GB1013034A - Process for preparing resin - Google Patents

Process for preparing resin

Info

Publication number
GB1013034A
GB1013034A GB292964A GB292964A GB1013034A GB 1013034 A GB1013034 A GB 1013034A GB 292964 A GB292964 A GB 292964A GB 292964 A GB292964 A GB 292964A GB 1013034 A GB1013034 A GB 1013034A
Authority
GB
Grant status
Application
Patent type
Prior art keywords
polyester
weight
molecular
acid
glycol
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
GB292964A
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Goodyear Tire and Rubber Co
Original Assignee
Goodyear Tire and Rubber Co
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date

Links

Classifications

    • CCHEMISTRY; METALLURGY
    • C08ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08GMACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G63/00Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
    • C08G63/78Preparation processes
    • C08G63/785Preparation processes characterised by the apparatus used

Abstract

A low molecular weight polyester is produced by adding a glycol and a dicarboxylic acid in a molar ratio of 1 : 1.05-1.7 to a preformed low molecular weight polyester of the glycol and acid or another low molecular weight polyester and heating at a temperature above the m.p. of the polyester present at the start of the reaction at a pressure between 20 and 1000 p.s.i.g. The polyester present at the start of the reaction has a molecular weight of 300-2000. The polyester produced may have a higher or lower molecular weight. Glycols specified are ethylene, propylene, butylene, hexylene and decylene glycols, cyclohexane diols, di-(hydroxymethyl) cyclohexanes, di-(b -hydroxy-ethoxy) benzenes, and 2,2-bis[4-(b -hydroxy-ethoxy) phenyl] propane. Acids specified are ortho-, iso- and terephthalic acids, 2,6-naphthalic acid, diphenyl-4,41-dicarboxylic acid, hexahydroterephthalic acid, succinic, adipic and sebacic acids. A copolyester may be prepared from a mixture of acids. The condensation may take place under an N2 atmosphere with stirring at a maximum temperature of 300 DEG C. A catalyst, e.g. zinc or manganous acetate, or an alkali metal alkoxide, may be used. Water vapour may be distilled out at such a rate that the pressure remains constant and a reflux condenser may be used to return ethylene glycol vapour to the reactor. The process may be continuous, a weight of low molecular weight polyester, equal to the weights of acid and glycol added, being withdrawn continuously. The low molecular weight product may be polymerized by addition of a catalyst, e.g. Sb2O3, zinc borate, litharge, lead acetate or MgO, to give a product of intrinsic viscosity of at least 0.40. This reaction may occur under an N2 atmosphere, at a temperature of 260-290 DEG C. and at a pressure below 10 mm. Hg. The eliminated glycol may be recovered. The process may be continuous and the product may be made into films or fibres.ALSO:A polyester of degree of polymerization 1.4-10 is produced by adding a glycol and a dicarboxylic acid in a molar ratio of 1: 1.05-1 7 to a preformed low molecular weight polyester of the glycol and acid or another low molecular weight polyester and heating at a temperature above the m.p. of the polyester present at the start of the reaction and at a pressure of 20-1000 p.s.i.g. The polyester present at the start of the reaction may have a M.W. of 300-2000. The polyester produced may have a higher or lower molecular weight. Glycols specified are: ethylene, propylene, butylene, hexylene and decylene glycols, cyclohexane diols, di-(hydroxymethyl) cyclohexanes, di-(b -hydroxyethoxy) benzenes, and 2,2-bis-[4-(b -hydroxyethoxy) phenyl]propane. Acids specified are g -, iso- and terephthalic, 2,6-naphthalic, diphenyl - 4,41 - dicarboxylic, hexahydroterephthalic, succinic, adipic and sebacic acids. A copolyester may be prepared from a mixture of acids. The condensation may take place under an N2 atmosphere with stirring at a maximum temperature of 300 DEG C. A catalyst, e.g. zinc or manganous acetate or an alkali metal alkoxide may be used. Water vapour may be distilled out at such a rate that the pressure remains constant and a reflux condenser may be used to return ethylene glycol vapour to the reactor. The process may be continuous.
GB292964A 1963-01-29 1964-01-23 Process for preparing resin Expired GB1013034A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US25475463 true 1963-01-29 1963-01-29

Publications (1)

Publication Number Publication Date
GB1013034A true true GB1013034A (en) 1965-12-15

Family

ID=22965468

Family Applications (1)

Application Number Title Priority Date Filing Date
GB292964A Expired GB1013034A (en) 1963-01-29 1964-01-23 Process for preparing resin

Country Status (3)

Country Link
JP (1) JPS494835B1 (en)
DE (1) DE1495955B2 (en)
GB (1) GB1013034A (en)

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2015174A1 (en) * 1969-04-01 1970-10-08
US7649109B2 (en) 2006-12-07 2010-01-19 Eastman Chemical Company Polyester production system employing recirculation of hot alcohol to esterification zone
US7718759B2 (en) 2000-12-07 2010-05-18 Eastman Chemical Company Polyester process using a pipe reactor
US7829653B2 (en) 2007-07-12 2010-11-09 Eastman Chemical Company Horizontal trayed reactor
US7842777B2 (en) 2007-07-12 2010-11-30 Eastman Chemical Company Sloped tubular reactor with divided flow
US7847053B2 (en) 2007-07-12 2010-12-07 Eastman Chemical Company Multi-level tubular reactor with oppositely extending segments
US7858730B2 (en) 2007-07-12 2010-12-28 Eastman Chemical Company Multi-level tubular reactor with dual headers
US7863477B2 (en) 2007-03-08 2011-01-04 Eastman Chemical Company Polyester production system employing hot paste to esterification zone
US7868130B2 (en) 2007-07-12 2011-01-11 Eastman Chemical Company Multi-level tubular reactor with vertically spaced segments
US7868129B2 (en) 2007-07-12 2011-01-11 Eastman Chemical Company Sloped tubular reactor with spaced sequential trays
US7872089B2 (en) 2007-07-12 2011-01-18 Eastman Chemical Company Multi-level tubular reactor with internal tray
US7872090B2 (en) 2007-07-12 2011-01-18 Eastman Chemical Company Reactor system with optimized heating and phase separation
US7943094B2 (en) 2006-12-07 2011-05-17 Grupo Petrotemex, S.A. De C.V. Polyester production system employing horizontally elongated esterification vessel
US9624342B2 (en) 2008-02-06 2017-04-18 Valspar Sourcing, Inc. Process for manufacturing medium and high molecular weight polyesters

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5299125U (en) * 1976-01-23 1977-07-26

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2015174A1 (en) * 1969-04-01 1970-10-08
US7718759B2 (en) 2000-12-07 2010-05-18 Eastman Chemical Company Polyester process using a pipe reactor
US7842778B2 (en) 2000-12-07 2010-11-30 Eastman Chemical Company Polyester process using a pipe reactor
US8114954B2 (en) 2000-12-07 2012-02-14 Grupo Petrotemex, S.A. De C.V. Polyester process using a pipe reactor
US7649109B2 (en) 2006-12-07 2010-01-19 Eastman Chemical Company Polyester production system employing recirculation of hot alcohol to esterification zone
US8470250B2 (en) 2006-12-07 2013-06-25 Grupo Petrotemex, S.A. De C.V. Polyester production system employing horizontally elongated esterification vessel
US7943094B2 (en) 2006-12-07 2011-05-17 Grupo Petrotemex, S.A. De C.V. Polyester production system employing horizontally elongated esterification vessel
US7863477B2 (en) 2007-03-08 2011-01-04 Eastman Chemical Company Polyester production system employing hot paste to esterification zone
US7858730B2 (en) 2007-07-12 2010-12-28 Eastman Chemical Company Multi-level tubular reactor with dual headers
US7868130B2 (en) 2007-07-12 2011-01-11 Eastman Chemical Company Multi-level tubular reactor with vertically spaced segments
US7868129B2 (en) 2007-07-12 2011-01-11 Eastman Chemical Company Sloped tubular reactor with spaced sequential trays
US7872089B2 (en) 2007-07-12 2011-01-18 Eastman Chemical Company Multi-level tubular reactor with internal tray
US7872090B2 (en) 2007-07-12 2011-01-18 Eastman Chemical Company Reactor system with optimized heating and phase separation
US7847053B2 (en) 2007-07-12 2010-12-07 Eastman Chemical Company Multi-level tubular reactor with oppositely extending segments
US7842777B2 (en) 2007-07-12 2010-11-30 Eastman Chemical Company Sloped tubular reactor with divided flow
US7829653B2 (en) 2007-07-12 2010-11-09 Eastman Chemical Company Horizontal trayed reactor
US9624342B2 (en) 2008-02-06 2017-04-18 Valspar Sourcing, Inc. Process for manufacturing medium and high molecular weight polyesters

Also Published As

Publication number Publication date Type
DE1495955A1 (en) 1970-02-19 application
DE1495955B2 (en) 1975-02-20 application
JPS494835B1 (en) 1974-02-04 grant

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