A PROCESS FOR THE PURIFICATION OF FLUORINATED OLEFINS

Abstract

The present invention relates to a process for the purification of fluorinated olefins, in particular hexafluoro-1,3-butadiene, comprising a step wherein a liquid mixture comprising hexafluoro-1,3-butadiene in liquid phase is contacted with at least one adsorbent having an average pore size of less than 10 .

Claims

1. A process for the purification of hexafluoro-1,3-butadiene comprising a step wherein a liquid mixture comprising hexafluoro-1,3-butadiene in liquid phase is contacted with at least one adsorbent having an average pore size of less than 10 .

2. The process according to claim 1, wherein said at least one adsorbent has an average pore size of more than 2 and less than 8 .

3. The process according to claim 1, wherein said at least one adsorbent is a zeolite.

4. The process according to claim 3, wherein the zeolite has eight-membered-ring pores.

5. The process according to claim 4, wherein the zeolite is synthetic Chabazite.

6. The process according to claim 1, wherein the liquid mixture is contacted with said at least one adsorbent at an initial pressure of equal to or above 0.1 bar (abs.) and equal to or below 10 bar (abs.).

7. The process according to claim 1, wherein the liquid mixture is contacted with said at least one adsorbent at an initial temperature of equal to or above 5 C. and equal to or below 40 C.

8. The process according to claim 1, wherein the liquid mixture is contacted with said at least one adsorbent at a flow rate of equal to or above 2 g/min and equal to or below 200 g/min.

9. The process according to claim 1, wherein said at least one adsorbent is not thermally treated before being contacted with the liquid mixture.

10. The process according to claim 1, comprising a regeneration step of said at least one adsorbent, the regeneration step comprising a heat treatment of said at least one adsorbent at a temperature ranging from 200 to 400 C.

11. A process for the production of a gas mixture comprising the process according to claim 1 and subsequently, mixing the purified hexafluoro-1,3-butadiene with a further gas selected from the group consisting of an inert gas, oxygen and another fluorinated etching gas.

12. A gas mixture comprising hexafluoro-1,3-butadiene and at least one further gas selected from the group consisting of an inert gas, oxygen and another fluorinated etching gas, wherein a volume ratio of hydrofluorocarbons possibly contained therein is lower or equal to 500 ppmv, relatively to the total volume of the gas mixture.

13. The gas mixture according to claim 12, wherein the volume ratio of 1,1,4,4-tetrafluoro-1,3-butadiene or isomers thereof possibly contained therein is lower or equal to than ppmv, relatively to the total volume of the gas mixture.

14. The gas mixture according to claim 12, wherein the volume ratio of 1,1,3,4,4-pentafluoro-1,3-butadiene or isomers thereof possibly contained therein is lower or equal to 70 ppmv, relatively to the total volume of the gas mixture.

15. A process for the production of a semiconductor material, a solar panel, a flat panel or a microelectromechanical system, or a process for cleaning the chamber of an apparatus used for semiconductor manufacturing, comprising producing the semiconductor material, solar panel, flat panel or microelectromechanical system or cleaning the chamber with the hexafluoro-1,3-butadiene purified according to claim 1 with a gas mixture comprising hexafluoro-1,3-butadiene and at least one further gas selected from the group consisting of an inert gas, oxygen and another fluorinated etching gas, wherein a volume ratio of hydrofluorocarbons possibly contained therein is lower or equal to 500 ppmv, relatively to the total volume of the gas mixture.

Description

[0011] FIG. 1 shows a flow diagram of an apparatus suitable for performing the process according to the present invention.

[0012] The liquid mixture to be purified may contain various impurities in liquid phase in admixture with the hexafluoro-1,3-butadiene, such as hydrohalogenocarbons, especially hydrofluorocarbons and/or hydrochlorofluorocarbons, more particularly hydrohalogenoolefins, especially hydrofluoroolefins such as 1,1,3,4,4-pentafluoro-1,3-butadiene and/or isomers thereof (commonly referred to as C4HF5 thereafter), 1,1,4,4-tetrafluoro-1,3-butadiene and/or isomers thereof (commonly referred to as C4H2F4 thereafter). The liquid mixture, in the framework of this invention, may be composed of hexafluoro-1,3-butadiene in liquid phase as major component and of the various possible impurities contained therein, equally in liquid phase. Said impurities may come from the formation of byproducts, from residual solvents, unreacted starting materials and/or partially unreacted starting materials.

[0013] Without being particularly limited, the initial purity of the raw hexafluoro-1,3-butadiene to be purified by the process according to the invention may be equal to or greater than 90% by volume, in particular equal to or greater than 95% by volume, more particularly equal to or greater than 98% by volume, even more particularly equal to or greater than 99% by volume, relatively to the total volume of raw hexafluoro-1,3-butadiene. Especially, the raw hexafluoro-1,3-butadiene may comprise from 0 ppmv to 1500 ppmv, in particular from 5 ppmv to 1000 ppmv of C4H2F4. The raw hexafluoro-1,3-butadiene may comprise from 0 ppmv to 1000 ppmv, in particular from 5 to 500 ppmv of C4HF5.

[0014] Said at least one adsorbent is selected from adsorbents having an average pore size of less than 10 . It is believed that such an adsorbent is effective to trap most of all the possible impurities likely to be present in the raw hexafluoro-1,3-butadiene. Above 10 , the hexafluoro-1,3-butadiene itself could be at least partially adsorbed: it could decompose and generate thereby further impurities.

[0015] According to one sub-embodiment, said at least one adsorbent may be selected from adsorbents having an average pore size of more than 2 and less than 8 , in particular of more than 3 and less than 6 and more particularly of more than 3 and less than 5,5 . It is believed that adsorbents having such an average pore size are very suitable to trap the main impurities potentially present in the raw hexafluoro-1,3-butadiene, such as C4H2F4 and/or C4HF5.

[0016] Suitable adsorbents that can be used in the framework of the invention include zeolites having a pore size of less than 10 A, especially the ones having eight-membered-ring pores such as Zeolite P, Gmelinite, synthetic Chabazite, in particular SSZ-13 or SSZ-62; zeolite 5A; zeolite 1VIFI. Zeolite type adsorbents having eight-membered-ring pores are preferred and among them, synthetic Chabazite is particularly advantageous, especially regarding its selectivity towards C4H2F4 and/or C4HF5, which are the main impurities likely to be present in the hexafluoro-1,3-butadiene to be purified. A very suitable synthetic Chabazite includes the HCZC S (H-form) from CLARIANT.

[0017] The hexafluoro-1,3-butadiene is in liquid phase when contacted with said at least one adsorbent. Accordingly, the contacting step is preferably performed in suitable conditions of pressure, temperature and/or flow rate to maintain the hexafluoro-1,3-butadiene and the possible impurities contained therein in the liquid state.

[0018] Preferably, the process is conducted at an initial pressure of equal to or above 0.1 bar (abs.) and equal to or below 10 bar (abs.), in particular from 0.1 bar (abs.) to 5 bar (abs.).

[0019] Also preferably, the process is conducted at an initial temperature of equal to or above 5 C. and equal to or below 40 C., in particular from 5 C. to 30 C.

[0020] Also preferably, the process is conducted at an initial flow rate ranging from 2 g/min to 200 g/min, in particular from 2 to 150 g/min, more particularly from 2 to 100 g/min, even more particularly from 2 to 50 g/min.

[0021] The contacting step may in particular be operated at an initial pressure of equal to or above 0.1 bar (abs.) and equal to or below 10 bar (abs.), at an initial temperature of equal to or above 5 C. and equal to or below 40 C. and at an initial flow rate ranging from 2 g/min to 200 g/min. The contacting step may more particularly be operated at an initial pressure of equal to or above 0.1 bar (abs.) and equal to or below 5 bar (abs.), at an initial temperature of equal to or above 5 C. and equal to or below 30 C. and at an initial flow rate ranging from 2 g/min to 50 g/min.

[0022] The term initial as used herein is intended to denote respectively the temperature, pressure and flow rate of the liquid mixture before coming into contact with said at least one adsorbent having an average pore size of less than 10 .

[0023] According to one embodiment, said at least one adsorbent used within the purification process of the invention is not pre-treated, in particular by any heat treatment, before being contacted with the liquid mixture. Contrary to the purification processes of the state of the art, wherein a pre-treatment often called activation which consists in keeping the adsorbent at an elevated temperature, typically between 150 and 400 C., under inert atmosphere to remove moisture from the adsorbent before its first use, the purification process of the invention does not require such a step. It advantageously enables production savings, as it avoids a waste of time, of energy and the management of effluents (mainly water, carbon dioxide and the inert gas used).

[0024] The process of the invention can comprise one or more additional purification steps, before or after the contacting step with said at least one adsorbent, using other types of adsorbents than the ones described above or even different purification means. Among the possible means which could be used and without being specifically limited to these means, mention can be made of other adsorbents like silica gel, zeolite 3A, zeolite 5A, zeolite 13X, zeolite MFI, zeolite P, gmelinite, activated alumina, activated carbon and the like. According to one specific embodiment, the process of the invention does not comprise any other purification step than the contacting step with said at least one adsorbent having an average pore size of less than 10 . It is nevertheless possible to use more than one adsorbent having an average pore size of less than 10 , which can be the same or different from each other. The further adsorbent(s) used can be advantageously selected among the list of suitable adsorbents having an average pore size of less than 10 listed above. Other less preferred adsorbents can be used alternatively.

[0025] If more than one adsorbent is used in the purification process of the invention, the adsorbents can be present in different zones in the same adsorber cartridge. Thus, only one adsorber cartridge may be used in the purification process and the adsorbents may be located within the one cartridge in different zones, preferably in subsequent zones allowing the liquid mixture to be in contact with one adsorbent after the other. Alternatively, the adsorbents may be present in different adsorber cartridges, so that the liquid mixture can be brought into contact with the adsorbents one after the other and the adsorbents can be regenerated individually.

[0026] The final purity of the hexafluoro-1,3-butadiene achieved by the process according to the invention may be equal to or greater than 99.9% by volume, preferably equal to or greater than 99.95% by volume, more preferably equal to or greater than 99.98% by volume, and most preferably equal to or greater than 99.99% by volume, relatively to the total volume of the hexafluoro-1,3-butadiene.

[0027] The total amount of hydrofluorocarbons potentially remaining in the purified hexafluoro-1,3-butadiene may be lower or equal to 1400 ppmv, in particular lower or equal to 1000 ppmv, in particular lower or equal to 600 ppmv, in particular lower or equal to 500 ppmv, in particular lower or equal to 300 ppmv, in particular lower or equal to 150 ppmv. The total amount of hydrofluorocarbons potentially remaining in the purified hexafluoro-1,3-butadiene may be equal to or greater than 0 ppmv, equal to or greater than 1 ppmv, in particular equal to or greater than 10 ppmv, in particular equal to or greater than 30 ppmv. It may be measured by conventional methods, such as gas chromatography or mass spectroscopy.

[0028] The total amount of C4H2F4 potentially remaining in the purified hexafluoro-1,3-butadiene may be lower or equal to 400 ppmv, in particular lower or equal to 200 ppmv, in particular lower or equal to 100 ppmv, in particular lower or equal to 50 ppmv, in particular lower or equal to 10 ppmv, in particular lower or equal to 6 ppmv. The total amount of C4H2F4 potentially remaining in the purified hexafluoro-1,3-butadiene may be equal to or greater than 0 ppmv. It may be in the limit of detection of the apparatus used to quantify this impurity. It may for instance be equal to or greater than 0.001 ppmv, in particular equal to or greater than 0.1 ppmv, in particular equal to or greater than 1 ppmv. It may be measured by any known method such as gas chromatography or mass spectroscopy.

[0029] The total amount of C4HF5 potentially remaining in the purified hexafluoro-1,3-butadiene may be lower or equal to 80 ppmv, in particular lower or equal to 70 ppmv, in particular lower or equal to 60 ppmv, in particular lower or equal to 55 ppmv, in particular lower or equal to 50 ppmv, The total amount of C4HF5 potentially remaining in the purified hexafluoro-1,3-butadiene may be equal to or greater than 0 ppmv, equal to or greater than 1 ppmv, in particular equal to or greater than 10 ppmv. It may be measured by any known method such as gas chromatography or mass spectroscopy.

[0030] The purification process can be repeated as many times as necessary to achieve the desired purity for the final hexafluoro-1,3-butadiene. In the purification unit designed for implementing the process of the invention, a recycling loop can therefore be settled to recover the purified hexafluoro-1,3-butadiene downstream of the purification unit and send it back upstream of the purification unit. According to one embodiment, the purification process of the invention, which may consist in the contacting step with said at least one adsorbent, is run only one time. It is believed that the process of the invention is suited to achieve a very good purity in a single passage of the liquid mixture comprising hexafluoro-1,3 -butadiene.

[0031] The purification process according to the invention may comprise a regeneration step of said at least one adsorbent. The regeneration step may comprise or consist in a heat treatment thereof, preferably at a temperature ranging from 200 to 400 C., more preferably from 250 to 350 C., even more preferably from 280 to 300 C. The pressure conditions are not particularly limited: the regeneration step may be advantageously performed at atmospheric pressure.

[0032] The hexafluoro-1,3-butadiene purified according to the present invention can be used neat. However, it is often desired to use the hexafluoro-1,3-butadiene of the present invention as an admixture with other fluorinated etching gases to control the carbon/fluoro ratio of the gas mixture. Additionally, mixtures with suitable inert gases like nitrogen, argon or xenon or with oxygen might be desired.

[0033] Accordingly, a further aspect of the present invention is a process for the production of a gas mixture according to the present invention, comprising the process for the purification of hexafluoro-1,3-butadiene described above and subsequently, mixing the purified hexafluoro-1,3-butadiene with a further gas selected from the group consisting of an inert gas, oxygen and another fluorinated etching gas as well as the gas mixture formed in such a process.

[0034] In particular, one object of the invention is a gas mixture comprising hexafluoro-1,3-butadiene and at least one further gas selected from the group consisting of an inert gas, oxygen and another fluorinated etching gas, wherein the volume ratio of hydrofluorocarbons is lower or equal to 500 ppmv, in particular lower or equal to 300 ppmv, in particular lower or equal to 150 ppmv, relatively to the total volume of the gas mixture.

[0035] Preferably, the volume ratio of C4H2F4 possibly present in said gas mixture is lower or equal to 50 ppmv, in particular lower or equal to 10 ppmv, in particular lower or equal to 5 ppmv, relatively to the total volume of the gas mixture.

[0036] Preferably, the volume ratio of C4HF5 possibly present in said gas mixture is lower or equal to 70 ppmv, in particular lower or equal to 60 ppmv, in particular lower or equal to 55 ppmv, in particular lower or equal to 50 ppmv, relatively to the total volume of the gas mixture.

[0037] The lower limits of some impurities may be in the limit of quantification of the measurement tool. For hydrofluorocarbons in general, including the two specific ones mentioned above, the limit of quantification shall appear under 4 ppmv, as measured by GC.

[0038] The inventive gas mixtures can easily be prepared by condensing or pressing the desired amounts of hexafluoro-1,3-butadiene and any other desired gas into a pressure tank.

[0039] Furthermore, the invention concerns a process for the production of a semiconductor material, a solar panel, a flat panel or a microelectromechanical system, or a process for cleaning the chamber of an apparatus used for semiconductor manufacturing using the hexafluoro-1,3-butadiene purified according to this invention or the gas mixture according to this invention. The preferred use is in the production of a microelectromechanical system.

[0040] Should the disclosure of any patents, patent applications, and publications which are incorporated herein by reference conflict with the description of the present application to the extent that it may render a term unclear, the present description shall take precedence.

[0041] The invention will be illustrated in more detail with reference to FIG. 1 and the following Example, but it should be understood that the present invention is not deemed to be limited thereto.

[0042] Crude hexafluoro-1,3-butadiene was provided by Solvay under the brand name Sifren 46. It was analyzed by gas chromatography and mass spectroscopy to quantify the main organic impurities contained therein. The results are indicated in Table 1. The adsorbent used was Chabazite HCZC S (H-form) supplied by CLARIANT, having an average pore size of 3.8 . It was not thermally pre-treated before usage and used as it was.

[0043] FIG. 1 shows a suitable apparatus which was used to run the process according to the present invention. A source tank C1, having a 1 L capacity, intended to be loaded with the crude hexafluoro-1,3-butadiene, was connected to a stainless steel column A1 containing the adsorbent bed, charged with 82.07 g of Chabazite. The column had an internal diameter of 18 mm and a length of 406 mm. It was double jacketed and connected to a cooling bath for being able to cool down the bed in case of an exothermic reaction inside. The column A1 was connected to a receiver tank C2 for collecting the purified hexafluoro-1,3-butadiene, submersed in a cooling bath at 5 C. (mix of dry ice and acetone). Pressure gauges P1, P2 and thermocouples T1, T2 were set before and after column A1 as shown on FIG. 1. All piping was made of stainless steel. Before flowing the hexafluoro-1,3-butadiene into the apparatus, the tightness thereof was checked under vacuum. Afterwards, the source tank C1 was loaded with 500 g of crude hexafluoro-1,3-butadiene (as measured with a balance). The pressure inside the source tank was set at 2.8 bar abs and the temperature within the source tank was set at room temperature (about 22 C.) so as to keep the hexafluoro-1,3-butadiene in liquid phase. The crude hexafluoro-1,3-butadiene in liquid state was then allowed to flow through column Al and the purified hexafluoro-1,3-butadiene in liquid state was collected in receiver tank C2. The flow rate was manually set at about 5 g/min by adjusting needle valves V1, V2 and V3 accordingly. During the run, a pressure of 2.8 bar (abs.) was measured at pressure gauge P1 and a temperature of 22 C. was measured at thermocouple T1. A pressure of 1.15 bar (abs.) was measured at pressure gauge P2 and a temperature of 26 C. was measured at thermocouple T2. After all the crude hexafluoro-1,3-butadiene was passed through column A1, receiver tank 2 was isolated by closing valve V4 and then allowed to warm to room temperature.

[0044] A sample of the purified hexafluoro-1,3-butadiene in receiver tank 2 was analyzed by gas chromatography and mass spectroscopy to quantify the main organic impurities remaining therein. The results are indicated in Table 1.

TABLE-US-00001 TABLE 1 Analysis results impurites (ppmv) relative to the total volume of Source tank Receiver tank hexafluoro-1,3-butadiene C1 C2 C4H2F4 505 <5 C4HF5 91 43 Total hydrofluorocarbons <1500 <120