CA2263578A1 - Method for preparing poly-p-dioxanone polymer - Google Patents
Method for preparing poly-p-dioxanone polymer Download PDFInfo
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- CA2263578A1 CA2263578A1 CA002263578A CA2263578A CA2263578A1 CA 2263578 A1 CA2263578 A1 CA 2263578A1 CA 002263578 A CA002263578 A CA 002263578A CA 2263578 A CA2263578 A CA 2263578A CA 2263578 A1 CA2263578 A1 CA 2263578A1
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- dioxanone
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/02—Polyesters derived from hydroxycarboxylic acids or from polycarboxylic acids and polyhydroxy compounds
- C08G63/06—Polyesters derived from hydroxycarboxylic acids or from polycarboxylic acids and polyhydroxy compounds derived from hydroxycarboxylic acids
- C08G63/08—Lactones or lactides
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/66—Polyesters containing oxygen in the form of ether groups
- C08G63/664—Polyesters containing oxygen in the form of ether groups derived from hydroxy carboxylic acids
Abstract
Poly-p-dioxanone is prepared in a process comprising: (a) heating a reaction mixture comprising p-dioxanone and an effective amount of a polymerization catalyst under conditions of temperature and pressure effective to produce a reaction product mixture comprising molten poly-p-dioxanone and unreacted p-dioxanone; (b) adding to said reaction product mixture a cyclic anhydride under conditions effective for reaction of the poly-p-dioxanone with the cyclic anhydride to form an end-capped poly-p-dioxanone; (c) exposing the reaction product mixture to a temperature within the range of 50 to 150 ~C
under reduced pressure and removing unreacted p-dioxanone from the reaction product mixture; and (d) recovering the end-capped poly-p-dioxanone. The invention process permits the economical production of high molecular weight poly-p-dioxanone in the melt.
under reduced pressure and removing unreacted p-dioxanone from the reaction product mixture; and (d) recovering the end-capped poly-p-dioxanone. The invention process permits the economical production of high molecular weight poly-p-dioxanone in the melt.
Description
CA 02263~78 1999-02-17 W O~ 7 PCT~EP97/04730 METHOD FOR PREPARING POLY-P-DIOXANONE POLYMER
This invention relates to the preparation of poly-p-dioxanone. In a specific aspect, the invention relates to the preparation of high molecular weight poly-p-dioxanone in the melt.
p-Dioxanone is known to be readily polymerized in the solid state below the melting point (about 110 ~C) of the polymer. With active polymerization catalysts such as aluminium and zinc complexes, high molecular weight polymer can be obtained with conversions of p-dioxanone monomer to polymer approaching 100%.
To permit commercial scale-up of the polymerization without adversely affecting process economics, it would be desirable to carry out the polymerization reaction in the melt rather than in the solid state. However, as a result of the dynamic chemical equilibrium between p-dioxanone and poly-p-dioxanone above the melting point of the polymer, conversion of monomer to polymer in the melt ~s typically limlted to about 78%. Removal and recovery of unreacted monomer from the melt is difficult because of the tendency, given this dynamic equilibrium, of the polymer to degrade or lose molecular weight as the monomer is removed.
It is therefore an object of the invention to provide a process for preparing high molecular weight poly-p-dioxanone in the melt.
According to the invention, poly-p-dioxanone is prepared in a process comprising:
CA 02263~78 1999-02-17 W O 98/08887 PCT~P97/04730 (a) heating a reaction mixture comprising p-dioxanone and an effective amount of a polymerization catalyst under conditions of temperature and pressure effective to produce a reaction product mixture comprising molten poly-p-dioxanone and unreacted p-dioxanone;
(b) adding to said reaction product mixture a cyclic anhydride under conditions effective to produce an end-capped poly-p-dioxanone;
(c) maintaining the reaction product mixture comprising end-capped poly-p-dioxanone under reduced pressure at a temperature within the range of 50 to 150 ~C for a time effective for removal of a major portion of the unreacted p-dioxanone from the reaction product mixture; and (d) recovering said end-capped poly-p-dioxanone.
The invention process permits the production of high molecular weight poly-p-dioxanone in the melt.
The starting monomer for preparation of the desired high molecular weight poly-p-dioxanone is an optionally alkyl-substituted 2-p-dioxanone according to the formula O ~OXR2 Rl ~ 0 H
in which each of R1 and R2 can be H or C1_3 alkyl. The monomer can be prepared, for example, by the oxidative dehydrogenation of dialkylene glycols such as diethylene glycol. To prepare high molecular weight polymer, it is desirable to use monomer of a purity of at least about 98%. Such purity can generally be achieved by distilla-tion.
If desired for modification of polymer properties, other cyclic lactones, e.g., such as lactide and glycolide can be copolymerized with the p-dioxanone. As CA 02263~78 1999-02-17 used herein, "poly-p-dioxanone" shall refer to polymers comprising p-dioxanone monomer units and up to about 40 mole percent other cyclic lactone comonomer units.
The polymerization reaction is carried out in the presence of an effective amount of a polymerization catalyst. Suitable polymerization catalysts include, for example, organo tin compounds such as dibutyl tin oxide, dibutyl tin dilaurate and dibutyl tin di-2-ethylhexanoate (U.S. 3, 695,941~, organozinc compounds such as diethyl zinc (U.S. 3,063,968) and organoaluminium compounds such as triisobutyl aluminium (U.S. 3,063,967). The preferred polymerization catalyst for the invention melt poly-merization process is tin octoate.
The catalyst is present in the polymerization reaction mixture in an amount within the range of 0.0001 to 3, preferably 0.007 to 0.08 weight percent, based on the weight of the monomer. The polymerization reaction can be carried out at a pressure generally within the range of 5 to 500 kPa (0.05 to 5 atmospheres), preferably 50 to 200 kPa (0.5 to 2 atm.). The polymerization reaction temperature is a temperature higher than the melting temperature of the target polymer. For poly-p-dioxanone, the polymerization temperature will range from 110 to 175 ~C, preferably 120 to 150 ~C. The poly-merization reaction is preferably carried out in a stirred reactor vessel under an inert or reducing atmosphere such as nitrogen, argon or hydrogen. The polymerization can be carried out continuously or batchwise, in a single vessel or a series of two or more reactors. Reaction time can vary depending upon catalyst concentration, temperature, pressure and other reaction variables, but will generally range within 0.5 to 5 hours.
CA 02263~78 1999-02-17 WO 98/08887 PCT~EP97/04730 When the desired degree of polymerization has been achieved, as determined by product number average molecular weight of at least about 20,000 or by the corresponding viscosity, for example, a cyclic anhydride is added to the reaction product mixture in an amount sufficient to react with a majority of the polymer endgroups. The cyclic anhydride will generally be added in an amount of 2 mole percent or less, preferably within the range of 0.0001 to 0.1 mole percent, based on the original amount of p-dioxanone monomers.
As used herein, "cyclic anhydride" refers to a compound having the chemical moiety O O
-C-O-C- joined to an aliphatic or aromatic ring. Such compounds include pyromellitic anhydride, phthalic anhydride, maleic anhydride, diglycolic anhydride and itaconic anhydride. The currently preferred cyclic anhydride is pyromellitic anhydride.
After addition of the cyclic anhydride, the reaction product mixture is maintained under conditions suitable for the cyclic anhydride to react with the majority of the polymer endgroups present, generally a temperature within the range of 60 to 150 ~C for a time of 0.5 to 3 hours. The reaction product mixture is then exposed to reduced pressure, preferably 47 to 0.0001 kPa (350 to 0.001 torr) and a temperature within the range of 110 to 160 ~C for a time sufficient to remove p-dioxanone mono-mer, generally 1 to 5 hours.
The end-capped poly-p-dioxanone is removed from the polymerization vessel and formed into particles such as nibs, chips, pellets and the like. Preferably, this process is carried out by pumping the molten mixture from the reactor into a screw extruder, and extruding, CA 02263~78 1999-02-17 cooling, solidifying and then dividing the mixture into solid particles.
The poly-p-dioxanone preparation process can be described by reference to the Figure. Shown is a con-tinuous process in which two polymerization reactors are operated in series. P-dioxanone monomer, with any desired comonomer, and the polymerization catalyst in optional solvent are introduced into stirred reactor vessel 3 via conduits 1 and 2, respectively. The contents of the reactor are heated above the melting temperature of the desired polymer or copolymer to a monomer conversion of 25 to 50 mole percent.
The molten reaction product mixture containing poly-p-dioxanone, unreacted p-dioxanone and catalyst is transferred via conduit 4 to a second stirred reactor 5, wherein polymerization is continued in the melt to greater conversion and higher molecular weight. The poly-p-dioxanone is reacted with cyclic anhydride introduced via conduit 6 to produce an end-capped poly-p-dioxanone.
The molten reaction product mixture 7 containing end-capped poly-p-dioxanone, up to about 30 weight percent p-dioxanone and catalyst residue is cooled and passed to vessel 8 wherein volatiles including unreacted p-dioxa-none are removed by, for example, evaporation or distillation under reduced pressure. Unreacted monomer may be recycled via conduit 9 to the initial poly-merization reactor. End-capped polymer may be passed via conduit 10 to extruder 11 for cooling and formation into pellets.
The molecular weight average of the product poly-p-dioxanone will depend upon the desired application but will typically range from 50,000 to 300,000.
CA 02263~78 1999-02-17 W O 98/08887 PCT~EP97/04730 The polymerization can be carried out in batch or continuous form.
The poly-p-dioxanone polymer prepared in the inven-tion process can be used in coatings, films, moulding powders and fibres, particularly where degradability or biodegradability is desired.
Example 1 Polymerization of Poly-p-Dioxanone This experiment demonstrates the problem of polymer degradation in the melt polymerization of poly-p-dio-xanone.
A standard polymerization kettle was charged with 50.06 g of p-dioxanone monomer and 0.15 ml of 0.33 M tin octoate in toluene. The mixture was heated to 125 ~C for 5 hours and sampled for molecular weight determination.
The number average molecular weight at this stage of the polymerization was 4~,000.
The temperature was reduced to 110 ~C and vacuum was applied for 1.5 hour to remove unreacted monomer. The polymer was then removed from the reactor and analyzed by GPC (PMMA standard in HFIPA solvent). The number average molecular weight of the polymer at this stage was 30,200, which was 31% less than the molecular weight of the polymer after melt polymerization, suggesting degradation of the polymer as a result of a shift in chemical equi-librium as the monomer was removed from the polymer/mono-mer mixture.
Example 2 Polymerization of p-Dioxanone A standard polymerization kettle was charged with 50.06 g of p-dioxanone monomer, 0.0005 mole dodecanol ~as a catalyst initiator) and 0.15 ml of 0.33 M tin octoate solution in toluene. The mixture was heated to 125 ~C for CA 02263~78 1999-02-17 W 098/08887 PCT~EP97/04730 3 hours, and a sample was taken from molecular weight determination. GPC analysis (PMMA standard in HFIPA
solvent) gave a number average molecular weight of 28,100. The temperature was then reduced to 115 ~C and vacuum was applied for 2.5 hour to remove unreacted monomer. GPC analysis of the polymer showed a number average molecular weight of 10,000, indicating a signi-ficant loss of molecular weight under the vacuum.
Example 3 Preparation of End-Capped Poly-p-Dioxanone A polymerization kettle was charged with 120.5 g of p-dioxanone monomer. A 0.55 ml aliquot of 0.2 M tin octoate solution in toluene was injected into the reactor at 60 ~C, and the temperature was raised to 125 ~C. After 3 hours of stirring, the melt was thick and viscous. A
sample of the melt was taken for H NMR and GPC analyses, which indicated 75% conversion of monomer to polymer with a number average molecular weight of 75,900.
7.6 ml of 0.16 M pyromellitic anhydride in THF was then added and the melt was stirred for 1 hour. Vacuum was then applied and the melt was maintained at 125 ~C
for 5 hours under vacuum. The product was analyzed by GPC. The anhydride-capped polymer contained less than 2.7% monomer and had a number average molecular weight of 78,600.
Example 4 Preparation of End-Capped Poly-p-Dioxanone The procedure of Example 3 was repeated with the exception that the vacuum was applied to the melt at 125 ~C for a period of 2.5 hours. Before endcapping, the melt contained 67% polymer and 33~ p-dioxanone monomer.
The number average molecular weight of the polymer was 81,000. After vacuum removal of the monomer from the W O 98/08887 PCT~P97/04730 melt, the poly-p-dioxanone contained less than 2% monomer and had a number average molecular weight of 90,000.
This invention relates to the preparation of poly-p-dioxanone. In a specific aspect, the invention relates to the preparation of high molecular weight poly-p-dioxanone in the melt.
p-Dioxanone is known to be readily polymerized in the solid state below the melting point (about 110 ~C) of the polymer. With active polymerization catalysts such as aluminium and zinc complexes, high molecular weight polymer can be obtained with conversions of p-dioxanone monomer to polymer approaching 100%.
To permit commercial scale-up of the polymerization without adversely affecting process economics, it would be desirable to carry out the polymerization reaction in the melt rather than in the solid state. However, as a result of the dynamic chemical equilibrium between p-dioxanone and poly-p-dioxanone above the melting point of the polymer, conversion of monomer to polymer in the melt ~s typically limlted to about 78%. Removal and recovery of unreacted monomer from the melt is difficult because of the tendency, given this dynamic equilibrium, of the polymer to degrade or lose molecular weight as the monomer is removed.
It is therefore an object of the invention to provide a process for preparing high molecular weight poly-p-dioxanone in the melt.
According to the invention, poly-p-dioxanone is prepared in a process comprising:
CA 02263~78 1999-02-17 W O 98/08887 PCT~P97/04730 (a) heating a reaction mixture comprising p-dioxanone and an effective amount of a polymerization catalyst under conditions of temperature and pressure effective to produce a reaction product mixture comprising molten poly-p-dioxanone and unreacted p-dioxanone;
(b) adding to said reaction product mixture a cyclic anhydride under conditions effective to produce an end-capped poly-p-dioxanone;
(c) maintaining the reaction product mixture comprising end-capped poly-p-dioxanone under reduced pressure at a temperature within the range of 50 to 150 ~C for a time effective for removal of a major portion of the unreacted p-dioxanone from the reaction product mixture; and (d) recovering said end-capped poly-p-dioxanone.
The invention process permits the production of high molecular weight poly-p-dioxanone in the melt.
The starting monomer for preparation of the desired high molecular weight poly-p-dioxanone is an optionally alkyl-substituted 2-p-dioxanone according to the formula O ~OXR2 Rl ~ 0 H
in which each of R1 and R2 can be H or C1_3 alkyl. The monomer can be prepared, for example, by the oxidative dehydrogenation of dialkylene glycols such as diethylene glycol. To prepare high molecular weight polymer, it is desirable to use monomer of a purity of at least about 98%. Such purity can generally be achieved by distilla-tion.
If desired for modification of polymer properties, other cyclic lactones, e.g., such as lactide and glycolide can be copolymerized with the p-dioxanone. As CA 02263~78 1999-02-17 used herein, "poly-p-dioxanone" shall refer to polymers comprising p-dioxanone monomer units and up to about 40 mole percent other cyclic lactone comonomer units.
The polymerization reaction is carried out in the presence of an effective amount of a polymerization catalyst. Suitable polymerization catalysts include, for example, organo tin compounds such as dibutyl tin oxide, dibutyl tin dilaurate and dibutyl tin di-2-ethylhexanoate (U.S. 3, 695,941~, organozinc compounds such as diethyl zinc (U.S. 3,063,968) and organoaluminium compounds such as triisobutyl aluminium (U.S. 3,063,967). The preferred polymerization catalyst for the invention melt poly-merization process is tin octoate.
The catalyst is present in the polymerization reaction mixture in an amount within the range of 0.0001 to 3, preferably 0.007 to 0.08 weight percent, based on the weight of the monomer. The polymerization reaction can be carried out at a pressure generally within the range of 5 to 500 kPa (0.05 to 5 atmospheres), preferably 50 to 200 kPa (0.5 to 2 atm.). The polymerization reaction temperature is a temperature higher than the melting temperature of the target polymer. For poly-p-dioxanone, the polymerization temperature will range from 110 to 175 ~C, preferably 120 to 150 ~C. The poly-merization reaction is preferably carried out in a stirred reactor vessel under an inert or reducing atmosphere such as nitrogen, argon or hydrogen. The polymerization can be carried out continuously or batchwise, in a single vessel or a series of two or more reactors. Reaction time can vary depending upon catalyst concentration, temperature, pressure and other reaction variables, but will generally range within 0.5 to 5 hours.
CA 02263~78 1999-02-17 WO 98/08887 PCT~EP97/04730 When the desired degree of polymerization has been achieved, as determined by product number average molecular weight of at least about 20,000 or by the corresponding viscosity, for example, a cyclic anhydride is added to the reaction product mixture in an amount sufficient to react with a majority of the polymer endgroups. The cyclic anhydride will generally be added in an amount of 2 mole percent or less, preferably within the range of 0.0001 to 0.1 mole percent, based on the original amount of p-dioxanone monomers.
As used herein, "cyclic anhydride" refers to a compound having the chemical moiety O O
-C-O-C- joined to an aliphatic or aromatic ring. Such compounds include pyromellitic anhydride, phthalic anhydride, maleic anhydride, diglycolic anhydride and itaconic anhydride. The currently preferred cyclic anhydride is pyromellitic anhydride.
After addition of the cyclic anhydride, the reaction product mixture is maintained under conditions suitable for the cyclic anhydride to react with the majority of the polymer endgroups present, generally a temperature within the range of 60 to 150 ~C for a time of 0.5 to 3 hours. The reaction product mixture is then exposed to reduced pressure, preferably 47 to 0.0001 kPa (350 to 0.001 torr) and a temperature within the range of 110 to 160 ~C for a time sufficient to remove p-dioxanone mono-mer, generally 1 to 5 hours.
The end-capped poly-p-dioxanone is removed from the polymerization vessel and formed into particles such as nibs, chips, pellets and the like. Preferably, this process is carried out by pumping the molten mixture from the reactor into a screw extruder, and extruding, CA 02263~78 1999-02-17 cooling, solidifying and then dividing the mixture into solid particles.
The poly-p-dioxanone preparation process can be described by reference to the Figure. Shown is a con-tinuous process in which two polymerization reactors are operated in series. P-dioxanone monomer, with any desired comonomer, and the polymerization catalyst in optional solvent are introduced into stirred reactor vessel 3 via conduits 1 and 2, respectively. The contents of the reactor are heated above the melting temperature of the desired polymer or copolymer to a monomer conversion of 25 to 50 mole percent.
The molten reaction product mixture containing poly-p-dioxanone, unreacted p-dioxanone and catalyst is transferred via conduit 4 to a second stirred reactor 5, wherein polymerization is continued in the melt to greater conversion and higher molecular weight. The poly-p-dioxanone is reacted with cyclic anhydride introduced via conduit 6 to produce an end-capped poly-p-dioxanone.
The molten reaction product mixture 7 containing end-capped poly-p-dioxanone, up to about 30 weight percent p-dioxanone and catalyst residue is cooled and passed to vessel 8 wherein volatiles including unreacted p-dioxa-none are removed by, for example, evaporation or distillation under reduced pressure. Unreacted monomer may be recycled via conduit 9 to the initial poly-merization reactor. End-capped polymer may be passed via conduit 10 to extruder 11 for cooling and formation into pellets.
The molecular weight average of the product poly-p-dioxanone will depend upon the desired application but will typically range from 50,000 to 300,000.
CA 02263~78 1999-02-17 W O 98/08887 PCT~EP97/04730 The polymerization can be carried out in batch or continuous form.
The poly-p-dioxanone polymer prepared in the inven-tion process can be used in coatings, films, moulding powders and fibres, particularly where degradability or biodegradability is desired.
Example 1 Polymerization of Poly-p-Dioxanone This experiment demonstrates the problem of polymer degradation in the melt polymerization of poly-p-dio-xanone.
A standard polymerization kettle was charged with 50.06 g of p-dioxanone monomer and 0.15 ml of 0.33 M tin octoate in toluene. The mixture was heated to 125 ~C for 5 hours and sampled for molecular weight determination.
The number average molecular weight at this stage of the polymerization was 4~,000.
The temperature was reduced to 110 ~C and vacuum was applied for 1.5 hour to remove unreacted monomer. The polymer was then removed from the reactor and analyzed by GPC (PMMA standard in HFIPA solvent). The number average molecular weight of the polymer at this stage was 30,200, which was 31% less than the molecular weight of the polymer after melt polymerization, suggesting degradation of the polymer as a result of a shift in chemical equi-librium as the monomer was removed from the polymer/mono-mer mixture.
Example 2 Polymerization of p-Dioxanone A standard polymerization kettle was charged with 50.06 g of p-dioxanone monomer, 0.0005 mole dodecanol ~as a catalyst initiator) and 0.15 ml of 0.33 M tin octoate solution in toluene. The mixture was heated to 125 ~C for CA 02263~78 1999-02-17 W 098/08887 PCT~EP97/04730 3 hours, and a sample was taken from molecular weight determination. GPC analysis (PMMA standard in HFIPA
solvent) gave a number average molecular weight of 28,100. The temperature was then reduced to 115 ~C and vacuum was applied for 2.5 hour to remove unreacted monomer. GPC analysis of the polymer showed a number average molecular weight of 10,000, indicating a signi-ficant loss of molecular weight under the vacuum.
Example 3 Preparation of End-Capped Poly-p-Dioxanone A polymerization kettle was charged with 120.5 g of p-dioxanone monomer. A 0.55 ml aliquot of 0.2 M tin octoate solution in toluene was injected into the reactor at 60 ~C, and the temperature was raised to 125 ~C. After 3 hours of stirring, the melt was thick and viscous. A
sample of the melt was taken for H NMR and GPC analyses, which indicated 75% conversion of monomer to polymer with a number average molecular weight of 75,900.
7.6 ml of 0.16 M pyromellitic anhydride in THF was then added and the melt was stirred for 1 hour. Vacuum was then applied and the melt was maintained at 125 ~C
for 5 hours under vacuum. The product was analyzed by GPC. The anhydride-capped polymer contained less than 2.7% monomer and had a number average molecular weight of 78,600.
Example 4 Preparation of End-Capped Poly-p-Dioxanone The procedure of Example 3 was repeated with the exception that the vacuum was applied to the melt at 125 ~C for a period of 2.5 hours. Before endcapping, the melt contained 67% polymer and 33~ p-dioxanone monomer.
The number average molecular weight of the polymer was 81,000. After vacuum removal of the monomer from the W O 98/08887 PCT~P97/04730 melt, the poly-p-dioxanone contained less than 2% monomer and had a number average molecular weight of 90,000.
Claims (10)
1. A process for melt polymerization of p-dioxanone, the process comprising:
(a) heating a reaction mixture comprising p-dioxanone and an effective amount of a polymerization catalyst under conditions of temperature and pressure effective to produce a reaction product mixture comprising molten poly-p-dioxanone and unreacted p-dioxanone;
(b) adding a cyclic anhydride to said reaction product mixture under conditions effective for reaction of the poly-p-dioxanone with the cyclic anhydride to form an end-capped poly-p-dioxanone;
(c) exposing the reaction product mixture to a temperature within the range of about 50 to about 150 °C
under less than atmospheric pressure and removing unreacted p-dioxanone from the reactlon product mixture;
and (d) recovering the end-capped poly-p-dioxanone.
(a) heating a reaction mixture comprising p-dioxanone and an effective amount of a polymerization catalyst under conditions of temperature and pressure effective to produce a reaction product mixture comprising molten poly-p-dioxanone and unreacted p-dioxanone;
(b) adding a cyclic anhydride to said reaction product mixture under conditions effective for reaction of the poly-p-dioxanone with the cyclic anhydride to form an end-capped poly-p-dioxanone;
(c) exposing the reaction product mixture to a temperature within the range of about 50 to about 150 °C
under less than atmospheric pressure and removing unreacted p-dioxanone from the reactlon product mixture;
and (d) recovering the end-capped poly-p-dioxanone.
2. The process of claim 1 in which the cyclic anhydride is selected from the group consisting of cycloaliphatic anhydrides and aromatic anhydrides.
3. The process of claim 1 in which the cyclic anhydride is pyromellitic anhydride.
4. The process of claim 1 in which the cyclic anhydride is added to the reaction product mixture in an amount within the range of 0.0001 to 2 mole percent, based on p-dioxanone.
5. The process of claim 1 in which step (a) is carried out at a temperature greater than 110 °C.
6. The process of claim 1 in which step (a) is carried out at a pressure within the range of 5 to 500 kPa.
7. The process of claim 1 in which the polymerization catalyst comprises at least one of a tin compound, a zinc compound and an aluminium compound.
8. The process of claim 1 in which the molecular weight of the poly-p-dioxanone is within the range of 50,000 to 300,000.
9. The process of claim 1 in which the poly-p-dioxanone is a copolymer of p-dioxanone and a second cyclic lactone.
10. The process of claim 1 which further comprises recycling the unreacted p-dioxanone from step (c) to the reaction mixture of step (a).
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US697805 | 1996-08-30 | ||
| US08/697,805 US5652331A (en) | 1996-08-30 | 1996-08-30 | Method for preparing poly-p-dioxanone polymer |
| PCT/EP1997/004730 WO1998008887A1 (en) | 1996-08-30 | 1997-08-29 | Method for preparing poly-p-dioxanone polymer |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2263578A1 true CA2263578A1 (en) | 1998-03-05 |
Family
ID=24802621
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002263578A Abandoned CA2263578A1 (en) | 1996-08-30 | 1997-08-29 | Method for preparing poly-p-dioxanone polymer |
Country Status (8)
| Country | Link |
|---|---|
| US (1) | US5652331A (en) |
| EP (1) | EP0923614A1 (en) |
| JP (1) | JP3194587B2 (en) |
| KR (1) | KR100356763B1 (en) |
| AU (1) | AU4619697A (en) |
| BR (1) | BR9711242A (en) |
| CA (1) | CA2263578A1 (en) |
| WO (1) | WO1998008887A1 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BRPI0514166A (en) | 2004-08-09 | 2008-06-03 | Univ Michigan State | improved process for forming a poly (1,4-dioxan-2-one) copolymer with a cyclic ester monomer, process for forming a poly (1,4-dioxan-2-one) copolymer and a cyclic ester, process for forming a poly (1,4-dioxan-2-one) copolymer and a cyclic ester mixed with additional ingredients, anhydrous poly (1,4-dioxan-2-one) copolymer, and a copolymer of poly (1,4-dioxan-2-one) with a cyclic ester monomer |
| CN109111566A (en) * | 2018-08-24 | 2019-01-01 | 南京普立蒙医疗科技有限公司 | A kind of preparation method of high-purity polydioxanone |
| US11028222B2 (en) | 2018-11-28 | 2021-06-08 | Ethicon, Inc. | Advanced processing of absorbable poly(p-dioxanone) containing high level of p-dioxanone monomer |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3115475A (en) * | 1958-02-18 | 1963-12-24 | Process for theproduction of | |
| US3063967A (en) * | 1959-10-07 | 1962-11-13 | Gen Aniline & Film Corp | Polymers of 2-p-dioxanone and method for making same |
| US3645941A (en) * | 1970-04-01 | 1972-02-29 | Eastman Kodak Co | Method of preparing 2-p-dioxanone polymers |
| US4643191A (en) * | 1985-11-29 | 1987-02-17 | Ethicon, Inc. | Crystalline copolymers of p-dioxanone and lactide and surgical devices made therefrom |
| US4653497A (en) * | 1985-11-29 | 1987-03-31 | Ethicon, Inc. | Crystalline p-dioxanone/glycolide copolymers and surgical devices made therefrom |
| US5321113A (en) * | 1993-05-14 | 1994-06-14 | Ethicon, Inc. | Copolymers of an aromatic anhydride and aliphatic ester |
| US5770683A (en) * | 1994-11-02 | 1998-06-23 | Mitsui Toatsu Chemicals, Inc. | Preparation process of polyhydroxycarboxylic acid |
-
1996
- 1996-08-30 US US08/697,805 patent/US5652331A/en not_active Expired - Fee Related
-
1997
- 1997-08-29 KR KR1019997001464A patent/KR100356763B1/en not_active IP Right Cessation
- 1997-08-29 BR BR9711242-9A patent/BR9711242A/en not_active Application Discontinuation
- 1997-08-29 CA CA002263578A patent/CA2263578A1/en not_active Abandoned
- 1997-08-29 AU AU46196/97A patent/AU4619697A/en not_active Abandoned
- 1997-08-29 WO PCT/EP1997/004730 patent/WO1998008887A1/en not_active Application Discontinuation
- 1997-08-29 JP JP51129898A patent/JP3194587B2/en not_active Expired - Fee Related
- 1997-08-29 EP EP97944815A patent/EP0923614A1/en not_active Withdrawn
Also Published As
| Publication number | Publication date |
|---|---|
| JP2000516979A (en) | 2000-12-19 |
| BR9711242A (en) | 2000-08-08 |
| AU4619697A (en) | 1998-03-19 |
| US5652331A (en) | 1997-07-29 |
| KR20000035816A (en) | 2000-06-26 |
| EP0923614A1 (en) | 1999-06-23 |
| WO1998008887A1 (en) | 1998-03-05 |
| JP3194587B2 (en) | 2001-07-30 |
| KR100356763B1 (en) | 2002-10-18 |
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| Date | Code | Title | Description |
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| EEER | Examination request | ||
| FZDE | Discontinued |