst particles.

[0029] (3) Before use, the catalyst particles are transferred into a fixed bed reactor, and a mixed gas of HF / N2 with a volume fraction of 8% is introduced. The gas flow rate is controlled at 40 mL / min, and the catalyst is activated at 280℃ for 2 h to obtain the finished MgF2-based fluorinated catalyst.

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

[0031] (1) The continuous production process of perfluoropentanone of the present invention uses hexafluoropropylene and trifluoroacetyl fluoride as raw materials. Trifluoroacetyl fluoride is taken from the by-product of the preparation of hexafluoropropylene oxide. It does not need to be prepared separately. This not only solves the problem of by-product disposal and reduces waste emissions, but also significantly reduces the cost of raw material procurement and preparation, realizing the recycling of resources. At the same time, the raw materials have strong compatibility and can be used directly in the reaction without complicated pretreatment, further simplifying the process flow.

[0032] (2) The continuous production process of perfluoropentanone of the present invention uses MgF2-based fluorination catalyst. The catalyst has good thermal and chemical stability. The solid catalyst is suitable for continuous flow mode, can operate stably for a long time, and can be reused. It improves the conversion rate of hexafluoropropylene and trifluoroacetyl fluoride, the selectivity of the target product, and is suitable for industrial continuous large-scale production. Attached Figure Description

[0033] Figure 1 This is a gas chromatogram of trifluoroacetyl fluoride, the raw material used in this invention;

[0034] Figure 2 This is a gas chromatogram of perfluoropentanone prepared in Example 2 of the present invention. Detailed Implementation

[0035] The technical solution of the present invention will be further described below with reference to the embodiments and comparative examples. Unless otherwise specified, the raw materials used in the embodiments and comparative examples are all conventional commercial raw materials, and the process methods used are all conventional methods in the art unless otherwise specified.

[0036] The raw materials for the examples and comparative examples are described below:

[0037] Trifluoroacetyl fluoride: a byproduct of the continuous production process of hexafluoropropylene oxide (patent CN118324721A). It is obtained through distillation purification after the reaction is complete. Before participating in the production of perfluoropentanone, the purity of trifluoroacetyl fluoride is ≥98%. Figure 1 Table 1 shows the gas chromatograms of trifluoroacetyl fluoride used in the embodiments and comparative examples of this invention. Figure 1 The corresponding gas chromatography data.

[0038] Table 1 Gas Chromatographic Data for Trifluoroacetyl Fluoride

[0039]

[0040] Example 1

[0041] The preparation method of the MgF2-based fluorination catalyst includes the following steps:

[0042] (1) The effective components anhydrous MgCl2, anhydrous Fe(NO3)3, La2O3, NH4HF2 and graphite powder were mixed in a mass ratio of 10:0.8:0.4:9:0.7, ground at room temperature for 5 hours, and then pressed into cylindrical wet particles using a mold with a pore size of 2 mm.

[0043] (2) The wet particles were placed in a muffle furnace and roasted under a nitrogen atmosphere. In the first stage, the temperature was raised to 200°C at a rate of 3°C / min and held for 1 hour. In the second stage, the temperature was raised to 480°C at a rate of 5°C / min and held for 6 hours. The roasting tail gas was absorbed by a 10wt.% sodium hydroxide aqueous solution and cooled naturally to obtain catalyst particles.

[0044] (3) Before use, the catalyst particles are transferred into a fixed bed reactor, and a mixed gas of HF / N2 with a volume fraction of 8% is introduced. The gas flow rate is controlled at 40 mL / min, and the catalyst is activated at 280℃ for 2 h to obtain the finished MgF2-based fluorinated catalyst.

[0045] The continuous production process of perfluoropentanone, carried out in a tubular reactor, includes the following steps:

[0046] The MgF2-based fluorination catalyst obtained above was loaded into a DN50 container. In a 1000 reaction tube, the bulk density of the fluorination catalyst was controlled at 0.25 g / cm³. 3 Nitrogen gas was introduced for purging, maintaining a pressure of 0.03 MPa, and purging at 200℃ for 5 hours. The moisture content was measured to be <50 ppm. After purging, the control valves for hexafluoropropylene and trifluoroacetyl fluoride were opened, and they were mixed and preheated to 150℃ in a static mixer at a molar ratio of 1:2. Subsequently, the inlet flow rate of the mixed gas was controlled at 200 mL / min, and it was introduced into the reaction tube for continuous reaction at a pressure of 0.1 MPa and a reaction temperature of 200℃. The gas after reaction was partially condensed and transported to a storage tank with a back pressure of 0.3 MPa to obtain the target product perfluoropentanone. 12% of the total mass of the reaction liquid was recycled back to the static mixer for mixing and preheating. The product was analyzed by gas chromatography, and the conversion rate of hexafluoropropylene was 99.59%, and the selectivity of perfluoropentanone was 86.91%.

[0047] Example 2

[0048] The preparation method of the MgF2-based fluorination catalyst includes the following steps:

[0049] (1) The effective components anhydrous MgCl2, anhydrous Fe(NO3)3, La2O3, NH4HF2 and graphite powder were mixed in a mass ratio of 9:0.9:0.5:8:0.8, ground at room temperature for 4.5 h, and then pressed into cylindrical wet particles using a mold with a pore size of 2 mm.

[0050] (2) The wet particles were placed in a muffle furnace and roasted under a nitrogen atmosphere. In the first stage, the temperature was raised to 200°C at a rate of 3°C / min and held for 1 hour. In the second stage, the temperature was raised to 480°C at a rate of 5°C / min and held for 6 hours. The roasting tail gas was absorbed by a 10wt.% sodium hydroxide aqueous solution and cooled naturally to obtain catalyst particles.

[0051] (3) Before use, the catalyst particles are transferred into a fixed bed reactor, and a mixed gas of HF / N2 with a volume fraction of 8% is introduced. The gas flow rate is controlled at 40 mL / min, and the catalyst is activated at 280℃ for 2 h to obtain the finished MgF2-based fluorinated catalyst.

[0052] The continuous production process of perfluoropentanone, carried out in a tubular reactor, includes the following steps:

[0053] The MgF2-based fluorination catalyst obtained above was loaded into a DN50 container. In a 1000 reaction tube, the bulk density of the fluorination catalyst was controlled at 0.51 g / cm³. 3 Nitrogen gas was introduced for purging, maintaining a pressure of 0.01 MPa at 250°C for 2 hours, and the moisture content was measured to be <50 ppm. After purging, the control valves for hexafluoropropylene and trifluoroacetyl fluoride were opened, and they were mixed and preheated to 180°C in a static mixer at a molar ratio of 1:1. Subsequently, the inlet flow rate of the mixed gas was controlled at 120 mL / min, and it was introduced into the reaction tube for continuous reaction at a pressure of 0.05 MPa and a reaction temperature of 250°C. After the reaction, part of the gas was condensed and sent to a storage tank with a back pressure of 0.3 MPa to obtain the target product perfluoropentanone. 12% of the total mass of the reaction solution was recycled back to the static mixer for mixing and preheating. The product was analyzed by gas chromatography, and the conversion rate of hexafluoropropylene was 99.89%, and the selectivity of perfluoropentanone was 86.75%.

[0054] Figure 2 Table 2 shows the gas chromatogram of perfluoropentanone obtained in this embodiment. Figure 2 The corresponding gas chromatography data.

[0055] Table 2 Gas Chromatographic Data of Perfluoropentanone

[0056]

[0057] Example 3

[0058] The preparation method of the MgF2-based fluorination catalyst includes the following steps:

[0059] (1) The effective components anhydrous MgCl2, anhydrous Fe(NO3)3, La2O3, NH4HF2 and graphite powder were mixed in a mass ratio of 8:0.8:0.3:7:0.9, ground at room temperature for 4 hours, and then pressed into cylindrical wet particles using a mold with a pore size of 2 mm.

[0060] (2) The wet particles were placed in a muffle furnace and roasted under a nitrogen atmosphere. In the first stage, the temperature was raised to 200°C at a rate of 3°C / min and held for 1 hour. In the second stage, the temperature was raised to 480°C at a rate of 5°C / min and held for 6 hours. The roasting tail gas was absorbed by a 10wt.% sodium hydroxide aqueous solution and cooled naturally to obtain catalyst particles.

[0061] (3) Before use, the catalyst particles are transferred into a fixed bed reactor, and a mixed gas of HF / N2 with a volume fraction of 8% is introduced. The gas flow rate is controlled at 40 mL / min, and the catalyst is activated at 280℃ for 2 h to obtain the finished MgF2-based fluorinated catalyst.

[0062] The continuous production process of perfluoropentanone, carried out in a tubular reactor, includes the following steps:

[0063] The MgF2-based fluorination catalyst obtained above was loaded into a DN50 container. In a 1000 reaction tube, the bulk density of the fluorination catalyst was controlled at 0.80 g / cm³. 3 Nitrogen gas was introduced for purging, maintaining a pressure of 0.05 MPa, and purging at 230°C for 3 hours. The moisture content was measured to be <50 ppm. After purging, the control valves for hexafluoropropylene and trifluoroacetyl fluoride were opened, and the mixtures were mixed and preheated to 200°C in a static mixer at a molar ratio of 1:1.5. Subsequently, the inlet flow rate of the mixed gas was controlled at 360 mL / min, and the mixture was introduced into the reaction tube for continuous reaction at a pressure of 0.07 MPa and a reaction temperature of 300°C. The gas after reaction was partially condensed and transported to a storage tank with a back pressure of 0.3 MPa to obtain the target product, perfluoropentanone. 12% of the total mass of the reaction solution was recycled back to the static mixer for mixing and preheating. The product was analyzed by gas chromatography, and the conversion rate of hexafluoropropylene was 99.90%, and the selectivity of perfluoropentanone was 87.03%.

[0064] Comparative Example 1

[0065] The difference from Example 1 is that all the gas discharged from the outlet of the tubular reactor was condensed into a storage tank, and no circulation device was used. Gas chromatography was used to analyze the products, and calculations showed that the conversion rate of hexafluoropropylene was 91.57%, and the selectivity of perfluoropentanone was 75.98%. These results indicate that the feedstock recycling design utilizes unreacted feedstock, improving feedstock utilization while maintaining the stability of the reaction system.

[0066] Comparative Example 2

[0067] 28.0g of MgF2-based fluorination catalyst (prepared in Example 1) and 184.5g of acetonitrile were added to a high-pressure reactor. Nitrogen gas was used for purging. 75g of hexafluoropropylene and 58g of trifluoroacetyl fluoride were added. The temperature was raised to 60°C and the reaction was carried out for 4 hours. The pressure during the reaction was controlled at 2MPa by a back pressure valve. After the reaction was completed, the pressure was lowered to room temperature and the pressure was released to atmospheric pressure. The reactor was then opened to obtain crude perfluoropentanone.

[0068] The products were analyzed using gas chromatography. Calculations showed that the conversion rate of hexafluoropropylene was 87.82%, and the selectivity of perfluoropentanone was 68.47%. These results indicate that the conversion rate and selectivity of the reactants in a high-pressure reactor are significantly lower than those in a continuous gas-phase process. This is because the presence of organic solvents in the liquid phase system adsorbs some of the catalyst's active sites, reducing catalytic efficiency; the mass transfer efficiency of intermittent high-pressure operation is lower than that of continuous gas-phase flow; and side reactions are more likely to occur.

[0069] Comparative Example 3

[0070] The difference from Example 1 is that the preparation process of the MgF2-based fluorination catalyst does not include anhydrous Fe(NO3)3 component, while the rest is the same as in Example 1;

[0071] The products were analyzed using gas chromatography, and the conversion rate of hexafluoropropylene was calculated to be 85.91%, while the selectivity of perfluoropentanone was 85.37%. These results indicate that the present invention, by introducing Fe(NO3)3 into the fluorination catalyst, can effectively improve the conversion activity of the raw materials. Its synergistic effect with the main components MgF2 and La2O3 significantly enhances the reactivity of hexafluoropropylene with trifluoroacetyl fluoride, thereby improving the selectivity of the target product.

Claims

1. A continuous production process of perfluoropentanone, characterized in that, This continuous production process is carried out in a tubular reactor and includes the following steps: The fluorination catalyst was packed into a reaction tube and purged with nitrogen. A mixture of preheated hexafluoropropylene and trifluoroacetyl fluoride gas was then introduced into the reaction tube for continuous reaction. Part of the gas was condensed to obtain the target product perfluoropentanone, while the other part was recycled back to the mixing and preheating stage. The recycling ratio was 12% of the total mass of the reaction liquid. The fluorination catalyst is a MgF2-based fluorination catalyst, and its preparation method includes the following steps: (1) The effective components anhydrous MgCl2, anhydrous Fe(NO3)3, La2O3, NH4HF2 and graphite powder are mixed and ground at room temperature for 4-5 hours. The mixture is then pressed into cylindrical wet particles using a mold with a pore size of 1-3 mm. (2) The wet particles are placed in a muffle furnace and roasted under a nitrogen atmosphere. The roasting exhaust gas is absorbed by an alkaline absorbent and cooled naturally to obtain catalyst particles. (3) Before use, the catalyst particles are transferred into a fixed bed reactor, and HF / N2 mixed gas is introduced. After activation treatment, the finished MgF2-based fluorinated catalyst is obtained. In step (1), the mass ratio of anhydrous MgCl2, anhydrous Fe(NO3)3, La2O3, NH4HF2 and graphite powder is (8-10):(0.8-0.9):(0.3-0.5):(7-9):(0.7-0.9).

2. The continuous production process of perfluoropentanone according to claim 1, characterized in that, The bulk density of the fluorination catalyst in the tubular reactor is 0.25-0.80 g / cm3 3 .

3. The continuous production process of perfluoropentanone according to claim 1, characterized in that, The continuous reaction is carried out at a pressure of 0.05-0.1 MPa and a temperature of 200-300℃.

4. The continuous production process of perfluoropentanone according to claim 1, characterized in that, The molar ratio of hexafluoropropylene to trifluoroacetyl fluoride is 1:(1-2), and the inlet flow rate of the mixed gas is 100-500 mL / min.

5. The continuous production process of perfluoropentanone according to claim 1, characterized in that, In step (2), the calcination process is as follows: in the first stage, the temperature is raised to 200-250℃ at a heating rate of 2-5℃ / min and held for 1-2 hours. In the second stage, the temperature is increased to 400-500℃ at a rate of 2-5℃ / min, and then held for 6-8 hours.

6. The continuous production process of perfluoropentanone according to claim 1, characterized in that, In step (2), the alkaline absorbent is a sodium hydroxide aqueous solution with a concentration of 10-15 wt.%.

7. The continuous production process of perfluoropentanone according to claim 1, characterized in that, In step (3), the volume fraction of HF in the HF / N2 mixed gas is 5-8%, the inlet flow rate of the HF / N2 mixed gas is 30-60 mL / min, the activation temperature is 250-300℃, and the activation time is 2-4 h.

Images