WO2001019891A1 - Procede de production de poly(p-dioxanone), et monofilament de poly(p-dioxanone) et son procede de production - Google Patents
Procede de production de poly(p-dioxanone), et monofilament de poly(p-dioxanone) et son procede de production Download PDFInfo
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- WO2001019891A1 WO2001019891A1 PCT/JP2000/006223 JP0006223W WO0119891A1 WO 2001019891 A1 WO2001019891 A1 WO 2001019891A1 JP 0006223 W JP0006223 W JP 0006223W WO 0119891 A1 WO0119891 A1 WO 0119891A1
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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
- C08G63/78—Preparation processes
- C08G63/82—Preparation processes characterised by the catalyst used
- C08G63/823—Preparation processes characterised by the catalyst used for the preparation of polylactones or polylactides
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- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
- D01F6/00—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof
- D01F6/58—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolycondensation products
- D01F6/62—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolycondensation products from polyesters
- D01F6/625—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolycondensation products from polyesters derived from hydroxy-carboxylic acids, e.g. lactones
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
- Y10T428/00—Stock material or miscellaneous articles
- Y10T428/29—Coated or structually defined flake, particle, cell, strand, strand portion, rod, filament, macroscopic fiber or mass thereof
- Y10T428/2913—Rod, strand, filament or fiber
Definitions
- the present invention relates to a method for producing poly (p-dioxanone), a poly (p-dioxanone) monofilament, and a method for producing the same. More specifically, poly (p-dioxanone) monofilament which has a high retention of mechanical properties and is suitably used as a surgical suture, a method for producing the same, and poly (p-dioxanone) which can be suitably used as a raw material of the monofilament ).
- PDS II (trade name) manufactured by Ethicon Corporation of the United States, and it is known that it exhibits extremely excellent hydrolysis resistance.
- Monocryl (trade name, manufactured by Ethicon), Maxon (trade name, manufactured by ACC), Biocin (trade name, manufactured by U.S. Surgical) and the like are known. ing.
- the latter monofilaments hydrolyze faster than PDS II, are longer and less effective in retaining hydrolysis resistance, and are used only for short-term applications. When longer hydrolyzability was required, it was necessary to use poly-prolactone monofilament or the like. However, in practice, heat resistance is insufficient, and the water content is too slow.
- the molecular weight is controlled by the amount of the organometallic catalyst and the purity of the monomer, so that the suture with a solution viscosity of tetrachlorethane solution of at least 0.5 d 1 / g or more Is described.
- the higher the molecular weight the greater the amount of catalyst contained, and even if the used catalyst is removed, it is not a good method in terms of safety.
- the molecular weight of the latter poly (p-dioxanone) is controlled by the amount of tin dioctanoate, which is far from the catalyst amount intended by the present inventors. Also, even if the used catalyst is removed, it is not a good method in terms of safety.
- Japanese Patent Application Laid-Open No. 8-52205 discloses a method for producing poly (p-dioxanone) having a high solution viscosity, and a solution of 2.3 to 8.0 dI in 7 g of hexafluoroisopropanol solvent. Surgical monofilaments having a viscosity are disclosed.
- the publication further discloses that poly (p-dioxanone) is produced by one-stage polymerization using a reactor suitable for a polymer exhibiting high viscosity, or two-stage polymerization in which low-molecular-weight prepolymer is polymerized in a two-stage solid state. It states that it can be manufactured.
- an object of the present invention is to provide a poly (p-dioxanone) which is more excellent in water resistance to decomposing water and is safer than a conventionally known poly (p-dioxanone) filament such as PDS II. It is an object of the present invention to provide a monofilament of the present invention and a method for producing the same, and a method for producing poly (p-dioxanone) useful as a raw material thereof. Disclosure of the invention
- stannous dioctanoate which was conventionally believed to be a liquid, forms a solid at a low temperature when purified by distillation or the like.
- stannous dioctanoate which was conventionally believed to be a liquid, forms a solid at a low temperature when purified by distillation or the like.
- liquid-phase ring-opening polymerization of p-dioxanone is started, and the polymerization proceeds, and the viscosity (stirring load) of the reaction system is specified.
- the stirring was stopped, the polymerization temperature was lowered, and the method was switched to solid-state polymerization.
- the resulting poly (p-dioxanone) was compared with the case where unpurified stannous dioctanoate was used. Despite having the same molecular weight of), the inventors have found that the filament strength and hydrolysis resistance obtained by spinning it are excellent, and have arrived at the present invention.
- the first invention of the present invention is a method for producing poly (p-dioxanone) in which ring-opening polymerization of p-dioxanone is carried out in the presence of a catalyst and an initiator.
- Just And start the liquid-phase ring-opening polymerization of p-dioxanone stop stirring when the stirring load increases by 10 to 100% of the initial load, and raise the polymerization temperature to 65 to 85 ° C.
- This is a method for producing poly (p-dioxanone), characterized by performing solid-state polymerization at a reduced temperature.
- an unreacted p-dioxanone is removed by passing an inert gas at a temperature of 60 to 80 ° C. and a pressure of 1 OmmHg or less to reduce the content thereof. 0.5% by weight or less of the above production method, and the conversion to poly (p-dioxanone) is 95% by weight. /.
- the above-described production method in which the polymerization reaction is continued until the above is reached is exemplified. In any of the production methods, it is preferable to use p-dioxanone having a water content of 150 ppm or less as a raw material.
- stannous dioctanoate should have a melting point of 3 ° C or more.Furthermore, commercially available products should be purified by distillation to obtain 0.25 to 0.3 mmHg and a top temperature of 180 to It is preferable to use a distillate under the condition of 200 ° C. It is preferable to stop stirring when the stirring load increases by 20 to 80% of the initial load.
- the intrinsic viscosity of the poly (p-dioxanone) produced by the above method can be changed by adjusting the amount of the initiator, and specifically, at 25 ° C, 1.8 to 2.5. d1 / g.
- the melting point of tin dioctanoate in the present invention can be measured by the method described in Examples described later.
- the second invention of the present invention provides a method for producing poly (p-dioxanone) by the above method, and then (1) a spinning step of melt-spinning the obtained poly (p-dioxanone) at 125 to 165 ° C. (2) a stretching step of stretching at a stretching ratio of 3 to 8 at 60 to 110 ° C, (3) a step of relaxing 80 to 90% at 60 to 110 ° C, (4) 80 to 100
- a method of producing a poly (p-dioxanone) monofilament which comprises a step of performing a heat treatment at 1 ° C. for 1 to 24 hours.
- the diameter of the drawn monofilament produced by this method is 4 to 40 mils.
- a third invention of the present invention is a poly (p-dioxanone) monofilament produced according to the second invention, which has a single knot tensile strength of at least 30,000 psi and is immersed in a physiological saline solution at 37 ° C for 4 weeks. Retention rate of the tensile strength after Above is the poly (p-dioxanone) monofilament.
- the monofilament according to the present invention is suitably used as a surgical suture.
- the poly (p-dioxanone) monofilament according to the present invention has a lower hydrolysis rate than known hydrolyzable polyester filaments, for example, PDSII.
- PDSII hydrolyzable polyester filaments
- it even when subjected to hydrolysis treatment in physiological saline, it has a high retention rate such as single knot tensile strength and is excellent in hydrolysis resistance. Therefore, it is a very useful material that can be used as a surgical suture for a long healing period.
- stannous dioctanoate is used as a catalyst.
- Stannous dioctanoate has been approved by the US FDA as a food additive.
- the stannous dioctanoate used in the present invention produces white crystals at 0 ° C.
- the melting point is 3 ° C or higher.
- These catalysts can be obtained by purifying a commercial product by distillation and the like. Examples of commercially available products include Nitka Octic Tin 28%, manufactured by Nippon Chemical Industry Co., Ltd. The product is a pale yellow liquid at a temperature of 0 ° C.
- This commercial product was purified by distillation, and the distillate at a pressure of 0.25 to 0.3 mmHg and an overhead temperature of 180 to 200 ° C was collected to meet the object of the present invention.
- a catalyst having a purity is obtained.
- the recovery of the distillate is about 80% by weight.
- distillates with a top temperature of less than 180 ° C are removed as initial fractions, and those with a temperature of more than 200 ° C are removed as bottoms.
- Stannous dioctanoate purified by distillation is a colorless and viscous liquid at room temperature, and furthermore, a nitrogen atmosphere Below, it is a white crystal at 0 ° C with a melting point of 13 ° C. Furthermore,-From NMR and IR measurement results, most of the first distillate is a free carboxylic acid.
- the amount of the catalyst used is preferably in the range of 0.002 to 0.005 mol% based on the charged amount of p-dioxanone.
- the initiator examples include the following. Examples thereof include aliphatic alcohols, daricols, hydroxycarboxylic acids, and phenols. Specifically, aliphatic saturated alcohols such as methanol, ethanol, propanol, butanol, amyl alcohol, caprylic alcohol, and lauryl alcohol; alicyclic alcohols such as cyclopentanol and cyclohexanol; diethylene dalicol; And carboxylic acids such as lactic acid and glycolic acid, and phenols such as aminophenol and acetoaminophen. Of these, laurinole alcohol is preferably used.
- the amount of the initiator used is preferably in the range of 0.01 to 0.1 mol% based on the amount of p-dioxanone described below.
- the p-dioxanone (monomer) used in the present invention may be distilled or purified by distillation, but preferably has low water content.
- the allowable range of water is desirably 150 ppm or less. When the water content exceeds 150 ppm, generation of a polymer using water as an initiator becomes dominant, and a large amount of poly (p-dioxanone) having a high hydrolysis rate tends to be generated.
- a dye may be added to the polymerization system.
- the time of addition is preferably at the start of polymerization.
- Dyes that can be used include D & C, Green—No. 6 (CAS No. 1 28—80—3), and D & C, Vio 1 et-No. 2 (CAS No. : 81-48- 1).
- the amount of dye used is 0.21 weight for the former, based on the amount of monomer charged. / 0 below, the latter Shi preferred range of less than 0.3 wt% Re. More preferably, the former is less than 0.15% by weight, and the latter is 25% by weight. / 0 range.
- a polymer and a filler having excellent hydrolysis resistance without adding a dye are used.
- ring-opening polymerization of p-dioxanone is carried out in the presence of the catalyst and the initiator and, if necessary, with the addition of a dye.
- the reaction is started in the liquid phase at 85 to 105 ° C, preferably 90 to 100 ° C, with stirring.
- the polymerization reaction proceeds, and as the production of the polymer proceeds, the viscosity of the reaction system increases. In the present invention, this increase in viscosity is captured by an increase in the stirring load.
- the stirring load will be described as an example.
- Stirring was started at a stirring load of 0.006 V at the start of the reaction (maximum load of the stirrer: 5 V, torque at that time: 10 kgf ⁇ cm), and the stirring load was 0.008 V, for example.
- the point at which viscosity exceeds is defined as the point at which viscosity occurs, that is, the point at which the stirring load increases.
- the load increase at this time is 0.002 V, which is 33% higher than the initial load.
- the polymerization temperature at this time is 85 to 105 ° C. Preferably it is in the range of 90 to 100 ° C.
- the ring-opening polymerization is started, and after the viscosity is generated and the stirring load increases by a specific value, the stirring is stopped. At the same time, the polymerization temperature is lowered to switch to solid-state polymerization.
- the target of the degree of increase in the stirring load when switching to solid-state polymerization is at the time when the stirring load is increased by 10 to 100% with respect to the initial stirring load. Preferably, it is the point of time when it increases by 20 to 80%.
- the polymerization temperature for solid-phase polymerization is 65 to 85 ° C. It is preferably in the range of 70 to 80 ° C.
- the monomer conversion rate was 95% by weight. It is preferable to continue until it reaches the maximum.
- the polymerization time varies depending on the temperature, the amount of the catalyst, and the amount of the initiator. Usually, the reaction time of the liquid phase reaction under stirring is preferably about 2 to 24 hours. More preferably, it is about 6 to 12 hours. During this time, workability is greatly improved by incorporating a control system that automatically detects the increase in the stirring load due to the occurrence of viscosity, automatically stops stirring, and automatically switches to solid state polymerization. Can be. Solid state polymerization The polymerization time is preferably about 3 to 6 days.
- the poly (p-dioxanone) polymer is spun to obtain the desired properties. It becomes difficult to obtain a monofilament having the same.
- the heating medium is not limited, and may be an oil bath or a dryer. However, a dryer is preferable in consideration of an efficient method.
- the intrinsic viscosity of poly (p-dioxanone) produced by the above method is 1.8 to 2.5 d 1 / g at 25 ° C. Preferably it is in the range of about 1.9 to 2.4 dl / g.
- melt viscosity during molding will be low, and it will be difficult to obtain a filament having a good shape.
- melt viscosity will be too high during molding, and it will be difficult to obtain good moldability.
- the purity of the catalyst compared to the case where the commercially available product is used without purification, the purity of the monomer can be improved even if the molar ratio of the monomer to the initiator (hereinafter referred to as M / I) is the same by using the purified catalyst.
- M / I the molar ratio of the monomer to the initiator
- poly (p-dioxanone) having a high intrinsic viscosity, that is, a high molecular weight is obtained (comparison between Examples 1 and 2 and Comparative Example 1 or Comparative Example 4 and Comparative Example 2).
- the filament obtained by spinning the poly (p-dioxanone) obtained using the purified catalyst is more specific to the poly (p-dioxanone) than when the commercial product is used without purification.
- stirring load control when the M / I is the same and the distillation purified catalyst is used, stirring is stopped when the stirring load increases to a predetermined value, and the polymerization temperature is increased to a predetermined value.
- the polymerization is carried out at a lower temperature, a higher molecular weight poly (p-dioxanone) having a higher intrinsic viscosity can be obtained (comparison between Examples 1 to 3 and Comparative Examples 3 and 4).
- the control of the molecular weight is uniquely determined by the addition amount of the initiator and the like.
- the initiator and the like mean water and an initiator. Open all moles of monomer The MZ I value divided by the number of moles of the initiator is used as the index. After measuring the water content of the monomer, determine the amount of initiator to be added from the calibration curve created in advance.
- Poly (p-dioxanone) is preferably one from which impurities are removed as much as possible. That is, it is preferable to minimize substances that promote hydrolysis, such as water and monomers.
- the content of the monomer in poly (p-dioxanone) is preferably 0.5% by weight or less, more preferably 0.1% or less.
- any method can be used as long as the heating medium can be passed through and the filled container can be heated under reduced pressure.
- stripping may be performed by using a rotary conical dryer that heats the container surface and passing heat and dry nitrogen through. If the scale is small, method 1 is effective and convenient. For a scale of 5 kg or more, it is effective to use the method of 2. By these methods, poly (p-dioxanone) from which monomers have been removed can be obtained.
- the heating temperature is in the range of 60 to 80 ° C. It is more preferably in the range of 60 to 70 ° C.
- the flow rate of inert gas such as nitrogen depends on the pumping capacity of the vacuum pump and the size of the container. However, if the flow rate is too large, the degree of vacuum will not increase and the initial target cannot be achieved. Preferably, it is performed at a flow rate of 0.5 liter / min or less. More preferably, it is desirable to carry out at about 0.3 liter Zmin. Depressurization 'The pressure during suction is preferably 1 OmmHg or less.
- the poly (p-dioxanone) thus obtained, from which the monomer has been removed, can be suitably used as a spinning raw material.
- the monofilament according to the present invention is produced by spinning the above-mentioned poly (p-dioxanone), and then drawing it.
- Known spinning methods can be employed for spinning. The same applies to stretching.
- the spinning temperature is preferably from 125 to 165 ° C. 1 25 ° C below this, the melt viscosity of poly (p-dioxanone) is too high and spinning is difficult.
- the temperature exceeds 165 ° C, poly (p-dioxanone) is decomposed, and the strength of the obtained monofilament decreases. It is also possible to prepare a solution of poly (p-dioxanone) and spin the solution.
- a solvent such as tetrachloroethane can be used as the solvent.
- spinning is performed at a temperature equal to or lower than the boiling point of the solvent.
- the solution concentration is usually preferably 10 to 30% by weight. However, from the economic point of view, the former melt spinning method is preferred.
- a monofilament having a linear tensile strength of 500,000 psi or more By producing an undrawn yarn by spinning and stretching the obtained undrawn yarn, a monofilament having a linear tensile strength of 500,000 psi or more can be obtained.
- Preferred stretching conditions are a stretching temperature of 60 to 110 ° C. and a stretching ratio of 3 to 8 times.
- the stretching method is preferably two-stage stretching. In this case, the stretching is performed so that the total stretching ratio of the one-stage stretching and the two-stage stretching is within the above range. If the stretching ratio is less than 3 times, sufficient tensile strength cannot be obtained. On the other hand, when the ratio exceeds 8 times, a whitening phenomenon occurs at the time of stretching, so that sufficient strength cannot be obtained. Further, the monofilament may be broken during the stretching, which is not preferable.
- the monofilament according to the present invention is relaxed by 80 to 90% at 60 to 110 ° C.
- heat treatment is performed.
- the heat treatment temperature is preferably from 80 ° C. to a temperature lower than the melting point of poly (p-dioxanone). Specifically, it is about 80 to 100 ° C.
- the processing time is preferably about 1 to 24 hours. Usually, for example, it is carried out under a moderate tension while wound on a bobbin or the like.
- the monofilament obtained under the above conditions is subjected to a hydrolysis test.
- the monofilament to which the dye is added clearly shows superior hydrolysis resistance as compared with the monofilament (trade name: PDS II) manufactured by Ethicon having the same intrinsic viscosity.
- the monofilament according to the present invention has a linear tensile strength of at least 500,000 psi, preferably at least 600,000 Opsi.
- the single knot tensile strength is at least 30,000 Psi, preferably at least 40,000 psi.
- the Young's modulus is less than 290,000 psi, preferably less than 220,000 psi.
- the elongation is 60% or less, preferably 40% or less.
- the diameter of the monofilament is 4 to 40 mils. 3 After 4 weeks of single knot tensile strength when immersed in physiological saline at 77 ° C Is 58% or more.
- a monofilament having such properties can be suitably used, for example, as a bioabsorbable surgical suture, particularly a wound healing surgical suture having a long healing period.
- HF IP hexafluoroisopropanol
- a tensile tester manufactured by Orientec Co., Ltd., type: Tensilon RTA-100
- the single knot tensile strength is obtained by forming a single knot on the filament, attaching the knot to the center of the clamp, and using it as a sample.
- the Young's modulus is calculated by the following equation from the gradient of the initial linear elastic region of the obtained stress-strain curve.
- the sample was immersed in a physiological saline solution at 37 ° C (a solution prepared by dissolving 9.0 g of sodium chloride in distilled water to a total volume of 1,000 ml) for 7, 14, 21, and 28 days, respectively. Measure the tensile strength once by the method and calculate the retention rate for the unimmersed sample.
- a physiological saline solution at 37 ° C a solution prepared by dissolving 9.0 g of sodium chloride in distilled water to a total volume of 1,000 ml
- Samples 6.8 to 7. Omg are weighed and packaged in an aluminum pan, and allowed to stand in a freezer at -5 ° (: 1 day and night.
- DSC RI GAKU Co., Ltd., type: DS C-8230
- using the a 1 2 0 3 as a standard substance.
- PD ⁇ Distilled and p-dioxanone with a water content of 27.7 ppm (hereinafter referred to as PD ⁇ ) 298.2 g (2.921 mol) was added to both ends of a 30 Om1 reaction flask to prevent water from being further mixed.
- the catalyst was added under a nitrogen atmosphere with a force syringe and 0.004 mole of the purified catalyst was added. /.
- the temperature was further increased to 95 ° C. while stirring at the same rotation speed in a nitrogen atmosphere, and the rotation speed of the stirring was switched to 5 rpm to start polymerization. It took 2 hours to raise the internal temperature from room temperature to 95 ° C.
- the load value of the recorder (Yokogawa Electric, model // R100) at the initial stage of stirring was 0.006V (5 corresponds to a value of 101 ⁇ . .Cm).
- the upper limit of the load due to viscosity was set to 0.008V (33% increase from the initial load), and control was performed so that stirring was stopped when a load exceeding this value was generated.
- the polymerization temperature was controlled by a temperature controller (manufactured by Rikagaku Kogyo Co., Ltd., type: REX-P100) under automatic control in which switching was switched to the next setting pattern when an agitation stop signal was generated.
- a temperature controller manufactured by Rikagaku Kogyo Co., Ltd., type: REX-P100
- the temperature reached 95 ° C
- stirring was stopped 4 hours after the polymerization was started. With the stirring stopped, solid state polymerization was further performed at 80 ° C. for 6 days to complete the polymerization.
- the mixture was quenched with liquid nitrogen, and poly (p-dioxanone) was taken out of the reactor and crushed with a Morita mill (JC-2). It was dried at room temperature for 12 hours with a vacuum dryer to obtain 290 g of a pulverized product.
- the demonomer operation was performed by the following method. Charge the pulverized product into a column with a capacity of 40 ⁇ 1 and heat and maintain the column at a reduced pressure of 8 mmHg at a temperature of 63 ° C. For 36 hours. The content of unreacted monomer after demonomerization is 0.1 weight. / 0 or less.
- the intrinsic viscosity (r?) Of the obtained poly (p-dioxanone) was 2.31 [dlZg].
- the amount of the obtained poly (p-dioxanone) was 280 g.
- the amount of polymer loss in the kettle deposits, grinding and post-treatment was 12.3 g, and the conversion to polymer was 98 weight. /. Met.
- the melting point of the polymer was 115.
- Example 2 The same operation as in Example 1 was performed except that the amounts of PDO, LAOH and the purification catalyst charged, and the water content of PDO were changed as described in Table 1, to obtain poly (p-dioxanone). Obtained. Reproducibility was confirmed.
- Poly (p-dioxanone) was obtained by performing the same operation as in Example 3 except that the charged amounts of PDO, LAOH and the purification catalyst, and the water content of PDO were changed as described in Table 11. .
- Example 1 Example 2 Example 3 Example 3 Example 4 Example 5 Example 6
- the poly (p-dioxanone) obtained in Example 1 was spun at an extrusion temperature of 150 ° C. to produce a monofilament undrawn yarn.
- the extruder had a nozzle diameter of 1.0 mm.
- the obtained undrawn yarn was drawn at a drawing temperature of 90 ° C to a draw ratio of 4.0 times, and further drawn at 110 ° C at a draw ratio of 1.5 times. Further, the obtained drawn yarn was subjected to 90% relaxation at 110 ° C., and then heat-treated at 90 ° C. for 6 hours.
- the linear tensile strength, single knot tensile strength, elongation and Young's modulus of the stretched monofilament after the heat treatment were measured and are shown in Table 13.
- PDSII a commercially available suture thread, manufactured by Ethicon Co., Ltd., a c1ear product containing no dye
- Example 9 Comparing Example 9 with Comparative Examples 9 and 10, the intrinsic viscosity is almost the same, that is, although the molecular weight of the polymer is hardly changed, the resistance of the filament of Example 9 to hydrolytic decomposition is improved. You can see that.
- the monofilament produced by spinning and drawing using the poly (p-dioxanone) obtained by the production method according to the present invention has a slower hydrolysis than the existing poly (p-dioxanone) monofilament, and has a healing period. Has long-term wound repair surgery Excellent as a yarn. Therefore, poly (p-dioxanone) obtained by the production method of the present invention is a very useful material as a bioabsorbable surgical suture in the form of a monofilament.
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- General Chemical & Material Sciences (AREA)
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Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP00957116A EP1136511B1 (en) | 1999-09-13 | 2000-09-12 | PROCESS FOR PRODUCING POLY(p-DIOXANONE), AND POLY(p-DIOXANONE) MONOFILAMENT AND PROCESS FOR PRODUCING THE SAME |
US09/830,988 US6448367B1 (en) | 1999-09-13 | 2000-09-12 | Method of producing poly(p-dioxanone), poly (p-dioxanone) monofilaments and method for producing the same |
DE60034765T DE60034765T2 (de) | 1999-09-13 | 2000-09-12 | Verfahren zur herstellung von poly(p-dioxanon), und poly(p-dioxanon)-monofilament und verfahren zur herstellung desselben |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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JP25826299 | 1999-09-13 | ||
JP11/258262 | 1999-09-13 |
Publications (1)
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WO2001019891A1 true WO2001019891A1 (fr) | 2001-03-22 |
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PCT/JP2000/006223 WO2001019891A1 (fr) | 1999-09-13 | 2000-09-12 | Procede de production de poly(p-dioxanone), et monofilament de poly(p-dioxanone) et son procede de production |
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US (1) | US6448367B1 (ja) |
EP (1) | EP1136511B1 (ja) |
DE (1) | DE60034765T2 (ja) |
WO (1) | WO2001019891A1 (ja) |
Families Citing this family (6)
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US6660813B2 (en) * | 2001-08-03 | 2003-12-09 | University Of Florida | Solid state metathesis chemistry |
US8262963B2 (en) | 2002-10-04 | 2012-09-11 | Tyco Healthcare Group Lp | Process of making bioabsorbable filaments |
RU2520970C1 (ru) * | 2013-02-05 | 2014-06-27 | Федеральное государственное бюджетное учреждение науки Институт органического синтеза им. И.Я. Постовского Уральского отделения Российской академии наук | Способ получения поли-пара-диоксанона |
RU2570904C2 (ru) * | 2013-12-23 | 2015-12-20 | Общество с ограниченной ответственностью "ИнБио Полимеры" | Реактор периодического действия и способ его использования для полимеризации лактонов |
US11028222B2 (en) | 2018-11-28 | 2021-06-08 | Ethicon, Inc. | Advanced processing of absorbable poly(p-dioxanone) containing high level of p-dioxanone monomer |
CN114262950B (zh) * | 2022-01-12 | 2023-01-10 | 西安交通大学 | 一种高韧性聚对二氧环己酮可吸收丝线及其制备方法 |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4643191A (en) * | 1985-11-29 | 1987-02-17 | Ethicon, Inc. | Crystalline copolymers of p-dioxanone and lactide and surgical devices made therefrom |
Family Cites Families (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3284417A (en) * | 1963-11-13 | 1966-11-08 | Union Carbide Corp | Process for the preparation of lactone polyesters |
US4052988A (en) * | 1976-01-12 | 1977-10-11 | Ethicon, Inc. | Synthetic absorbable surgical devices of poly-dioxanone |
US5611986A (en) * | 1994-07-05 | 1997-03-18 | Ethicon, Inc. | Medical devices containing high inherent viscosity poly(p-dioxanone) |
ES2230780T3 (es) * | 1999-08-18 | 2005-05-01 | Christian Dr. Med. Jurgens | Copolilactidos resorbibles y su empleo. |
-
2000
- 2000-09-12 EP EP00957116A patent/EP1136511B1/en not_active Expired - Lifetime
- 2000-09-12 US US09/830,988 patent/US6448367B1/en not_active Expired - Fee Related
- 2000-09-12 DE DE60034765T patent/DE60034765T2/de not_active Expired - Lifetime
- 2000-09-12 WO PCT/JP2000/006223 patent/WO2001019891A1/ja active IP Right Grant
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4643191A (en) * | 1985-11-29 | 1987-02-17 | Ethicon, Inc. | Crystalline copolymers of p-dioxanone and lactide and surgical devices made therefrom |
Non-Patent Citations (1)
Title |
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See also references of EP1136511A4 * |
Also Published As
Publication number | Publication date |
---|---|
EP1136511A1 (en) | 2001-09-26 |
US6448367B1 (en) | 2002-09-10 |
DE60034765D1 (de) | 2007-06-21 |
EP1136511B1 (en) | 2007-05-09 |
DE60034765T2 (de) | 2008-01-31 |
EP1136511A4 (en) | 2002-12-18 |
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