Process for the polymerization of hexafluoropropene oxide

Abstract: In polymerizing hexafluoropropene oxide (HFPO) into a fluorinated polyether, a liquefied gas of fluorocarbon having 1 to 4 carbon atoms is added to a reactor. HFPO is polymerized in the reactor while maintaining a gas phase in the reactor under a pressure lower than the vapor pressure of the liquefied gas and allowing the liquefied gas to evaporate from the polymerization system. Heat of polymerization can be efficiently removed from the HFPO polymerization system of high viscosity, and the polymerization temperature is kept low.

Description: This invention relates to a method for polymerizing hexafluoropropene oxide (to be abbreviated as HFPO, hereinafter), with particular reference to thermal control of the reaction. Several methods for the polymerization of HFPO are known in the art. For example, USP 3,660,315 and JP-B 5360/1978 disclose a method for polymerizing HFPO using a tetraethylene glycol dimethyl ether (to be abbreviated as tetraglyme, hereinafter) solution of a compound of the following formula (1a) as a polymerization initiator, thereby producing a difunctional polymer of the following formula (2a). This method is characterized in that polymerization of HFPO is carried out using a uniform solution obtained by mixing cesium fluoride, tetraglyme and FOCCF(CF 3 )OCF 2 CF 2 OCF(CF 3 )COF and separating the excess of cesium fluoride. This prevents the homo-polymerization of HFPO which is otherwise catalyzed by the excess of cesium fluoride, eventually suppressing the formation of a monofunctional HFPO polymer, that is, HFPO polymer which is functional at one terminal end. J. Macromol. Sci. - Chem., 48 (3), 499-520 (1974), describes that the presence of hexafluoropropene (abbreviated as HFP, hereinafter) during polymerization of HFPO is effective for preventing chain transfer reaction and increasing the degree of polymerization of a polymer produced. Allegedly, the effect of the HFP is to prevent chain transfer by trapping free fluoride anions. As mentioned above, it is important to carry out polymerization of HFPO under such conditions as to suppress chain transfer reaction, that is, initiation of polymerization from a chemical species other than the initiator. To this end, the polymerization temperature should be kept as low as possible. With regard to the polymerization of HFPO, the tendency is well known that as the polymerization temperature lowers, the selectivity of the reaction increases, chain transfer is suppressed, the degree of polymerization of the polymer produced increases, and less monofunctional polymer (by-product) forms when a difunctional initiator is used. However, attempts to lower the temperature encounter the problem that the polymerization system wherein the product is a polymer is essentially viscous, and increasingly thickens at lower temperatures. The practically acceptable temperature range is thus limited. If the reactor is of small size for laboratory use, the high viscosity content can be cooled. Since a large size reactor for commercial production, however, has a relatively smaller heat transfer area, a cooling efficiency comparable to that in the small size reactor cannot be accomplished unless the heat transfer area is increased by special measures. Differently stated, in a conventional cylindrical reactor whose wall is cooled, the amount of HFPO which can be polymerized per unit time is governed by the effective heat transfer area rather than by the internal volume of the reactor. Additionally, the coefficient of heat transfer at the reactor wall is drastically reduced as the viscosity of the content increases. Thus, a rise of the internal temperature cannot be avoided unless the feed rate of HFPO is reduced to suppress the level of heat release or heat of polymerization. On scale-up of manufacture, this causes serious barriers including an extended HFPO feed time and a drop of quality of the product due to the increased polymerization temperature. In general, the heat transfer area can be increased by providing a coil within the reactor or circulating the content through a heat exchanger. These means are only applied with difficulty in the case of HFPO polymerization because the content is highly viscous. Therefore, there is a need for a cooling method which is fully efficient for removing the heat of HFPO polymerization in a reactor of simple structure. The aim herein is to provide a new HFPO polymerisation method with control of the reaction heat. A preferred aim is to provide a method for polymerizing HFPO by using a cooling means capable of efficiently removing the heat of HFPO polymerization from a high viscosity HFPO polymerization system in order to keep the polymerization temperature low. Another preferred aim is to provide such a HFPO polymerization method which can be readily practised on a large commercial scale. Regarding a process of polymerizing HFPO into a fluorinated polyether, we have found that by adding a liquefied gas of fluorocarbon having 1 to 4 carbon atoms to a reaction system and polymerizing HFPO in the reactor while allowing the liquefied gas to evaporate from the polymerization system, the heat of polymerization can be efficiently removed as the latent heat of vaporization of the liquefied gas. Accordingly, the invention as claimed in claim 1 provides a method for polymerizing HFPO into a fluorinated polyether, comprising the steps of adding a liquefied gas of fluorocarbon having 1 to 4 carbon atoms to a reactor, maintaining a gas phase in the reactor under a pressure lower than the vapor pressure of the liquefied gas, and polymerizing HFPO in the reactor while allowing the liquefied gas to evaporate from the polymerization system. Preferred measures are either or both of (a) cooling the vapor resulting from evaporation of the liquefied gas into a liquid and flowing the liquid back into the reactor and (b) maintaining the liquid phase in the reactor at a temperature in the range of -70°C to -10°C. These steps may be accomplished by attaching a reflux means to the reactor. Alternatively, the method may further include the steps of compressing the vapor resulting from evaporation of the liquefied gas to liquid and flowing the liquid back into the reactor and/or maintaining the interior of the reactor at a temperature in the range of -70°C to -10°C. DETAILED DESCRIPTION Briefly stated, HFPO is polymerized by feeding a liquefied gas of fluorocarbon having 1 to 4 carbon atoms to a reaction system, that is, to a polymerization initiator for HFPO in advance or concurrent with HFPO, and removing the heat resulting from polymerization of HFPO (including heat of polymerization and mechanically generated heat) from the polymerization system through evaporation of the liquefied gas. The polymerization initiator is not critical insofar as it can initiate the polymerization of HFPO. Commonly used polymerization initiators are mixtures of an alkali metal fluoride and an aprotic polar solvent and solutions prepared by adding carbonyl-bearing compounds such as ketones, acid anhydrides and acid halides to mixtures of an alkali metal fluoride and an aprotic polar solvent. Polymerization initiators may be prepared by well-known methods as described in USP 3,660,315. Cesium fluoride is a typical alkali metal fluoride. Glymes such as monoglyme, diglyme, triglyme and tetraglyme, diethyl ether and dioxane may be used as the aprotic polar solvent. Preferably, the polymerization initiator is of the following general formula (1): CsOCF 2 -Rf-CF 2 OCs wherein Rf is a perfluoroalkylene group having 1 to 4 carbon atoms or an ether bond-containing perfluoroalkylene group having 2 to 10 carbon atoms. A polymerization initiator solution consisting of this polymerization initiator and an aprotic polar solvent as mentioned above is advantageously used. Illustrative examples of the group represented by Rf are given below. -CF 2 -, -CF 2 CF 2 -. -CF 2 CF 2 CF 2 -, -(CF 2 ) 4 -, The polymerization initiator solution preferably contains the polymerization initiator in a concentration of about 10 to 60% by weight, more preferably about 25 to 45% by weight. Typically the reactor is charged with the polymerization initiator solution before HFPO is fed to the reactor where polymerization of HFPO takes place. In one preferred reactor embodiment, a pump is connected to a portion of the reactor surrounding the gas phase for adjusting the internal pressure of the reactor, and a condenser is connected to the suction or discharge side of the pump so that the liquid condensed in the condenser may flow back to the reactor. After the reactor is charged with the polymerization initiator solution, the reactor is cooled to the polymerization temperature. Cooling may be done either by passing a coolant through a jacket around the reactor or by introducing a liquefied gas into the reactor and refluxing it by way of the condenser. The polymerization temperature which is the temperature of the liquid phase in the reactor is typically -70°C to -10°C, preferably -50°C to -25°C, more preferably -45°C to -30°C. Polymerization of HFPO can be carried out by gradually or sequentially feeding HFPO into the above-mentioned reactor. It is recommended that a liquefied gas of fluorocarbon having 1 to 4 carbon atoms is concurrently fed into the reactor. The internal pressure of the reactor can be adjusted by means of a said pump so as to keep the polymerization temperature within the above-mentioned range. The liquefied gas used herein is of a fluorocarbon having 1 to 4 carbon atoms, which is preferably compatible with a polymer of HFPO and also preferably has a boiling point of lower than -15°C under atmospheric pressure, especially equal to or lower than the boiling point of HFPO. Exemplary fluorocarbons include tetrafluoroethane, hexafluoroethane, octafluoropropane, perfluorobutane, trifluoromethane, pentafluoroethane, heptafluoropropane, difluoromethane, hexafluoropropene, tetrafluoroethylene, and chlorotrifluoroethylene, with the hexafluoropropene (HFP) being especially preferred. The overall amount of the liquefied gas blended is preferably about 20 to 150 parts, especially about 40 to 70 parts by weight per 100 parts by weight of HFPO. Less than 20 parts of the liquefied gas may be insufficient to reflux, failing to achieve efficient cooling. With more than 150 parts of the liquefied gas, the yield of HFPO polymer per unit volume would be rather low. The amount of HFPO fed may be appropriately selected, often in the range of about 10 to 400 mol, typically about 20 to 200 mol per mol of the polymerization initiator. HFPO may be fed in either gas or liquid form, but preferably under such conditions that the internal temperature may be kept constant. Feed time may be from about 3 to 120 hours. The internal pressure is generally 9.8 to 196 kPa (absolute pressure) although it varies with the type and weight ratio of the liquefied gas added. Where HFP is used, it is preferred that about 20 to 150 parts by weight of HFP is added per 100 parts by weight of HFPO and the internal pressure is kept at about 12.7 to 90 kPa (absolute pressure). At the end of HFPO feed, the reactor may be heated whereupon the liquefied gas is recovered. The contents are taken out, and a HFPO polymer is collected therefrom. Heating should be avoided in the case of HFP. It is recommended to recover HFP below -30°C under vacuum because HFP reacts at elevated temperatures to form an oligomer. The HFPO polymer produced varies in accordance with the type of polymerization initiator. For example, when a polymerization initiator of formula (1) is used, a fluorinated polyether is obtained as shown by the following reaction scheme. EXAMPLE Examples of the present invention are given below by way of illustration and not by way of limitation. Example 1 A glass reactor having an internal volume of 500 ml was equipped with an agitator, temperature sensor, and condenser. The condenser at the top was connected to a diaphragm type vacuum pump through a pressure sensor. An automatic valve having a mechanism which automatically opens and closes at a preset pressure was disposed between the pressure sensor and the vacuum pump for adjusting the pressure in the reactor to any desired level. The reactor was charged with 13 g of a tetraglyme solution containing 5.0x10 -4 mol of a polymerization initiator of the following composition: CsOCF 2 CF(CF 3 )OCF 2 CF 2 OCF(CF 3 )CF 2 OCs. While the agitator was rotated at 120 rpm, the reactor was cooled with a coolant bath adjusted at -35°C. After about 2 hours from the start of cooling, the temperature of the liquid phase within the reactor stabilized at -32°C. The condenser was then cooled at -80°C whereupon 3.9 g of gaseous HFP was fed at a rate of 3.9 g/hr. into the reactor which was maintained under atmospheric pressure. Reflux behavior, i.e the liquid condensed in the condenser flowing back to the reactor, was observed during the feed of HFP but the reflux stopped when the feed stopped. Next, the pressure within the reactor was adjusted to 58 kPa (absolute pressure) whereupon 108 g of HFPO and 54 g of HFP were continuously fed at a rate of 7.2 g/hr. and 3.6 g/hr., respectively, over about 15 hours. The reflux behavior that the liquid condensed in the condenser flowed back to the reactor was observed during the feed. The liquid phase in the reactor was at a temperature of -35°C to -38°C during the feed of HFPO. After the feed of HFPO was over, the reaction solution was agitated for a further 2 hours. The cooling of the condenser was interrupted, the reactor was evacuated to about 5 kPa (absolute pressure), and the coolant bath was allowed to gradually warm up to near room temperature whereby the HFP was evaporated off. The contents of the reactor were a white turbid oily liquid recovered in an amount of 118 g. To 50 g of the recovered liquid were added 50 g of methanol and 40 g of 1,3-bistrifluoromethylbenzene. The mixture was agitated at 20 to 25°C for 30 minutes. Methanol, 50 g, was added to the solution, which was allowed to stand to induce phase separation. The lower layer was collected and the volatiles were removed therefrom at 120°C and 3 mmHg, yielding 44 g of a colorless, clear, oily liquid represented by the following formulae (A) and (B). The results of 19 F-NMR analysis of this liquid are shown below. (A)/(B) molar ratio = 94/6 = 100( k - 0.5 x ) k + 0.5 x / 100 x k + 0.5 x Average degree of polymerization = 92 = 2 m k + 0.5 x It is evident from the above data that the mix molar ratio of (A)/(B) was 94/6 and the average degree of polymerization was 92. Comparative Example 1 The same reactor as used in Example 1 was charged with 13 g of the same initiator as in Example 1. While the agitator was rotated at 120 rpm, the reactor was cooled with a coolant bath adjusted at -40°C. After about 2 hours from the start of cooling, the temperature of the liquid phase within the reactor stabilized at -37°C. The condenser was then cooled at -80°C whereupon 3.9 g of gaseous HFP was fed at a rate of 3.9 g/hr. into the reactor which was maintained under atmospheric pressure. Reflux behavior, in which the liquid condensed in the condenser flowed back to the reactor, was observed during the feed of HFP but stopped at the end of the feed. Next, with the reactor kept under atmospheric pressure, 108 g of HFPO and 54 g of HFP were continuously fed at a rate of 7.2 g/hr. and 3.6 g/hr., respectively, over about 15 hours. The liquid phase in the reactor was at a temperature of -35°C to -37°C during the feed of HFPO. After the feed of HFPO was over, the reaction solution was agitated for a further 2 hours. The cooling of the condenser was interrupted, the reactor was evacuated to about 5 kPa (absolute pressure), and the coolant bath was allowed to gradually warm up to near room temperature whereby the HFP was evaporated off. The contents of the reactor were a white turbid oily liquid recovered in an amount of 116 g. The recovered liquid, 50 g, was treated as in Example 1, yielding 42 g of a colorless, clear, oily liquid. The results of 19 F-NMR analysis of this liquid are shown below. It is evident from the above data that the mix molar ratio of (A)/(B) was 92/8 and the average degree of polymerization was 90. Example 2 The same reactor as used in Example 1 was charged with 13 g of the same initiator as in Example 1. While the agitator was rotated at 120 rpm, the reactor was cooled with a coolant bath adjusted at -35°C. After about 2 hours from the start of cooling, the temperature of the liquid phase within the reactor stabilized at -32°C. The condenser was then cooled at -80°C whereupon 3.9 g of gaseous HFP was fed at a rate of 3.9 g/hr. into the reactor which was maintained under atmospheric pressure. Next, the pressure within the reactor was adjusted to 58 kPa (absolute pressure) whereupon 108 g of HFPO and 54 g of HFP were simultaneously and continuously fed at a rate of 21.6 g/hr. and 10.8 g/hr., respectively, over about 5 hours. The liquid phase in the reactor was at a temperature of -35°C to -38°C during the feed of HFPO. After the feed of HFPO was over, the same operation as in Example 1 was carried out whereby HFP was evaporated off and the contents in the reactor were recovered. The amount was 120 g. The recovered liquid was reacted with methanol as in Example 1, yielding an oily liquid. Similar analysis of this liquid showed that the mix molar ratio of (A)/(B) was 93/7 and the average degree of polymerization was 91. Comparative Example 2 The same procedure as in Comparative Example 1 was carried out except that HFPO and HFP were fed at a rate of 21.6 g/hr. and 10.8 g/hr., respectively, over 5 hours. The temperature of the liquid phase within the reactor was -37°C at the start of feed, gradually increased, and reached 12°C at the end of feed. No HFP could be recovered from this reaction mixture. The reaction mixture was reacted with methanol as in Example 1, yielding an oily liquid. Similar analysis of this liquid showed that the mix molar ratio of (A)/(B) was 53/47 and the average degree of polymerization was 52. The outline of the polymerization process of the foregoing Examples and Comparative Examples is shown in Table 1. E1 CE1 E2 CE2 Coolant bath temperature -35°C -40°C -35°C -40°C Temperature of liquid phase in reactor -35°C to -38°C -35°C to -37°C -35°C to -38°C 12°C to -37°C Pressure of gas phase in reactor 58 kPa 1 atm. 53 kPa 1 atm. Reflux during HFPO feed found no found no HFPO feed time 15 hr. 15 hr. 5 hr. 5 hr. Note that HFP has a boiling point of -29.6°C at 101 kPa (1 atm.), a vapor pressure of 80 kPa at -35°C, and a vapor pressure of 62 kPa at -40°C. When the gas phase pressure within the reactor is below the vapor pressure of HFP at the liquid phase temperature within the reactor as in Example 1, HFP refluxes whereby the liquid phase temperature within the reactor lowers below the temperature of the coolant bath. This suggests that the heat of HFPO polymerization is completely removed in the condenser. In contrast, the liquid phase temperature within the reactor is higher than the temperature of the coolant bath in Comparative Example 1. This suggests that heat removal takes place at the wall of the reactor. A comparison of Example 2 with Comparative Example 2 reveals that when the feed rate of HFPO is increased, the liquid phase temperature within the reactor is appropriately adjusted in Example 2 whereas the liquid phase temperature within the reactor rises far beyond the appropriate range in Comparative Example 2. In the high viscosity HFPO polymerization system as described above, heat of polymerization is efficiently removed so that the polymerization temperature can be kept low. Such heat removal is typically done through a condenser. Since it is easy from the design aspect to increase the heat transfer area of the condenser, HFPO can be rapidly polymerized in a scaled-up system. Although some preferred embodiments have been described, many modifications and variations may be made thereto in the light of the general teachings herein.

Claims: A method in which hexafluoropropene oxide (HFPO) is polymerised in a reactor to form a fluorinated polyether, characterized in that heat of polymerisation of the HFPO is removed by introducing into the reactor a liquefied C 1 - 4 fluorocarbon, maintaining the gas phase pressure in the reactor below the vapour pressure of the liquefied fluorocarbon for the fluorocarbon to evaporate from the polymerisation system. A method according to claim 1 in which the evaporated fluorocarbon is liquefied by cooling or compression and flowed back into the reactor, the liquid phase in the reactor being maintained at temperature in the range -70°C to -10°C. A method according to claim 2 in which the liquid phase in the reactor is maintained at temperature in the range -50°C to -25°C. A method according to any one of the preceding claims in which the liquefied C 1-4 fluorocarbon is fed into the reactor concurrently with HFPO. A method according to any one of the preceding claims in which the liquefied C 1-4 fluorocarbon is used at from 20 to 150 parts by weight per 100 parts by weight of HFPO. A method according to any one of the preceding claims in which the C 1-4 fluorocarbon has a boiling point below -15°C at atmospheric pressure. A method according to any one of claims 1 to 5 in which the C 1-4 fluorocarbon has a boiling point equal to or below that of HFPO. A method according to any one of claims 1 to 5 in which the C 1-4 fluorocarbon is selected from tetrafluoroethane, hexafluoroethane, octafluoropropane, perfluorobutane, trifluoromethane, pentafluoroethane, heptafluoropropane, difluoromethane, hexafluoropropene, tetrafluoroethylene and chlorotrifluoroethylene. A method according to claim 8 in which the C 1-4 fluorocarbon is hexafluoropropene. A method according to any one of the preceding claims in which the reaction system for polymerising the HFPO in the reactor uses a polymerisation initiator which is a mixture of an alkali metal fluoride and an aprotic polar solvent, to which a carbonyl-bearing compound may be added.

Inventors: ARAI MASATOSHI, KISHITA HIROFUMI, KOIKE NORIYUKI, MATSUDA TAKASHI, SATO SHINICHI, ARAI, MASATOSHI, KISHITA, HIROFUMI, KOIKE, NORIYUKI, MATSUDA, TAKASHI, SATO, SHINICHI, Arai, Masatoshi, c/o Silicone-Electr. Mat. Lab., KISHITA, HIROFUMI, C/O SILICONE-ELECTR. MAT. LAB., Koike, Noriyuki, c/o Silicone-Electr. Mat. Lab., Matsuda, Takashi, c/o Silicone-Electr. Mat. Lab., Sato, Shinichi, c/o Silicone-Electr. Mat. Lab.
Applicants: SHINETSU CHEMICAL CO, SHIN-ETSU CHEMICAL CO., LTD.
Application year: 1997
Main classification: C08G65
IPC codes: C08G65