An apparatus for continuous gas-phase production of perfluorononane
By designing a gas-phase continuous production unit, the problems of low production capacity and high cost of perfluorononane in existing technologies have been solved, realizing continuous and large-scale production of perfluorononane and reducing production costs.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- ZHEJIANG LIHUA NEW MATERIAL SCI&TECH CO LTD
- Filing Date
- 2025-07-30
- Publication Date
- 2026-07-03
AI Technical Summary
Existing technologies lack suitable equipment for the continuous production of perfluorononane, resulting in low production capacity and high production costs.
A gas-phase continuous production device including a chlorination reactor, a fluorination reactor, and a condenser was designed. The device achieves the mixing, reaction, and condensation of hexafluoropropylene trimer and chlorine through components such as a mixer, heating pipe, gas booster pump, and metering pump, thereby realizing the continuous production of perfluorononane.
This enabled continuous production of perfluorononane, increased production scale, and reduced production costs.
Smart Images
Figure CN224442182U_ABST
Abstract
Description
Technical Field
[0001] This utility model relates to the field of perfluorononane production, specifically to an apparatus for the continuous gas-phase production of perfluorononane. Background Technology
[0002] Perfluorononane is odorless, low in toxicity, non-conductive, and does not contaminate the protected object, nor does it damage precision equipment. It can be liquefied and stored at room temperature, and leaves no particulate or oily residue after use. It has no ozone-depleting effect (ODP value is zero) and a boiling point of approximately 125°C. As a high-performance, efficient fluorinated coolant, it meets environmental protection requirements. Therefore, it has been widely and deeply researched and applied in many cutting-edge technologies, major industrial projects, pharmaceuticals, and pesticides, and the demand is expected to continue to grow. Currently, the main processes for preparing perfluorononane are batch synthesis processes and equipment involving the addition of fluoroolefins and the fluorination of chlorofluorocarbons and halogenated hydrocarbons. These processes have relatively small production capacities, and there is currently no equipment suitable for continuous production of perfluorononane. Utility Model Content
[0003] The technical problem to be solved by this utility model is to provide an apparatus for continuous gas-phase production of perfluorononane, which can ensure the continuous operation of the preparation reaction, increase the production scale, and reduce the production cost.
[0004] To address the above technical problems, this utility model discloses an apparatus for the continuous gas-phase production of perfluorononane, comprising: a chlorination reactor, a fluorination reactor, and a condenser connected in sequence; the inlet of the chlorination reactor is connected to a first mixer that connects hexafluoropropylene trimer gas and chlorine gas, and the inlet of the fluorination reactor is connected to a second mixer that connects to hydrogen fluoride gas, with the chlorination reactor connected to the second mixer via a pipeline. The chlorination reactor contains a chlorination reaction catalyst, and the fluorination reactor contains a fluorination reaction catalyst.
[0005] Furthermore, the chlorination reactor is equipped with a first heating tube, which can be heated electrically or by passing heat transfer oil through it.
[0006] Furthermore, the chlorination reactor is provided with an unreacted chlorine inlet at the top, which is connected to an unreacted chlorine outlet at the top of the condenser via a pipe for the recovery and reuse of unreacted chlorine.
[0007] Furthermore, a gas booster pump is installed on the pipeline connecting the unreacted chlorine inlet and the unreacted chlorine outlet to increase the chlorine pressure, allowing the chlorine to enter the chlorination reactor through the pipeline for recycling.
[0008] Furthermore, the fluorination reactor is equipped with a second heating tube, which can be heated electrically or by passing heat transfer oil through it.
[0009] Furthermore, the fluorination reactor is provided with an unreacted hydrogen fluoride inlet at the top, which is connected to an unreacted hydrogen fluoride outlet located on one side of the upper part of the condenser via a pipe, for the recovery and reuse of unreacted hydrogen fluoride.
[0010] Furthermore, a metering pump and a vaporizer are installed on the pipeline connecting the unreacted hydrogen fluoride inlet and the unreacted hydrogen fluoride outlet. The metering pump is used to meter and deliver liquid hydrogen fluoride, and the vaporizer is used to convert the liquid hydrogen fluoride discharged from the condenser into hydrogen fluoride gas.
[0011] Furthermore, the condenser is provided with a perfluorononane outlet at the bottom.
[0012] Furthermore, the condenser is also equipped with a condenser tube connected to the low-temperature brine. The condenser tube is a coil, which increases the contact area between the reaction mixture and the low-temperature brine and improves the condensation efficiency.
[0013] This invention first mixes hexafluoropropylene trimer gas and chlorine gas in a mixer, then introduces the mixture into a chlorination reactor for heating and reaction. The resulting chlorinated product and unreacted gas are mixed with hydrogen fluoride gas and then introduced into a fluorination reactor for fluorination. The resulting fluorinated product is then purified by distillation in a condenser. Finally, the product, perfluorononane, is collected, and the unreacted gas is recovered and reused. This production device is a gas-phase reaction apparatus that can be operated continuously, is suitable for large-scale production, increases production capacity, and reduces production costs. Attached Figure Description
[0014] Figure 1 This is a schematic diagram of the apparatus for the continuous gas-phase production of perfluorononane according to this utility model.
[0015] In the diagram: 1. Chlorination reactor; 2. Fluorination reactor; 3. Condenser; 4. First mixer; 5. Second mixer; 6. First heating element; 7. Unreacted chlorine gas inlet; 8. Second heating element; 9. Unreacted hydrogen fluoride inlet; 10. Perfluorononane outlet; 11. Unreacted chlorine gas outlet; 12. Unreacted hydrogen fluoride outlet; 13. Metering pump; 14. Vaporizer; 15. Gas booster pump. Detailed Implementation
[0016] The present invention will be further explained below with reference to the embodiments. The following embodiments are only used to illustrate the present invention, but are not intended to limit the scope of implementation of the present invention.
[0017] Example 1
[0018] like Figure 1The apparatus shown is for the continuous gas-phase production of perfluorononane, comprising: a chlorination reactor 1, a fluorination reactor 2, and a condenser 3 connected in sequence; the inlet of the chlorination reactor 1 is connected to a first mixer 4 that connects hexafluoropropylene trimer gas and chlorine gas; the chlorination reactor 1 is equipped with a first heating tube 6 inside, and an unreacted chlorine gas inlet 7 is provided at the top; the unreacted chlorine gas inlet 7 is connected to an unreacted chlorine gas outlet 11 located at the top of the condenser 3 via a pipe; a gas booster pump 15 is provided on the pipe connecting the unreacted chlorine gas inlet 7 and the unreacted chlorine gas outlet 11; the fluorination reactor... The inlet of reactor 2 is equipped with a second mixer 5 that connects to hydrogen fluoride gas. The chlorination reactor 1 is connected to the second mixer 5 through a pipeline. The fluorination reactor 2 is equipped with a second heating tube 8 inside and an unreacted hydrogen fluoride inlet 9 at the top. The unreacted hydrogen fluoride inlet 9 is connected to an unreacted hydrogen fluoride outlet 12 located on one side of the upper part of the condenser 3 through a pipeline. A metering pump 13 and a vaporizer 14 are installed on the pipeline connecting the unreacted hydrogen fluoride inlet 9 and the unreacted hydrogen fluoride outlet 12. The condenser 3 is equipped with a perfluorononane outlet 10 at the bottom and a condenser tube connected to low-temperature brine inside.
[0019] according to Figure 1 The working principle of the apparatus for continuous gas-phase production of perfluorononane according to this utility model is explained.
[0020] like Figure 1 As shown, hexafluoropropylene trimer is first vaporized in a gasifier to obtain hexafluoropropylene trimer gas. Then, hexafluoropropylene trimer gas and chlorine gas, measured by a gas flow meter, are continuously fed into the first mixer 4 to ensure thorough mixing. The mixed gas is then fed into a chlorination reactor 1, which is equipped with several first heating tubes 6 and contains a chlorination catalyst, to carry out a chlorination catalytic reaction at a temperature of 250°C. After a period of reaction, the material is pumped from the chlorination reactor 1 into the second mixer 5 and mixed with hydrogen fluoride gas (measured by a gas flow meter) in the second reactor 5. The mixed gas is then fed into a fluorination reactor 2, which is equipped with several second heating tubes 8 and contains a fluorination catalyst, to carry out a fluorination catalytic reaction at a temperature of 350°C. After a period of reaction, the gas-liquid mixture is fed from the fluorination reactor 2 into a condenser 3. The condenser 3 is equipped with a condensation coil connected to low-temperature brine. The product, perfluorononane, is liquefied by condensation and released from the perfluorononane outlet 10 at the bottom of the condenser 3 and collected.
[0021] Unreacted chlorine gas is discharged from unreacted chlorine outlet 11, compressed and pressurized by gas booster pump 15, and then enters chlorination reactor 1 through pipeline through unreacted chlorine inlet 7 for recycling. Unreacted hydrogen fluoride gas and the product perfluorononane are liquefied under the condenser tube. Due to the density difference between the two substances, the hydrogen chloride liquid is above the perfluorononane and is discharged from unreacted hydrogen fluoride outlet 12. It is first metered and extracted by metering pump 13, and then transported to vaporizer 14 for vaporization treatment to obtain unreacted hydrogen fluoride gas. The unreacted hydrogen fluoride gas enters fluorination reactor 2 through unreacted hydrogen fluoride inlet 9 for recycling.
[0022] This utility model relates to a vaporizer for the vaporization of hexafluoropropylene trimer, as well as conventional components such as gas flow meters, valves, and pumps used on various gas pipelines. These components are not shown in the figures, but this does not mean they are not present.
[0023] The above description is only a preferred embodiment of the present utility model and is not intended to limit the present utility model. Any modifications, equivalent substitutions and improvements made within the spirit and principles of the present utility model should be included within the protection scope of the present utility model.
Claims
1. An apparatus for the continuous production of perfluorononane in the gas phase, characterized in that The device includes a chlorination reactor (1), a fluorination reactor (2) and a condenser (3) connected in sequence; the inlet of the chlorination reactor (1) is connected to a first mixer (4) that connects hexafluoropropylene trimer gas and chlorine gas, and the inlet of the fluorination reactor (2) is provided with a second mixer (5) that connects hydrogen fluoride gas, and the chlorination reactor (1) is connected to the second mixer (5) through a pipeline.
2. The apparatus for continuous gas-phase production of perfluorononane according to claim 1, characterized in that, The chlorination reactor (1) is equipped with a first heating tube (6).
3. The apparatus for continuous production of perfluorononane in the gas phase according to claim 1 or 2, characterized in that The chlorination reactor (1) is provided with an unreacted chlorine inlet (7) at the top, which is connected to the unreacted chlorine outlet (11) at the top of the condenser (3) via a pipe.
4. The apparatus for continuous production of perfluorononane by gas phase according to claim 3, characterized in that, A gas booster pump (15) is installed on the pipeline connecting the unreacted chlorine inlet (7) and the unreacted chlorine outlet (11).
5. The apparatus for continuous production of perfluorononane by gas phase according to claim 1, characterized by, The fluorination reactor (2) is equipped with a second heating tube (8).
6. The apparatus for continuous production of perfluorononane by gas phase according to claim 1 or 5, characterized in that, The fluorination reactor (2) is provided with an unreacted hydrogen fluoride inlet (9) at the top, which is connected to the unreacted hydrogen fluoride outlet (12) located on the upper side of the condenser (3) via a pipe.
7. The apparatus for continuous production of perfluorononane by gas phase according to claim 6, characterized in that, A metering pump (13) and a vaporizer (14) are installed on the pipeline connecting the unreacted hydrogen fluoride inlet (9) and the unreacted hydrogen fluoride outlet (12).
8. The apparatus for continuous production of perfluorononane by gas phase according to claim 1, characterized by, The condenser (3) is provided with a perfluorononane outlet (10) at the bottom.
9. The apparatus for continuous production of perfluorononane by gas phase according to claim 8, characterized in that, The condenser (3) is also provided with a condenser tube that is connected to low-temperature brine.