PROCESS FOR PRODUCING PROPYLENE-TETRAFLUOROETHYLENE COPOLYMER

Abstract: A propylene-tetrafluoroethylene copolymer is produced by copolymerizing propylene and tetrafluoroethylene in an aqueous medium in the presence of a redox catalyst comprising a combination of (1) a water soluble persulfate, (2) a water soluble iron salt, (3) a hydroxymethanesulfinate and (4) ethylenediaminetetraacetic acid or a salt thereof at a pH of 7 to 10.5, preferably 8 to 10.5.

Description: PROCESS FOR PRODUCING PROPYLENE TET RAFLUOROETHYLENE COPOLYMER The present invention relates to a process for producing a propylene-tetrafluoroethylene copolymer. More particularly, it relates to a novel process for producing the propylene-tetrafluoroethylene copolymer by copolymerizing propylene and tetrafluoroethylene in an aqueous medium in the presence of a specific redox catalyst to attain smooth copolymerization at high polymerization velocity without discoloring the latex or the copolymer and with high storage stability of the latex. Propylene-tetrafluoroethylene copolymers are known as vulcanizable elastic polymers having excellent heat resistance and chemical resistance. The copolymerization of propylene and tetrafluoroethylene in an aqueous medium has been disclosed in Japanese Examined Patent Publication No. 19188/1965, No. 4115/1978 and U.S. Patent 3,467,635. It has also been proposed that a propylene-tetrafluoroethylene copolymer having high molecular weight can be obtained by copolymerization at a relatively low temperature such as 0 to 50 0C if a redox catalyst comprising a water soluble persulfate/a water soluble thiosulfate or sulfite/a water soluble iron salt as a catalyst for the copolymerization in an aqueous medium, as disclosed in British Patent No. 1,456,615. On the other hand, many redox catalysts for emulsion polymerization at relatively low temperatures have been reported from long time ago. Sometimes catalytic activity is specifically dependent upon a combination of the redox catalyst with a particular monomer. The limitation for the selection is more severe in the case of multi-component copolymerization and is related to various factors such as reactivity of the monomer, efficiency of initiation, chain transfer, kinetic chain length, pH of the medium and the stabilities of the monomer and the catalyst. Therefore, it is not eas- to find an optimum redox catalyst for a specific polymerization system. In the case of a copolymerization system having high chain transfer activity and short kinetic chain length such as a copolymerization of propylene and tetrafluoroethylene, the selection of an optimum redox catalyst is especially difficult. For example, most catalysts having high catalytic activity for emulsion polymerizations of tetrafluoroethylene at low temperature are not active for copolymerizations of propylene and tetrafluoroethylene at low temperature. According to the inventor's studies, the specific redox catalysts disclosed in British Patent No. 1,456,615 are active for the copolymerization of propylene and tetrafluoroethylene at a low temperature, but copolymerizations at a low temperature with such catalysts have the following disadvantages. First, the copolymerization velocity is not high enough, the maximum being about 17 g./l.hr. The discoloring (dark-coloring) of the latex and the polymer is remarkably severe even when lengthy and complicated washing and purification steps are employed because of the use of an activating solution containing a reducing sugar. Moreover, the COD of the waste solution in the coagulation of the latex and the washing is remarkably high, which renders the treatment of the waste solution difficult. Furthermore, the storage stability of the latex is not high enough and sedimentation and separation with long storage of the latex. The reducing sugar is perishable and causes discoloring and an unpleasant odour. The preparation of the activated solution is complicated and the activated solution is immediately inactivated by contact with oxygen in air. Therefore, the preparation is not easy and the catalytic activity is not stable. It is an object of the present invention to overcome the above-mentioned disadvantages in a copolymerization of propylene and tetrafluoroethylene at a low temperature in an aqueous medium. The present invention provides a process for producing a propylene-tetrafluoroethylene copolymer which comprises copolymerizing propylene and tetrafluoroethylene in an aqueous medium in the presence of a redox catalyst of comprising (1) a water soluble persulfate and (2) a water soluble iron salt characterised in that the catalyst also includes (3) a hydroxymethanesulfinate and (4) ethylenediaminetetraacetic acid or a salt thereof and the copolymerization is carried out at pH 7 to 10.5. The inventors have studied the copolymerization of propylene and tetrafluoroethylene in an aqueous medium at a low temperature, which had not hitherto been easily carried out, so as to overcome the above-mentioned disadvantages in the process. As a result, it has been found that the specific redox catalyst of the combination of (1) a water soluble persulfate, (2) a water soluble iron salt, (3) a hydroxymethanesulfinate and (4) ethylenediaminetetraacetic acid or a salt thereof (EDTA) is effective for this purpose and the specific redox catalyst has high catalytic activity in an alkaline aqueous solution at pH of up to 10.5. Using the process of the present invention, it is possible to copolymerize propylene and tetrafluoroethylene at high copolymerization velocity in an aqueous medium. thus, the copolymerization can be smoothly performed at a low temperature, suitably lower than 400C and a propylene-tetrafluoroethylene copolymer of high molecular weight can be obtained. In the process of the present invention, smooth copolymerization in an aqueous medium is attained and the stability of the resulting latex is excellent. Coloring of the latex and the polymer is not found and the COD of the waste solution can be remarkably reduced. The copolymerization can be continued for a long time by continuously adding the hydrixymethanesulfinate as a reducing agent. The copolymerization velocity can be controlled as desired for example by adjusting the amount of the hydroxymethanesulfinate. In the process of the present invention, the molar ratio of C2F4/C3H6 in the reaction system is not critical and can be varied within a broad range, it is usually in a range of 95/5 to 20/80. In the process of the present invention, when the content of C 2F4 is larger, the copolymerization velocity is faster and the copolymer having high molecular weight is effectively produced. Therefore, the molar ratio of C2F4/C3H6 is preferably 95/5 to 40/60 especially 93/7 to 70/30. In the process of the present invention, it is possible to copolymerize C 2F4 and C 3116 as the major components with one or more other coinonomers, which make a multi-component polymer for the proper object by selecting the molar ratios. In the process of the present invention, various components for the specific redox catalyst can be used. Suitable water soluble per sulfates as the first component include ammonium or alkali metal salts such as ammonium persulfate, potassium persulfate and sodium persulfate. Suitable water soluble iron salts as the second component include divalent or trivalent iron salts such as ferrous sulfate, ferric sulfate, ferrous nitrate, ferric nitrate, ferrous chloride, ferric chloride, ammonium ferrous sulfate, and ammonium ferric sulfate. The ferric or ferrous sulfate is especially preferable as the second component. The first and second components are combined with a hydroxymethanesulfinate (referring to as HMSA) such as CH2(OH)SO2Na and ethylenediaminetetraacetic acid or a salt thereof (referring to EDTA). EDTA is preferably sodium salt and, the other salts or hydrate or ethylenediaminetetraacetic acid itself can be used. HMSA is preferably an alkali metal salt such as sodium or potassium salt thereof. It is possible to be a hydrate thereof or to contain a small amount of hydroxymethanesulfonate. The ratios of the components of the specific redox catalyst used in the present invention can be selected as desired. The following facts are found. With regard to the copolymerization velocity depending on the catalytic component content, the water soluble persulfate content causes low influence, but the iron ion content and HMSA content cause relatively high influence. EDTA has high chelate forming stability with iron ion and EDTA is used for resulting effective iron ion concentration as the catalytic component. Therefore, EDTA is incorporated at an equivalent concentration to the iron ion concentration in the optimum condition. In usual, the water soluble per sulfate is incorporated at a concentration of 1 to 50 m mol/liter; the water soluble iron salt and iEDTA are respectively incorporated at each concentration of 0. 05 to 5 m mol/liter; and HMSA is incorporated at a concentration of 0. 5 to 50 m mol/liter in the aqueous medium. When the concentrations of the water soluble iron salt and EDTA are set in relatively high level, the concentration of HMSA can be set in relatively low level, and vice versa. In order to give a desired copolymerization velocity, the concentrations of the components can be controlled as desired. The specific redox catalyst used in the present invention is usually used at a concentration of 0. 001 to 5 wt. t0 preferably 0. 01 to 2 wt. % based on the aqueous medium. The content of the specific redox catalyst can be greater than the range, and there is tendency to decrease the molecular weight of the resulting copolymer and it is economically disadvantageous. It is preferably to select the concentration from said range. The copolymerization is usually carried out at a relatively low temperature such as 0 to 50"C. If a reaction temperature is too high, the molecular weight of the resulting copolymer is lowering and the decomposing velocity of the catalyst is too fast and accordingly, the efficiency is lower. If a reaction temperature is too low, the copolymerization velocity is too low to attain a practical operation. The reaction temperature is preferably in a range of about 5 to 45"C especially about 10 to 40"C. The pH dependency of the copolymerization velocity is high as the characteristic of the copolymerization of the present invention. Thus, pH is preferably in a range of 7 to 10. 5, especially 8 to 10. 5. If pH is out of the range, the copolymerization velocity is lower. If pH is higher than 10. 5, the copolymerization velocity is especially lower. In the process of the present invention, the other condition for the copolymerization is not critical and it is possible to employ a batch operation or a continuous operation under stirring. The pressure in the copolmerization is not critical and is usually less than 100 kg./cmê(gauge), preferably in a range of 5 to 80 kg./cmê(gauge), especially 10 to 50 kg. /cm2 (gauge). In the process of the present invention, it is possible to use various additives which are used in the similar copolymerizations in an aqueous medium. For example, an emulsifier required for an emulsion polymerization can be used. Suitable emulsifiers include conventional polyfluoro- or polyfluorochloro-alkyl type emulsifiers such as water soluble salts of polyfluoroaliphatic carboxylic acids and perfluoroaliphatic carboxylic acids and water soluble salts of polyfluorochloroaliphatic carboxylic acids or perfluorochloroaliphatic carboxylic acids and phosphates or sulfates of polyfluoroalcohols. It is also possible to use nonfluorinated emulsifiers such as sulfates of higher fatty alcohol or water soluble salts of aromatic sulfonic acids. A mixture of the emulsifiers can be used. The emulsifier is usually used at a concentration of about 0.0001 to 10 wt.% preferably about 0.001 to 5 wit.% based on the aqueous medium. It is also possible to incorporate a dispersion stabilizer such as trifluorotrichloroethane, liquid chlorinated hydrocarbons, liquid saturated hydrocarbons, and a pH regulator, a buffering agent, an accelerator, and a chain transfer agent. In the present invention, it is preferable to carry out the copolymerization in a weak alkaline condition (pH of about 9 to 10) in view of copolymerization velocity. It is suitable to incorporate a pH regulator such as sodium hydroxide, potassium hydroxide, ammonium hydroxide and others, and a buffering agent such as sodium hydrogenphosphate, sodium borate and others. It is possible to incorporate a water soluble organic solvent such as methanol, tert-butanol, and methyl acetate so as to increase the copolymerization velocity In accordance with the process of the present invention, the product is obtained in a form of a dispersion such as an emulsion dispersing the propylene-tetrafluoroethylene copolymer in an aqueous medium. The propylene- tetrafluoroethylene copolymer having elasticity can be easily separated from such dispersion by a conventional manner or a well-known manner. It is possible to use the product in the form of a dispersion or a concentrated dispersion, in an operation for fabrication. The resulting copolymers have advantages of less discoloring and excellent electric properties, chemical resistance, heat resistance and mechanical resistance. These can be used for various usages in view of these characteristics. The present invention will be illustrated by certain examples and references which are provided for purposes of illustration only and are not intended to be limiting the present invention. EXAMPLE 1: In a 100 ml. stainless steel ampoule, (pressure re 2 sistanceof 50 kg. /cm ), 40 g, of deionized water, 5 g. of tert- butanol, 0. 5 g. of C8F17COONH4, 1.0 g. of Na2HPO4, 12H20, and 0. 1 g. of NaOH were charged and then, 0. 5 g. of ammonium persulfate dissolved in a small amount of water was added. The ampoule was cooled with liquid nitrogen, and 5 g. of an aqueous solution containing 0. 0075 g. of FeSO4. 7H20, 0. 009 g. of EDTA (disodium salt of ethylenediaminetetraacetic acid dihydrate) and 0. 04 g. of CH2(OH)SO2Na was charged and the ampoule was evacuated. The aqueous medium containing the catalyst had pH of 9. 1. Into the ampoule, 8. 2 g. of a mixed gas of propylene and tetrafluoroethylene (molar ratio of C2:F4/C3H6 of 85/15) was fed and the ampoule was vibrated in a constant temperature vessel at 250C to carry out the copolymerization. As a result, propylene-tetrafluoroethylene copolymer having a molecular weight of 133, 000 and a molar ratio of C2F4/C3116 of 55|45 was obtained at a copolymerization velocity of 120 g. /1. hr. EXAMPLES 2 to 4 and REFERENCES 1 and 2 In accordance with the process of Example 1 except varying kinds and amounts of the pH regulator and the buffering agent (NaHPO4.12H2O, NaOH etc. ) to change pH of the aqueous medium containing the catalyst as shown in Table 1, each copolymerization was carried out. The copolymerization velocities resulted by these copolymerizations are shown in Table 1. Table 1 EMI11.1 <tb> <SEP> Copolymerization <tb> <SEP> pH <SEP> velocity <SEP> ( <SEP> .11. <SEP> hr. <SEP> ) <tb> Reference <SEP> 1 <SEP> 5. <SEP> 5 <SEP> 4. <SEP> 5 <tb> Example <SEP> 2 <SEP> 7. <SEP> 9 <SEP> 20 <tb> Example <SEP> 3 <SEP> 9.7 <SEP> 120 <tb> Example <SEP> 4 <SEP> 10.5 <SEP> 110 <tb> Reference <SEP> 2 <SEP> 10.8 <SEP> 1.8 <SEP> <tb> EXAMPLE 5: In a 2 liter stainless steel autoclave having pressure resistance of 50 kg./cmê equipped with a stirrer and a jacket, 1014 g. of deionized water, 116 g. of tert-butanol, 5. 8 g. of C8 F C8F17COONH4, 34. 8 g. of Na2HPO4. 121120 and 2. 5 g. of NaOH were charged and then, 11. 6 g. of ammonium persulfate was added. An aqueous solution of 0. 058 g. of FeSO4. 7H2O, 0. 069 g. of EDTA in 50 g. of water was added and the autoclave was closed and evacuated to be a reduced pressure and nitrogen gas was fed to a pressure of 30 kg./cmê to purge it. The autoclave was evacuated to be a reduced pressure and was maintained at 22"C. Into the autoclave, 139 g. of C 2F4 monomer and 7 g. of C3116 monomer (molar ratio of C2F4/C 3116 of 93/7) were fed and then, a deionized water solution containing 8.7 wt. % of CH2(OX)SO2Na and 1 wt. % of NaOH was fed into the autoclave by a constant volumetric pump at a rate of 2. 4 ml. /hour (pH of 9. 5). A mixed gas of propylene and tetrafluoro ethylene (molar ratio of 56/44) was continuously fed so as to compensate the reduction of the pressure in the autoclave. The pressure in the reaction was 25 kg./cmê . After 12 hours for the reaction, a latex having a concentration of the polymer of 25. 6 wt. % was obtained at a selectivity of 99. 3% and 397 g. of the polymer was separated. An average copolymerization velocity was 28. 7 g. /1. hr. The resulting latex had pH of 8. 5 and was a stable white latex. The polymer separated by the addition of an aqueous solution of calcium chloride was a white spongy polymer having a C2F4 content of 56. 5 mol. % and a molecular weight of 202, 000. EXAMPLES 6 to 7: In accordance with the process of Example 5, except varying a molar ratio of C2F4/C3X6 (initial charge), a molar ratio of C2F4/C3H6 (additional charge), concentrations of iron ion and EDTA and a rate of the aqueous solution of CH2(OH)SO2Na(8.7 wt.%, without SaOili and a time for the copolymerization as shown in Table 2, eac'r copolerization was carried out. (In Examples 6 and 7, NaOH lt-as not incorporated). The results are shown in Table 2. Table 2 EMI13.1 <tb> <SEP> Example <SEP> 6 <SEP> Example <SEP> 7 <tb> Molar <SEP> ratio <SEP> of <SEP> C2F4/C3H6 <SEP> 85/15 <SEP> 93/7 <tb> (initial <SEP> charge) <tb> Molar <SEP> ratio <SEP> of <SEP> C2F4/C3H6 <SEP> <tb> (additional <SEP> charge)55/45 <SEP> 56.5/43.5 <SEP> <tb> Concentrations <SEP> of <SEP> iron <SEP> ion <SEP> and <SEP> <SEP> 0.54 <SEP> 0.18 <SEP> <tb> EDTA <SEP> (m <SEP> mol/l. <SEP> ) <SEP> <tb> Feed <SEP> rate <SEP> of <SEP> aqueous <SEP> solution <SEP> of <tb> CH2(OH)SO2Na <SEP> (ml./hr.) <SEP> 302 <SEP> <SEP> 9.3 <SEP> <tb> Polymerization <SEP> time <SEP> (hr. <SEP> ) <SEP> 4.0 <SEP> 8.5 <SEP> <tb> Yield <SEP> of <SEP> polymer <SEP> (g.) <SEP> 258 <SEP> 550 <tb> <SEP> * <SEP> 0.80/ <SEP> 0.95/ <tb> <SEP> molecular <SEP> weight <SEP> 1. <SEP> 33x105 <SEP> 1. <SEP> 8x105 <tb> C2F4 <SEP> component <SEP> in <SEP> <SEP> polymer <SEP> 54. <SEP> 8 <SEP> 56. <SEP> 2 <SEP> <tb> <SEP> (mol <SEP> %) <tb> Note: *[#] Intrinsic viscosity in tetrahydrofuran at 30 C. EXAMPLE 8: In the autoclave used in Example 5, 1014 g. of deionized water, 116 g. of tert-butanol, 5. 8 g. of C8F17COONH4, 34.8 g. of Na2HPO4. 12H20 and 2. 5 g. of NaOH were charged and then, ammonium per sulfate was added at a ratio of 44 m mol/l. An aqueous solution of FeSO4.7H2O and EDTA was added to give ratios of 0. 18 m mol/l. of FeSO4. 71120 and 0. 18 m mol/l. of EDTA. In accordance with the process of Example 5, the monomers were fed at a molar ratio of C 2F4/C3N6 of 93/7 and CH2(OH)SO2Na was fed at a rate of 1.6 g. /hr. and a molar ratio of C2F4/C3H6 for the additional charge of the monomers was 56. 5/43. 5, and a copoly 2 merization was carried out at 25 C under a pressure of 25 kg. /cm After 1. 3 hours for the copolymerization, a latex having a concentration of the polymer of 11. 8 wt. % was obtained at a selectivity of 99% and 155 g. of the polymer was separated. An average copolyuneriza- tion velocity was 100 g. /1. hr. The resulting latex was a stable white latex. The polymer separated by the salting-out was a white spongy polymer having a C2F4 content of 56. 5 mol % and a molecular weight of 195,000. EXAMPLE 9: In accordance with the process of Example 5 except that glycidyl vinyl ether (GVE) was added as a third monomer at a ratio of 2 mol % based on the total monomers and 40% of tert-butanol was substituted by sec-butanol for the adjustment of a molecular weight of the polymer, a copolyrnerization was carried out. GVE was continuously fed during the copolymerization by a pressure resistant constant volumetric pump to give said ratio. After 3. 6 hours for the copolymerization, a latex having a concentration of the polymer of 14. 6 wt. % was obtained and 200 g. of the polymer was separated. According to an NMR analysis, the polymer had 56 mol % of C2F4 component, 42 mol % of C 3116 component and 2 mol % of GVE. The polymer had an intrinsic viscosity of 0. 42 (in tetrahydrofuran at 30"C). EXAMPLE 10: In accordance with the process of Example 5 except that 17. 4 g. of C12H25SO4Na was used instead of C8Fl,;,COONH4, and the aqueous solution of CH2(OH)SO2Na was fed at a rate of 9.4 ml. /hr., a copolymerization was carried out. As a result, a polymer having a molecular weight of 105,000 and C F content of 56 mol % was obtained at a copolymerization velocity of 57 g. /1. hr. EXAMPLE 11: In accordance with the process of Example 1 except varying the temperature for the copolymerization from 25"C to 10 C, a copolymerization was carried out. As a result, a polymer having a molecular weight of 150, 000 and a molar ratio of C2F4/C3116 component of 55/45 was obtained at a copolymerization velocity of 35 g. /1. hr.

Claims: CLAIMS 1) A process for producing a propylene-tetrafluoroethylene copolymer which comprises copolymerizing propylene and tetrafluoroethylene in an aqueous medium in the presence of a redix catalyst of comprising (1) a water soluble persulfate and (2) a water soluble iron salt characterised in that the catalyst also includes (3) a hydroxymethanesulfinate and (4) ethylenediaminetetraacetic acid or a salt thereof and the copolymerization is carried out at pH 7 to 10.5.. 2) A process according ot claim 1 characterized in that the copolymerization is carried out at pH 8 to 10.5. 3) A process according to claim I or claim 2 characterized in that the temperature for the copolymerization is in a range of 0 to 50 C. 4) A process according to any preceding claim characterized in that the molar ratio of tetrafluoroethylene to propylene is in a range of 95/5 to 40/60.

Inventors: HISASUE, MICHIO, KOJIMA, GEN
Applicants: ASAHI GLASS COMPANY LTD.
Application year: 1980
Main classification: C08F210
IPC codes: C08F214, C08F210