WO1994002522A1 - Process for producing tetrafluoroethylene/hexafluoropropylene copolymer - Google Patents
Process for producing tetrafluoroethylene/hexafluoropropylene copolymer Download PDFInfo
- Publication number
- WO1994002522A1 WO1994002522A1 PCT/JP1993/000949 JP9300949W WO9402522A1 WO 1994002522 A1 WO1994002522 A1 WO 1994002522A1 JP 9300949 W JP9300949 W JP 9300949W WO 9402522 A1 WO9402522 A1 WO 9402522A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- polymerization
- atom
- tetrafluoroethylene
- acid
- copolymer
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F214/00—Copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen
- C08F214/18—Monomers containing fluorine
- C08F214/26—Tetrafluoroethene
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F214/00—Copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen
- C08F214/18—Monomers containing fluorine
Definitions
- the present invention relates to a method for producing a tetrafluoroethylene / hexafluoropropylene copolymer.
- an alkali such as sodium bicarbonate (NaHCO 3) is usually contained in an aqueous medium at the start of polymerization in order to prevent corrosion of the polymerization tank material.
- NaHCO 3 sodium bicarbonate
- acidic substances hydrofluoric acid, etc.
- the acidic substances may corrode the polymerization tank.
- the polymerization initiator In the early stage of polymerization, the polymerization initiator is not effectively used because the polymerization initiator is easily hydrolyzed with an aqueous solution of alkali metal.
- An object of the present invention is to stabilize the molecular weight in the production of a tetrafluoroethylene Z-hexafluoropropylene copolymer by polymerization in an aqueous medium using di (fluoroacyl) peroxide as a polymerization initiator, and to improve the efficiency of use of the initiator. Is to improve
- the present invention has the general formula:
- n is an integer of 4 to 8 when X 1 is a hydrogen atom, and is an integer of 3 to 8 when X 1 is a fluorine atom or a chlorine atom;
- n is an integer of 4 to 8 when X 2 is a hydrogen atom, and 3 to 8 when X 2 is a fluorine atom or a chlorine atom.
- Y 1 is a hydrogen, fluorine or chlorine atom
- p is an integer of 4 to 8 when Y 1 is a hydrogen atom, and 3 to 8 when Y 1 is a fluorine atom or a chlorine atom.
- the present invention provides a method for producing a tetrafluoroethylennohexafluoro propylene copolymer, which comprises charging a fluoroalkylcarboxylic acid represented by the formula:
- FIG. 1 is a graph showing the relationship between the reaction time and ⁇ ⁇ during the copolymerization of tetrafluoroethylene and hexafluoropropylene.
- Full O b alkyl carboxylic ⁇ in acid ⁇ one C P F 2P - groups may be filed either straight or branched.
- fluoralkylcarboxylic acids include ⁇ -hydroperfluoroheptanoic acid, ⁇ -hydroperfluorononanoic acid, ⁇ -hydroperfluoroheptanoic acid, and ⁇ -hydroperfluoroheptanic acid.
- the amount of the fluoroalkyl carboxylic acid to be used is preferably 0.05 to 0.5 part by weight based on 100 parts by weight of water in the polymerization system.
- Polymerization initiator di (Furuoroashiru) Paokisai de of X 1 to be used as a - C m F 2ra - group and X 2 - C n F 2 group may be either straight-chain, branched, identical to each other Or it could be different.
- di- (fluoroacyl) peroxyside di- ( ⁇ -Hydrodecafluoroheptanyl) peroxide, di- ( ⁇ -hydrotetradecafluorooctanoyl) peroxide, di ( ⁇ —High draw hexadecafluorononyl) no.
- the amount of the polymerization initiator used depends on the amount of tetrafluoroethylene (hereinafter, referred to as TFE) in the target copolymer. It is appropriately determined according to the ratio to fluoropropylene (hereinafter, referred to as HFP) and the molecular weight, but is usually about 0.01 to 1 part by weight based on 100 parts by weight of the monomer. However, since the decomposition rate of this polymerization initiator is relatively fast and its concentration tends to decrease considerably during the polymerization reaction, it is desirable to add it as needed during the polymerization reaction.
- TFE tetrafluoroethylene
- HFP fluoropropylene
- the Y! -CpFzp- group of the fluoroalkyl carboxylic acid is replaced with the di (fluoroacyl) peroxyside X 2 - C n F 2n - one of the radicals is preferably identical to both properly more preferred.
- the polymerization reaction is started by charging pure water and fluoroalkyl carboxylic acid into a pressure vessel, adding TFE and HFP, and further adding a polymerization initiator. At that time, the ratio of water: monomer should be about 1: 1 to 10: 1 by volume, especially about 2 ::! To 5: 1.
- the proportion of TFE in the TFEZEZP monomer mixture is determined according to the composition of the target copolymer, but at about 20 to 25 ° C, the following relationship generally holds.
- Water is used as the reaction medium, and if necessary, an appropriate amount of a solvent capable of dissolving TFE and HFP can be added.
- a solvent capable of dissolving TFE and HFP
- Preferred examples of such a solvent include trichloro-mouthed trifluoroethane, monofluorotrichloromethane, and other fluorinated solvents.
- a suspension stabilizer such as polyvinyl alcohol, sodium-carboxymethyl cellulose, sodium bicarbonate, borax, etc. may be added as necessary. Good.
- the polymerization temperature is mainly limited by the decomposition rate of the polymerization initiator
- the decomposition of the polymerization initiator in the presence of water proceeds as a first-order reaction
- the rate constant k is, for example, as follows.
- the polymerization temperature in the range of usually 0 to 35 ° C, preferably about 0 to 28 ° C.
- the pressure during the polymerization is determined according to the mixing ratio of the TFEZHFP mixed monomer, the presence or absence of a solvent, the polymerization temperature, and the like. Generally, when a solvent is not used, a pressure of about 5 to 15 kg / cm 2 (gauge pressure, the same applies hereinafter) is appropriate. When using a solvent such as tri-chloro-trifluoroethane as the solvent, the pressure should be about 0.5 to 15 Kg / cm 2 , depending on the ratio between the solvent and the monomer. Is appropriate.
- the reaction may be continued by adding only TFE to compensate for the decrease in pressure, and the consumption of each monomer may be reduced.
- TFE and HFP may be added in the appropriate amount.
- the polymerization time depends not only on the yield of the desired copolymer, but also on the amount of the polymerization initiator used, the proportion of TFE and HFP charged, and the polymerization temperature. Thus, usually, it is selected from the range of about 2 to 100 hours. During the polymerization reaction, the presence of oxygen should be avoided.
- the TFE / HFP copolymer obtained by the method of the present invention is stable without changing the melt viscosity in the melt extrusion step or the step of heating and molding the pelletized product after extrusion, and can be colored black.
- the method of the present invention is an aqueous reaction, and therefore, is much more industrially advantageous than a solvent-based reaction). It can be used advantageously.
- Table 1 shows the reaction conditions, the yield of the polymer and the physical properties in the polymerization.
- the specific melt viscosity of the polymer was measured by the following method. Specific melt viscosity means seen hanging melt viscosity measured at 372 ° C under a shear force of 0.475kgZciE 2. That is, the values are measured with a melt indexer. The polymer is filled into a cylinder with an inner diameter of 11.4 mm, kept at 372 for 5 minutes, and then loaded with a piston load of 5 kg.
- TFE feed pressure [Kg / cm 2 G] 8.30 8.30 Furuo ⁇ alkyl carboxylic acid [parts by weight] 0 1.0 fee NaHCO 3 [parts by weight] 1.25 0
- Table 2 shows the results of comparing the metal contents of the molded articles after heat melting.
- Example 1 shows that the metal content is small.
- hydrolysis of the initiator in the early stage of polymerization is suppressed and the initiator is effectively used, so that the amount of the initiator in the early stage of polymerization can be reduced by 30% or more.
- the total amount of catalyst used can be reduced, for example, by 20 to 30% or more.
- the pH is constant from the beginning to the end of the polymerization, and a copolymer with a constant molecular weight can be obtained with high reproducibility. Low metal content in polymer due to low corrosion of polymerization tank during polymerization. Further, the amount of coloring of the copolymer after heating and melting is small.
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- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
- Polymerisation Methods In General (AREA)
- Polymerization Catalysts (AREA)
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US08/211,022 US5399643A (en) | 1992-04-22 | 1992-07-09 | Method for preparation of tetrafluoroethylene/hexafluoropropylene copolymer |
DE69310126T DE69310126T2 (de) | 1992-07-22 | 1993-07-09 | Verfahren zur herstellung eines tetrafluorethylen/hexafluorpropen copolymers |
EP93914980A EP0606492B1 (en) | 1992-07-22 | 1993-07-09 | Process for producing tetrafluoroethylene/hexafluoropropylene copolymer |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP04195147A JP3114374B2 (ja) | 1992-07-22 | 1992-07-22 | テトラフルオロエチレン/ヘキサフルオロプロピレン共重合体の製造方法 |
JP4/195147 | 1992-07-22 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1994002522A1 true WO1994002522A1 (en) | 1994-02-03 |
Family
ID=16336222
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP1993/000949 WO1994002522A1 (en) | 1992-04-22 | 1993-07-09 | Process for producing tetrafluoroethylene/hexafluoropropylene copolymer |
Country Status (5)
Country | Link |
---|---|
US (1) | US5399643A (ja) |
EP (1) | EP0606492B1 (ja) |
JP (1) | JP3114374B2 (ja) |
DE (1) | DE69310126T2 (ja) |
WO (1) | WO1994002522A1 (ja) |
Families Citing this family (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
IT1271622B (it) * | 1994-03-21 | 1997-06-04 | Ausimont Spa | Processo di (co) polimerizzazione in sospensione per la preparazione ddi fluoropolimeri termoplastici contenenti idrogeno |
US5831131A (en) * | 1995-08-30 | 1998-11-03 | E. I. Du Pont De Nemours And Company | Process for preparing peroxides |
US5962746A (en) * | 1996-08-26 | 1999-10-05 | E. I. Du Pont De Nemours And Company | Process for preparing peroxides |
CN1371363A (zh) * | 1999-08-30 | 2002-09-25 | 纳幕尔杜邦公司 | 氟代烯烃聚合用低温引发剂 |
ITMI20010482A1 (it) * | 2001-03-08 | 2002-09-08 | Ausimont Spa | Perfluorodiacilperossidi iniziatori di polimerizzazione |
WO2005042636A1 (ja) * | 2003-10-31 | 2005-05-12 | Junkosha Inc. | フッ素樹脂組成物 |
CN101440143B (zh) * | 2007-11-20 | 2011-04-06 | 山东东岳神舟新材料有限公司 | 一种增加聚全氟乙丙烯树脂端基稳定性的聚合工艺 |
CN102675519A (zh) * | 2012-06-11 | 2012-09-19 | 江苏梅兰化工有限公司 | 用全氟酰基过氧化物类引发剂制备聚全氟乙丙烯的方法 |
CN111936572A (zh) * | 2018-03-27 | 2020-11-13 | 大金工业株式会社 | 成型材料以及管 |
CN114206953A (zh) * | 2019-08-07 | 2022-03-18 | 大金工业株式会社 | 含氟聚合物的制造方法 |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5740847B2 (ja) * | 1975-06-23 | 1982-08-31 | ||
JPS5928211B2 (ja) * | 1975-12-16 | 1984-07-11 | ダイキン工業株式会社 | テトラフルオロエチレン − ヘキサフルオロプロピレンキヨウジユウゴウタイ セイゾウホウホウ |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE1124242B (de) * | 1955-10-22 | 1962-02-22 | Hoechst Ag | Verfahren zur Polymerisation von polymerisationsfaehigen halogenhaltigen monomeren Verbindungen |
GB1260611A (en) * | 1969-04-21 | 1972-01-19 | Daikin Ind Ltd | Improvements in or relating to the polymerization of fluorine-containing haloolefins |
JPS4928675B1 (ja) * | 1970-01-30 | 1974-07-29 | ||
JPS61152652A (ja) * | 1984-12-27 | 1986-07-11 | Daikin Ind Ltd | 含フツ素ジアシルパ−オキサイドおよびその用途 |
JPH04292605A (ja) * | 1991-03-19 | 1992-10-16 | Nippon Oil & Fats Co Ltd | フルオロアルキル化されたポリマービーズ |
-
1992
- 1992-07-09 US US08/211,022 patent/US5399643A/en not_active Expired - Lifetime
- 1992-07-22 JP JP04195147A patent/JP3114374B2/ja not_active Expired - Fee Related
-
1993
- 1993-07-09 DE DE69310126T patent/DE69310126T2/de not_active Expired - Fee Related
- 1993-07-09 EP EP93914980A patent/EP0606492B1/en not_active Expired - Lifetime
- 1993-07-09 WO PCT/JP1993/000949 patent/WO1994002522A1/ja active IP Right Grant
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5740847B2 (ja) * | 1975-06-23 | 1982-08-31 | ||
JPS5928211B2 (ja) * | 1975-12-16 | 1984-07-11 | ダイキン工業株式会社 | テトラフルオロエチレン − ヘキサフルオロプロピレンキヨウジユウゴウタイ セイゾウホウホウ |
Non-Patent Citations (1)
Title |
---|
See also references of EP0606492A4 * |
Also Published As
Publication number | Publication date |
---|---|
DE69310126D1 (de) | 1997-05-28 |
US5399643A (en) | 1995-03-21 |
JPH0641247A (ja) | 1994-02-15 |
DE69310126T2 (de) | 1997-09-18 |
EP0606492B1 (en) | 1997-04-23 |
EP0606492A4 (en) | 1994-11-23 |
JP3114374B2 (ja) | 2000-12-04 |
EP0606492A1 (en) | 1994-07-20 |
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