POLYLACTIC ACID RESIN, TEXTILE PRODUCTS OBTAINED THEREFROM, AND PROCESSES FOR PRODUCING TEXTILE PRODUCTS

Abstract: A polylactic acid resin suitable for use especially in textile products; textile products obtained from the resin as a raw material (a fiber, multifilament, monofilament, staple, false-twist yarn, long-fiber nonwoven fabric, etc . ) ; and processes for producing these textile products. The polylactic acid resin is a resin consisting mainly of a polylactic acid and is characterized in that it is linear, has an L-isomer content of 95 mol% or higher, an Sn content of 0 or 30 ppm or lower, a monomer content of 0 or 0.5 wt.% or lower, and has a relative viscosity of 2.7 to 3.9 or has a weight-average molecular weight of 120,000 to 220,000 and a number-average molecular weight of 60,000 to 110,000. The textile products each comprises the polylactic acid resin as the main material. The textile products each comprises a polylactic acid excellent in processability and fiber properties and free from problems in practical use.

Description: The present invention relates to a multifilament comprising a synthetic resin, said synthetic resin mainly comprising linear polylactic acid containing 98 mol-% or more of the L-isomer and processes for producing the polylactic acid multifilament. The most widely used textile materials today include synthetic resins such as polyesters represented by polyethylene terephthalate and polyamides represented by 6-nylon and 66-nylon. While these synthetic resins are advantageous in their capability of cheap mass production, they involve some problems related to their disposal. The textile made of such synthetic resins can be hardly decomposed in the natural environment, and high heat of combustion is generated by incineration. Under these situations, use of biodegradable synthetic resins such as polycaprolactone and polylactic acid for textiles have been proposed. Although these resins are excellent in biodegradability, they are still not suitable for practical applications as compared with non-degradable synthetic resins such as polyethylene terephthalate and nylon that have been widely used. These problems are poor process throughput during the producing process (spinning, drawing, false twisting and the like), inferior properties such as tensile strength and elongation percentage of the textile products obtained as compared with conventional synthetic fibers. EP 0990678 A2 describes a resin composition comprising (A) a polylactic acid and (B) an aliphatic polyester carbonate, wherein the mixing ratio of polylactic acid (A) and an aliphatic polyester carbonate (B), in terms of the ratio of (A)/(B) by weight, is 95/5 to 5/95. The inventors of the present invention have made intensive survey on the physical and chemical properties of polylactic acid, and have investigated polylactic acid resins particularly suitable for use in the textile products. We have also found polylactic acid textile products being excellent in productivity and having favorable properties by using polylactic acid having selected properties, and a process for producing the textile products. The object of the present invention is to provide a multifilament practically acceptable textile products comprising polylactic acid having excellent properties for use in textiles with high productivity. DISCLOSURE OF THE INVENTION The object as hitherto described is attained by a multifilament comprising a synthetic resin, said synthetic resin being a linear polylactic acid resin containing 98 mol% or more of the L-isomer and containing 0 to 30 ppm of tin(Sn) and 0 to 0.5% by weight of monomer content with a relative viscosity ηrel of 2.7 to 3.9. The present invention also provides processes for producing the polylactic acid multifilament. (Polylactic acid resin) The polylactic acid resin used for the multifilament according to the present invention will be described first. The polylactic acid resin used for the multifilament according to the present invention includes a linear polylactic acid resin containing 98 mol% or more of the L-isomer and containing 0 to 30 ppm of Sn and 0 to 0.5% by weight of monomer content with a relative viscosity ηrel of 2.7 to 3.9. Polylactic acid to be used in the present invention has a linear structure, or substantially has no branched structure. A small amount of branching agent has been added during polymerization of polylactic acid in order to improve melt viscosity and degree of polymerization in the former proposal. However, it was confirmed by the inventors of the present invention that the branched structure of the starting resin material for producing the polylactic acid fiber has a far more negative effect on spinning work efficiency as compared with production of conventional polyester fibers. In other words, even a small amount of the branched structure adversely affects spinning work efficiency of polylactic acid, besides the fiber obtained has a low tensile strength. For excluding the branched structure, it is recommended that chemicals that cause branched structures in the polymer material, for example three valent or four valent alcohols and carboxylic acids, are not used at all. When these chemicals are forced to be used for some other reasons, the amount of use should be restricted within a range as small as possible so that spinning work efficiency is not adversely affected. Although polylactic acid used in the present invention is derived from a starting material such as L-lactic acid or D-lactic acid, or L-lactide or D-lactide as a dimer of lactic acid, or mesolactide, it is essential that the proportion of the L-isomer is 98 mol% or more. This is because increased proportion of the D-isomer makes the polymer amorphous and crystal orientation is not advanced in the spinning and drawing process, thereby deteriorating the properties of the fiber obtained. In particular, the tensile strength remarkably decreases with excess contraction ratio in boiling water to make the fiber to be practically inapplicable. Polylactic acid to be used in the present invention is required to contain 0 to 30 ppm, preferably 0 to 20 ppm, of Sn content in the polymer. While the Sn content based catalyst is used as a polymerization catalyst of polylactic acid, a content of more than 30 ppm causes depolymerization during the spinning process to allow the filtration pressure at the nozzle to increase in a short period of time, thereby remarkably decreasing spinning work efficiency. For decreasing the Sn content, the amount of use for polymerization may be decreased, or chips may be washed with an appropriate solvent. The polylactic acid to be used in the present invention contains 0.5% by weight, preferably 0.3% by weight or less and particularly 0 to 0.2% by weight of monomers. The monomer as defined in the present invention is referred to the component having a molecular weight of 1,000 or less as calculated from a GPC assay. A content of the monomer of more than 0. 5% by weight causes remarkable decrease of work efficiency, because heat resistance of polylactic acid decreases due to heat decomposition of the monomer component. For reducing the monomer content in polylactic acid, unreacted monomers are removed by evacuation of the reaction vessel immediately before completing the polymerization reaction, polymerized chips are washed with an appropriate solvent, or polylactic acid is produced by a solid phase polymerization. Polylactic acid to be used in the present invention preferably has a weight average molecular weight Mw of 120,000 to 220,000 and number average molecular weight Mn of 60,000 to 110,000. While the molecular weight in this range affords excellent spinning ability and sufficient tensile strength, the molecular weight out of this range causes large decrease of the molecular weight during spinning to fail in obtaining a sufficient tensile strength. Polylactic acid to be used in the present invention has a relative viscosity ηrel of 2.7 to 3.9. The relative viscosity of lower than this range causes to reduce heat resistance of the polymer and to fail in obtaining a sufficient strength, while the relative viscosity of higher than this range requires an elevated spinning temperature to cause heat-degradation during the spinning process. The relative viscosity having a lower reduction ratio during the spinning process is favorable and the preferable reduction ratio of relative viscosity is 7% or less for spinning multifilaments. A reduction ratio of 7% or less substantially results in no decomposition of the polymer during spinning, give rise to good spinning ability without arising broken fibers during spinning, and enabling particularly high tensile strength in the drawing process. It is preferable for practical production that the fiber produced has a tensile strength of 3.5 cN/dtex or more. The polylactic acid fiber according to the present invention is a multifilament. The fiber according to the present invention can be obtained by melt-spinning process known in the art. A biodegradable fiber excellent in work efficiency and properties of the textile may be obtained by producing the polylactic acid fiber using the resin as defined above. The polylactic acid fiber has physical properties such as tensile strength, drawing ratio and contraction ratio in boiling water comparable to conventional polyester and nylon fibers the fiber is excellent in heat resistance without decreasing spinning ability, the spinning nozzle has a sufficiently long service life, and the fibers are free from breakage and fluffs. The present invention will be described in more detail with reference to examples. Analysis of the properties of the polymer will be described first. (Molecular weight/monomer content) Samples were dissolved in chloroform in a concentration of 10 mg/mL, and Mw and Mn were measured by the GPC assay using Waters LC Model I Plus equipped with a RI detector. Polystyrene was used as a standard substance of the molecular weight. The proportions of the monomer in the polymer was calculated from the proportion of the component having a molecular weight of 1,000 or less. (Relative viscosity) The samples were dissolved in a mixed solvent of phenol/tetrachloroethane = 60/40 (in weight ratio) in a concentration of 1 g/dL, and the relative viscosity was measured at 20°C using a Ubbe/ohde viscosity tube. (Sn content) The sample (0.5g) was ashing by a wet process using sulfuric acid/nitric acid. The ashing sample was diluted with water to give a 50 mL sample solution, and the Sn content was measured using an ICP emission spectrometer SRS 1500VR made by Seiko Instruments Inc. Spinning work efficiency and fiber properties were measured and evaluated as follows. (Evaluation of spinning ability - 1) A 7-days' continuous spinning was performed by melt spinning. Incidence of broken fibers were evaluated in three steps (A, B and C) below: A: zero time of broken fiber in 7 days; B: one to two times of broken fiber in 7 days; and C: three or more times of broken fiber in 7 days. (Evaluation of spinning ability - 2) Service life of the spinning nozzle was evaluated in terms of days when the spinning nozzle was forced to change by increment of filtration pressure during the 7-days' continuous spinning. (Evaluation of spinning ability - 3) Incidence of broken fibers in the drawing process was evaluated in three steps of A, B and C: A: zero time of broken fiber in 7 days; B: one to two times of broken fiber in 7 days; and C: three or more times of broken fiber in 7 days. (Measurements of tensile strength and elongation percentage) Using a tensile strength tester manufactured by Shimadzu Co., a tensile test was performed at a speed of 20 cm/min using a sample with a length of 20 cm, and the tensile strength and elongation percentage was measured from the ultimate strength and ultimate elongation percentage, respectively. (Contraction ratio in boiling water) A 200mg weight was hanged to a sample with an initial length of 50 cm, and the sample was immersed in boiling water for 15 minutes followed by drying in the air for 5 minutes. The contraction ratio in boiling water was determined by the following equation: Contraction ratio (%) = (initial sample length - sample length after contraction)/initial sample length × 100 (Fluffs) Incidence of fluffs after reeling the drawn fiber was evaluated by the following two steps ( and ×). : no incidence of fluffs; and ×: incidence of fluffs. (Productivity of filament) Total evaluations of the filament was made in three steps of A, B and C by considering the evaluation of spinning ability 1, 2 and 3, and incidence of fluffs: A: very good B: good C: poor (Rate of decrease of viscosity during spinning) The relative viscosity (ηrel) of the filament extruded out of the spinning nozzle was measured, and the rate of decrease of viscosity during spinning was determined from the following equation. The residence time of the molten polymer in this example was about 10 minutes. The rate of decrease of viscosity during spinning (%) = [(relative viscosity of the polymer - relative viscosity of the filament)/relative viscosity of the polymer] × 100 (Polymerization of the polymer) L-lactide or D-lactide as a starting material was polymerized to polylactic acid using tin octylate as a polymerization catalyst by conventional polymerizing step. Polymerization was also carried out by adding 0.1 mol% of trimellitic acid as a cross-link agent (Comparative Example 10). While the polymer obtained was subsequently subjected to solid state polymerization at 135°C to reduce the amount of the residual monomers, the solid state polymerization was omitted in a part of the samples for comparison. (Spinning) Filaments of 84 dtex/24f were obtained by a conventional filament process of spinning and drawing by extruding the molten resin in the air through a spinning nozzle with a spinning hole diameter of 0.25 mm and number of spinning holes of 24. The spinning test was continued for 7 days to evaluate spinning ability, service life of the nozzle and incidence of fluffs during drawing. Reference Examples 1-1 to 1-2, and Comparative Examples 1-1 to 1-5 Table 1-1 shows the changes of spinning ability, service life of the nozzle and incidence of fluffs during drawing when the content of Sn in the polymer is changed, and the results of the quality of the fiber. In Comparative Examples 1-1 to 1-3, the polymer had been depolymerized during spinning due to particularly large content of Sn (the amount of the residual catalyst). Consequently, the viscosity was largely decreased during the spinning step to make it very difficult to spin. In addition, the service life of the nozzle was asshort as one day, quite large number of fluffs had generated during the spinning step due to large rate of decrease of viscosity during the drawing step, and the fiber obtained had a quite poor tensile strength of 2.6 cN/dtex or less to make it impossible to use the fiber for practical purposes. While the rate of decrease of viscosity during spinning was improved to 17.6% in Comparative Example 1-4, the service life of the nozzle was as short as three days. Although incidence of fluffs during drawing was also improved, the fiber was inappropriate for practical uses since a practical tensile strength of the fiber of 3.5 cN/dtex was not attained. The service life of the nozzle was increased to six days and the tensile strength of the fiber satisfied the practical level of 3.5 cN/dtex or more in Comparative Examples 1-5, since the rate of decrease of viscosity during spinning was improved to 12.3%. However, improvement of incidence of fluffs was yet insufficient because the resin contained as much Sn content as 35 ppm. In Reference Examples 1-1 and 1-2, the rate of decrease of viscosity was as small as 5.0%, and spinning ability, service life of the nozzle and incidence of fluffs during drawing were very excellent, since the content of Sn in the resin was 30 ppm or less. The tensile strength of the filament obtained was also excellent showing a level of 4.0 cN/dtex or more. Particularly, since the rate of decrease of viscosity during spinning was 7% or less, the degree of polymer degradation during the spinning process was small with no incidence of break of fibers during the spinning process, enabling good spinning ability to be obtained as a result of high tensile strength during the drawing process. Comparative Example Reference Example No.1- 1 2 3 4 5 1 2 Sn Content (ppm) 824 412 82 62 35 26 17 Relative Viscosity of Polymer (ηrel) 2.96 2.95 2.97 2.94 3.00 2.93 2.98 Monomer Content (% by weight) Branched Structure 0.26 0.23 0.25 0.24 0.26 0.26 0.25 Non Non Non Non Non Non Non L-isomer (mol%) 96.4 97.0 96.6 95.5 97.1 97.8 96.4 Spinning Temperature (°C) 230 230 230 230 230 230 230 Rate of Decrease of Viscosity during Spinning (%) 73.6 64.3 52.3 17.6 12.3 5.0 3.6 Spinning Ability 1 C C C C-B B A A Spinning Ability 2 1 1 1 3 6 ≥7 ≥7 Spinning Ability 3 C C C C-B B A A Fluffs × × × ×- productivity of Filament C C C C-B B A A Tensile Strength (cN/dtex) 1.78 1.87 2.23 3.14 3.76 4.38 4.53 Elongation (%) 26.3 27.3 28.3 28.6 30.3 29.3 28.6 Contraction Ratio in Boiling Water (%) 13.4 15.6 14.6 15.3 11.6 11.2 10.5 Examples 1-1 to 1-2, and Comparative Examples 1-6 to 1-9 Tables 1-2 and 1-3 show the changes of spinning ability, service life of the nozzle and incidence of fluffs during drawing when the monomer content in the polymer is changed and the results of the quality of the fiber. In Comparative Examples 1-6 to 1-8, the resin was heat-decomposed during spinning due to particularly large content of the monomer in the polymer. Spinning was quite difficult due to large decrease of the viscosity of the polymer during spinning, the service life of the nozzle was only one day, and a large quantity of fluffs was generated in the drawing process. The filament obtained had a poor fiber quality with a tensile strength of less than 3.5 cN/dtex to make the filament to be practically inapplicable. The monomer content was also large in Comparative Example 1-9, and the resin was inadequate for practical use since the service life of the nozzle was as short as five days. The rate of decrease of viscosity during spinning was improved to 5% or less in Examples 1-1 to 1-2, since heat decomposition could be suppressed by reducing the monomer content to 0.5% by weight or less. Spinning ability, service life of the nozzle and incidence of fluffs during drawing were also favorable in addition to high tensile strength of the filament obtained of 4.0 cN/dtex or more. Comparative Example No.1- 6 7 8 9 Monomer Content (% by weight) 10.2 5.76 3.46 0.98 Relative Viscosity of Polymer (ηrel) 2.96 2.89 2.92 3.02 Branched Structure Non Non Non Non Sn Content (ppm) 18 19 18 17 L-isomer (mol%) 95.4 96.0 95.6 96.5 Spinning Temperature (°C) 230 230 230 230 Rate of Decrease of Viscosity during Spinning (%) 25 20 15 10 Spinning Ability 1 C C C B Spinning Ability 2 1 1 2 5 Spinning Ability 3 C C C B Fluffs × × × ×- Productivity of Filament C C C C-B Tensile Strength (cN/dtex) 2.67 2.75 3.29 3.25 Elongation (%) 26.8 26.4 27.9 28.9 Contraction Ratio in Boiling Water (%) 12.4 14.6 13.2 12.3 Example No.1- 1 2 Monomer Content (% by weight) 0.26 0.15 Relative Viscosity of Polymer (ηrel) 2.98 3.02 Branched Structure Non Non Sn Content (ppm) 21 16 L-isomer (mol%) 98.4 98.4 Spinning Temperature (°C) 230 230 Rate of Decrease of Viscosity during Spinning (%) 2 1.5 Spinning Ability 1 A A Spinning Ability 2 ≥7 ≥7 Spinning Ability 3 A A Fluffs Productivity of Filament A A Tensile Strength (cN/dtex) 4.58 4.68 Elongation (%) 29.6 30.6 Contraction Ratio in Boiling Water (%) 10.9 9.8 (Multifilament) The multifilament according to the present invention will be described hereinafter. The multifilament according to the present invention comprises a synthetic resin, said synthetic resin being a linear polylactic acid containing 98 mol% or more of the L-isomer, 0 to 30 ppm of Sn content and 0 to 0.5% by weight of monomers with a relative viscosity of 2.7 to 3.9. The preferable embodiments comprise the following features: (α) a multifilament having a tensile strength of 3.9 cN/dtex or more, contraction ratio in boiling water of 12% or less, birefringence (Δn) of 0.025 or more and peak temperature of thermal stress of 85°C or more; and (β) a multifilament having an inert of 3.0 or less and contraction ratio in boiling water of 12% or less. The process for producing the multifilament according to the present invention comprises the following two alternatives: (1) a process for producing the polylactic acid multifilament using the polylactic acid as defined above comprising the steps of spinning at a speed of 3,000 m/min or more to 5,000 m/min or less, drawing at a draw magnification factor of 1.3 or more at a draw temperature of 100 to 125°C, and heat-setting at 125 to 150°C; and (2) a process for producing the polylactic acid multifilament using the polylactic acid as defined above comprising the steps of drawing the resulting multifilament between a roller heater (1) and a roller heater (2), and heat-setting at the roller heater (2). In the conventional method, the polylactic acid biodegradable fiber is manufactured by spinning at a low speed of 3,000 m/min or less followed by drawing. Although Japanese Patent Application Laid-open Nos. 7-216646 and 7-133569 disclose, for example, a producing method in which a non-drawn polylactic acid fiber spun at a speed of 1000 m/min or less is reeled and an orientation fiber is obtained in the drawing step, copolymerization of polyethylene glycol is necessary in the process disclosed above. However, work efficiency of the producing process can be hardly improved by the processes described above, and it was impossible to obtain physical and chemical properties and work efficiency comparable to the fibers made of conventional (non-biodegradable) synthetic resins. The inventors of the present invention have strictly surveyed the chemical and physical properties of polylactic acid as a starting material of the fiber, and have succeeded in providing a polylactic acid multifilament having such properties as tensile strength, elongation percentage and contraction ratio in boiling water comparable to polyester and nylon fibers, as well as being compatible to post-processing such as weaving, knitting and dyeing as in the polyester and nylon fibers, by using polylactic acid having selected properties and by investigating the spinning and drawing steps. Polylactic acid to be used in the present invention has a linear structure, or substantially has no branched structure. It has been proposed in the former proposal to add a small amount of branching agent in polymerization of polylactic acid in order to improve melt viscosity and degree of polymerization. However, it was confirmed by the inventors of the present invention that the branched structure of the resin material far more negatively affects work efficiency of spinning as compared with conventional polyester fibers in producing the polylactic acid fiber. Polylactic acid containing even a small amount of the branched structure exhibits lower tensile strength than polylactic acid containing no branched structure. For excluding the branched structure, it is recommended not to use any agents such as trivalent or quadrivalent alcohol and carboxylic acids that arise , the branched structure in the polymer material. When the components having such structure as described above are forced to be used for some reasons, the amount of use should be restricted within a minimum essential quantity that does not affect work efficiency of spinning such as break of fibers. While polylactic acid to be used in the present invention comprises L-lactic acid or D-lactic acid, or L-lactide or D-lactide as a dimer of lactic acid, it is crucial that lactic acid comprises 98 mol% or more of the L-isomer. This is because the polymer becomes amorphous when the proportion of the D-isomer increases and crystal orientation is inhibited in the spinning and drawing steps, thereby making the properties of the fiber obtained poor. In particular, the tensile strength is extremely degraded while excessively increasing the contraction ratio in boiling water to make practical application of the fiber impossible. Polylactic acid to be used in the present invention contains 0 to 30 ppm, preferably 0 to 20 ppm, of Sn. While Sn base catalyst used as a polymerization catalyst of polylactic acid, a residual amount of Sn of over 30 ppm causes depolymerization during spinning to bring about rapid increase of the nozzle pressure and extremely decreased work efficiency of spinning. In order to reduce the content of Sn, the amount of Sn used for polymerization is reduced to be as small as possible, or the chip is washed with an appropriate solvent. The monomer content in the polylactic acid to be used in the present invention is 0.5% by weight or less, preferably 0.3% by weight or less and in particular 0 or 0.2% by weight or less. The monomer as defined in the present invention refers to the component with a molecular weight of 1,000 or less as measured by the GPC analysis. Work efficiency of the fiber decreases due to occurrence of break of fibers in the spinning and drawing steps, when the monomer content exceeds 0.5% by weight. This is because the monomer component is decomposed by heat to decrease heat resistance of polylactic acid. Unreacted monomers may be removed by evacuating the reaction vessel just before completing the polymerization reaction, polymerized chips may be washed with an appropriate liquid, or polylactic acid is synthesized by solid phase polymerization in order to reduce the content of monomers in polylactic acid. Polylactic acid to be used in the present invention preferably has a weight average molecular weight Mw of 120,000 to 220,000, more preferably 130,000 to 160,000. Polylactic acid to be used in the present invention preferably also has a number average molecular weight Mn of 60,000 to 110,000, more preferably 70,000 to 90,000. While a molecular weight in this range allows an excellent spinning ability and sufficient tensile strength to be obtained, a sufficiently high tensile strength cannot be obtained at a molecular weight as low as out of this range because large decrease of the molecular weight. Polylactic acid to be used in the present invention has a relative viscosity of 2.7 to 3.9. A relative viscosity lower than this range makes heat resistance of the polymer poor, while a relative viscosity higher than this range requires the spinning temperature to be increased to cause heat degradation during spinning. The preferable relative viscosity is in the range of 2.9 to 3.3. A lower reduction ratio of the relative viscosity of the multifilament during spinning is preferable, and the reduction ratio is, for example, preferably 0 or 7% or less relative to the polymer. The reduction ratio of 0 or 7% or less substantially causes no decomposition of the polymer during spinning, makes spinning ability good without arising break of fibers during spinning, and allows the tensile strength in the drawing step to be particularly high. The multifilament according to the present invention preferably has a tensile strength of 4.0 cN/dtex or more, because no break of fibers occurs during each processing step. A birefringence of 0.030 or more is required for increasing the tensile strength to 4.0 cN/dtex or more. The peak temperature of thermal stress of the multifilament is preferably 85° C or more, more preferably 90°C or more, in order to prevent dyeing from being fatigued when the multifilament is dyed under an atmospheric pressure. A peak temperature of thermal stress of 85°C or more is preferable since the degree of fatigue of the dye is reduced. The multifilament preferably has an inert of 3% or less in the multifilament according to the present invention comprising linear polylactic acid containing 98 mol% or more of the L-isomer, 0 to 30 ppm of Sn and 0 to 0.5% by weight of monomers with a relative viscosity of 2. 7 to 3. 9. A content of the inert of 3% or less is preferable since uneven dyeing seldom occurs. The more preferable content of the inert is 1% or less. The present invention related to the process for producing the multifilament will be described hereinafter. In the present invention, the multifilament is spun at a spinning speed of 3,000 m/min or more and 5,000 m/min or less, drawn at a draw magnification ratio of 1,3 or more at a draw temperature of 100 to 125°C, and subjected to heat-setting at 125 to 150°C. Crystal orientation becomes insufficient at a spinning speed of less than 3,000 m/min to make work efficiency of the filament very poor due to break of fibers at a draw temperature of 110° C or more. A spinning speed of exceeding 4,500 m/min makes the filament uneven to generate uneven spots by cooling, thereby causing unstable work efficiency of spinning. Crystal orientation is prevented from advancing at a draw temperature of less than 110°C break of fibers and uneven spots by drawing causes. Too high draw temperature of exceeding 125°C causes break of fibers during the draw step. The tensile strength of the fiber becomes as low as less than 4.1 cN/dtex causing many troubles in the processing step such as break of fibers during weaving and knitting, unless the draw magnification factor exceeds 1.3. A draw magnification factor of 1.3 or more makes the fibers available for various processing by adjusting the elongation percentage. The draw magnification factor is preferably 1.3 to 1.8, more preferably 1.5 to 1.7, considering balance between the tensile strength and elongation percentage. A too low heat-set temperature of lower than 125°C makes the contraction ratio in boiling water high, and the fiber cannot be used due to large contraction in the post-processing. A heat-set temperature of exceeding 150°C causes break of fibers since the temperature is close to the melting point of the polylactic acid fiber. Therefore, a setting temperature of 135 to 150°C is preferable considering productivity of the filament. The process for producing the polylactic acid multifilament according to the present invention will be described hereinafter. In the process for producing the polylactic acid multifilament according to the present invention, the polylactic acid resin having a selected composition and property above mentioned is melt-spun, drawn between the roller heaters (1) and (2), and heat-set at the roller heater (2). The producing process is illustrated in Fig. 1. The conventional process is illustrated in Fig. 2. In this process, the non-drawn fiber 10 is drawn between a roller heater (21) and cold roller (23), heat-set at a plate heater (22) and rolled up through the cold roller to obtain rolled drawn fiber 20. The roller heater (1) is preferably heated at 100 to 125°C for orientation and crystallization of the multifilament in the producing process according to the present invention. The multifilament according to the present invention should be heat-set at the roller heater (2). Using the roller heater permits the draw point to be fixed at just under the roller heater (1), thereby enabling the linear density (tex) of the fine fibers from being uneven. The irregular linear density (tex) of the fine fiber is preferably restricted within ±10%, more preferably within ±7% or less, relative to the diameter of the multifilament. This range allows irregular dyeing to be prevented with favorable dyeing. The heat-set temperature of the roller heater (2) is preferably in the range of 125 to 150°C considering the contraction ratio in boiling water of the fiber obtained. The temperature is preferably 135 to 150°C considering productivity of the filament. (Example) The embodiments of the present invention will be described with reference to examples. The processes for measuring and evaluating each property will be described first. Measurements and evaluations other than described below were carried out in accordance with the processes as hitherto described. (Birefringence) The birefringence of the fiber was measured by a Berek compensator method using α-bromonaphthaline as an immersion solution. (Thermal stress) A thermal stress measuring instrument TYPE KE-2S made by Kanebo Engineering Co. was used. (Fatigue after dyeing) A cylindrical knit sample was prepared using the multifilament, and the sample was dyed under an atmospheric pressure using a disperse dye. Fatigue of the sample after dyeing was totally evaluated in three steps of A, B and C: A: very good (not fatigue at all) B: good C: poor (fatigue is so large that the product is not applicable as commercial products) (Inert) The inert (U%) was measured at a measuring speed of 50 m/min and twist speed of 5000 rpm using USTER-TESTER 4 made by Zelbeger-Uster Co. (Irregular linear density of the fiber) Irregularity in the diameter of the multifilament obtained by a measuring speed of 50 m/min and twist speed of 5,000 rpm was determined in percentage using USTER-TESTER 4 made by Zelbeger-Uster Co. (Dyeing) A test textile was woven using the filament after drawing, and the textile was dyed under an atmospheric pressure using a disperse dye. Dyeing of the textile was evaluated in two steps ( and ×) based on irregular dyeing, dimensional stability and pilling. : uniform dyeing x: irregular dyeing (Polymerization of polymer) Polylactic acid was synthesized by a process known in the art using L-lactide or D-lactide as a starting material and tin octylate as a polymerization catalyst. Trimellitic acid in a concentration of 0.1 mol% as a cross-link agent was added for polymerization for comparison. The polymer obtained was further polymerized at 135°C in the solid phase to reduce the amount of remaining monomers. However, no solid phase polymerization was applied for a part of the examples as comparative examples. Reference Examples 2-1 and 2-2 and Comparative examples 2-1 to 2-5 Table 2-1 shows the results of evaluations of spinning ability and (1), (2) and service life of the nozzle when the polymers with various contents of Sn are spun at a spinning speed of 3,800 m/min. With respect to Comparative Examples 2-1 to 2-3, the polymer was depolymerized during spinning due to particularly high content of Sn (residual catalyst). In addition, the rate of decrease of viscosity during spinning was very high to make spinning quite difficult, and the service life of the nozzle was as short as 1 day. Therefore, the polymer in these comparative examples are not practically applicable. While the rate of decrease of viscosity during spinning was improved to 17.6% in the polymer in Comparative Example 2-4, the service life of the nozzle was only three days due to large content of Sn, which makes the polymer practically inapplicable. The service life of the nozzle was prolonged to six days since the rate of decrease of viscosity during spinning was improved to 12.3%. However, the service life of seven days or more could not be attained since the content of Sn was as high as 35 ppm. The polymers in Reference Examples 2-1 and 2-2 was excellent in spinning ability because the rate of decrease of viscosity during spinning was as small as 5.0% due to the small content of Sn of 30 ppm or less with sufficient service life of the nozzle. Reference Example Comparative Example No.2- 1 2 1 2 3 4 5 Sn Content (ppm) 26 17 824 412 82 62 35 Relative Viscosity of Polymer (ηrel) 2.93 2.98 2.96 2.95 2.97 2.94 3.00 Monomer Content (% by weight) 0.26 0.25 0.26 0.23 0.25 0.24 0.26 Mw 12.5×10 4 13.9×10 4 13.9×10 4 13.9×10 4 13.7×10 4 13.5×10 4 14.4×10 4 Mn 6.6×10 4 6.9×10 4 6.8×10 4 6.7×10 4 6.9×10 4 6.6×10 4 7.0×10 4 Branched Structure Non Non Non Non Non Non Non L-isomer (mol%) 97.8 96.4 96.4 97.0 96.6 95.5 97.1 Spinning Temperature (°C) 230 230 230 230 230 230 230 Rate of Decrease of Viscosity during Spinning (%) 5.0 3.6 73.6 64.3 52.3 17.6 12.3 Spinning speed(m/min) 3800 3800 3800 3800 3800 3800 3800 Spinning Ability 1 A A C C C C-B B Spinning Ability 2 ≥7 ≥7 1 1 1 3 6 Examples 2-1 to 2-2, and Comparative Examples 2-6 to 2-9 Table 2-2 shows the results of spinning ability and service life of the nozzle when the spinning speed was adjusted to 3,500 m/min by varying the content of the monomer in the polymer. With respect to Comparative Examples 2-6 to 2-8, the polymer was heat-decomposed during spinning due to particularly high content of the monomer in the polymer. In addition, spinning was quite difficult due to large rate of decrease of viscosity during spinning besides the service life of the nozzle was as short as one day, making the polymer practically inapplicable. In the Comparative Example 2-9, the monomer content is still so high besides the service life of the nozzle is only five days, thereby also making the polymer practically inapplicable. With respect to Examples 2-1 to 2-2, heat decomposition was suppressed by reducing the monomer content to 0.5% by weight or less. Consequently, the rate of decrease of viscosity during spinning was improved to 5% or less, also making spinning ability, service life of the nozzle and occurrence of fluffs during drawing quite favorable. Example Comparative Example No.2- 1 2 6 7 8 9 Monomer Content (% by weight) 0.26 0.15 10.2 5.76 3.46 0.98 Relative Viscosity of Polymer (ηrel) 2.96 3.02 2.96 2.89 2.92 3.02 Branched Structure Non Non Non Non Non Non Sn Content (ppm) 21 16 18 19 18 17 L-isomer (mol%) 98.4 98.4 95.4 96.0 95.6 96.5 Mw 14.0×10 4 14.4×10 4 13.9×10 4 13.7×10 4 12.5×10 4 14.4×10 4 Mn 6.9×10 4 7.0×10 4 6.7×10 4 6.9×10 4 6.6×10 4 7.0×10 4 Spinning Temperature (°C) 230 230 230 230 230 230 Spinning speed(m/min) 3500 3500 3500 3500 3500 3500 Rate of Decrease of Viscosity during Spinning (%) 2 1.5 25 20 15 10 Spinning Ability 1 A A C C C B Spinning Ability 2 ≥7 ≥7 1 1 2 5 Example 2-3, and Comparative Examples 2-10 to 2-14 Tables 2-3 and 2-4 show productivity and properties of the multifilament by changing the proportion of the L-isomer, the molecular weight and relative viscosity of the polymer with or without the branched structure with the spinning speed and draw conditions constant, wherein the contents of Sn and monomers are adjusted to 30 ppm or less and 0.5% by weight, respectively. While the polymers in Example 2-3 and Comparative Example 2-10 have similar properties with each other except presence/absence of the branched structure, the polymer having the branched structure in Comparative Example 2-10 has somewhat poor spinning ability while generating fluffs during spinning. The tensile strength of the fiber was less than 3.5 cN/dtex, which is smaller than that of the fiber having no branched structure, and the peak temperature of thermal stress was 85°C or less, causing fatigue of dyeing to make the fiber practically inapplicable. Crystal orientation is hardly advanced during spinning and drawing in the fiber of Comparative Example 2-14 in Table 2-4 having the proportion of the L-isomer of less than 95 mol%. The tensile strength thereof is as small as less than 3.5 cN/dtex with the contraction ratio in boiling water of 30% or more. Therefore, the fiber is practically inapplicable as the multifilament due to poor dimensional stability in usual weave and knit processing. Since the fiber of Comparative Example 2-11 has a low molecular weight and relative viscosity, spinning and drawing ability becomes poor and the tensile strength thereof is as small as less than 3.5 cN/dtex. In Comparative Examples 2-12 and 2-13, on the other hand, the molecular weight and relative viscosity is so high that the spinning temperature is forced to be elevated. Increasing the spinning temperature results in the rate of decrease of viscosity during spinning to increase to 15% or more to make spinning and drawing ability poor with appearance of fluffs during drawing, thereby making the fiber to be practically inapplicable. Example No.2- 3 Monomer Content (% by weight) 0.27 Relative Viscosity of Polymer (ηrel) 3.02 Branched Structure Non Sn Content (ppm) 18 L-isomer (mol%) 98.7 Mw 14.6×10 4 Mn 7.2×10 4 Spinning Temperature (°C) 230 Rate of Decrease of Viscosity during Spinning (%) 3 Spinning speed(m/min) 3500 Spinning Ability 1 A Spinning Ability 2 ≥7 Draw temperature(°C) 110 Draw magnification factor 1.70 Set temperature(°C) 145 Spinning Ability 3 A Fluffs Productivity of Filament A Tensile Strength (cN/dtex) 4.43 Elongation (%) 30.3 Contraction Ratio in Boiling Water (%) 9.8 BirefringenceΔn 0.0350 Peak temperature of thermal stress(°C) 90 Fatigue after dyeing A Comparative Example No.2- 10 11 12 13 14 Monomer Content (% by weight) 0.26 0.26 0.25 0.24 0.27 Relative Viscosity of Polymer (ηrel) 3.04 2.58 4.02 4.03 3.02 Branched Structure Yes Non Non Yes Non Sn Content (ppm) 19 18 20 18 21 L-isomer (mol%) 99.0 96.4 97.0 98.7 92.6 Mw 14.8×10 4 10.2×10 4 23.8×10 4 24.0×10 4 14.5×10 4 Mn 7.6×10 4 5.4×10 4 12.1×10 4 12.4×10 4 7.1×10 4 Spinning Temperature (°C) 230 230 245 245 230 Rate of Decrease of Viscosity during Spinning (%) 6 8 15 20 3 Spinning speed(m/min) 3500 3500 3500 3500 3500 Spinning Ability 1 B B C C A Spinning Ability 2 4 4 5 3 ≥7 Draw temperature(°C) 110 110 110 110 110 Draw magnification factor 1.70 1.70 1.70 1.70 1.70 Set temperature(°C) 145 145 145 145 145 Spinning Ability 3 B C C C B Fluffs × × × × × Productivity of Filament C B C C B Tensile Strength (cN/dtex) 3.51 3.37 3.55 3.41 2.67 Elongation (%) 29.6 28.7 30.2 29.8 30.3 Contraction Ratio in Boiling Water (%) 10.2 10.1 9.7 10.2 30.5 Birefringence Δn 0.0276 0.02 65 0.02 89 0.0266 0.0235 Peak temperature of thermal stress(°C) 82 81 81 82 80 Fatigue after dyeing C B B C C Examples 2-4 to 2-6, Comparative Examples 2-15 to 2-19 Tables 2-5 and 2-6 show the results of spinning work efficiency and properties of the multifilament of the polylactic acid polymer having a relative viscosity of 3. 09, L-isomer content of 98.2 mol% and monomer content of 0.26% by weight without any branched structure based on the results in Tables 2-1 to 2-4 when the spinning and drawing conditions are changed. While Example 2-4 and Comparative Example 2-15 show the results obtained by changing the draw magnification factor of the fibers spun under the same condition, the fiber with the draw magnification factor of 1.3 or less in Comparative Example 2-15 has so low tensile strength and birefringence that the multifilament thereof is not suitable for practical applications. Comparative Example 2-16 shows the result obtained by reducing the spinning speed to 2,800 m/min. However, crystal orientation is so insufficient at a reel speed of 2800 m/min that the fiber cannot endure the draw temperature, and break of fiber often occurs to make productivity of the multifilament low for practical purposes. Example 2-5 and Comparative Example 2-17 show the results obtained by changing the draw temperature after reeling the fibers under the same condition. Since the draw temperature in Comparative Example 2-17 is lower than 100°C, break of fibers and generation of fluffs are often observed due to insufficient draw temperature. The fiber obtained has so low tensile strength and birefringence that it is not practically applicable. Example 2-5 and Comparative Example 2-18 show the results obtained by changing the set temperature after reeling the fibers under the same condition. Since the contraction ratio in boiling water is as high as 20% or more due to lower set temperature than 125°C in Comparative Example 2-18, the fiber is not practically applicable because the dimensional stability in post-processing such as dyeing is poor. Comparative Example 2-19 shows the results obtained by spinning at a speed exceeding 4,500 m/min. Although vibration of fibers, uneven fibers by cooling and break of fibers are often observed at a spinning speed of 4,800 m/min to make the fiber practically inapplicable, any problems are seen with respect to spinning and drawing at the spinning speed of 4,500 m/min in Example 2-6, and the multif ilament obtained had good physical and chemical properties. Example No. 2- 4 5 6 Spinning Temperature (°C) 230 230 230 Rate of Decrease of Viscosity during Spinning (%) 3 3 3 Spinning speed(m/min) 3200 4000 4500 Spinning Ability 1 A A A Spinning Ability 2 ≥7 ≥7 ≥7 Draw temperature(°C) 105 115 120 Draw magnification factor 1.7 1.5 1.3 Set temperature(°C) 145 135 150 Spinning Ability 3 A A A Fluffs Productivity of Filament A A A Tensile Strength (cN/dtex) 4.32 4.45 4.50 Elongation (%) 27.6 28.9 30.0 Contraction Ratio in Boiling Water (%) 10.2 9.8 9.7 Birefringence Δn 0.0332 0.0386 0.0394 Peak temperature of thermal stress(°C) 87 92 93 Fatigue after dyeing A A A Comparative Example No.2- 15 16 17 18 19 Spinning Temperature (°C) 230 230 230 230 230 Rate of Decrease of Viscosity during Spinning (%) 3 3 3 3 3 Spinning speed(m/min) 3200 2800 4000 4000 4800 Spinning Ability 1 × Spinning Ability 2 ≥7 ≥7 ≥7 ≥7 ≥7 Draw temperature (°C) 105 105 90 105 120 Draw magnification factor 1.2 1.9 1.5 1.5 1.3 Set temperature (°C) 150 150 150 115 150 Spinning Ability 3 C C B A C Fluffs × × × × productivity of Filament C C B B C Tensile Strength (cN/dtex) 2.83 3.64 3.50 4.30 4.18 Elongation (%) 35.0 27.6 27.4 28.6 25.4 Contraction Ratio in Boiling Water (%) 15.0 11.7 10.5 20.7 9.8 Birefringence Δn 0.0251 0.0271 0.0281 0.0310 0.0364 Peak temperature of thermal stress (°C) 78 81 79 83 90 Fatigue after dyeing C B B C B Example 3-1 and 3-2, Comparative Examples 3-1 to 3-8 Each polylactic acid polymer was melted at a given temperature and spun from a nozzle with a nozzle diameter of 0.3 mm. The fiber was reeled at a speed of 3,000 m/min followed by drawing to prepare a multifilament with a size of 84 dtex/24f, and dye affinity of the fiber was evaluated. Comparative Examples 3-1 and 3-2 show the results when the contents of residual Sn and monomers are large. Spinning ability is not so good due to large decrease of viscosity during spinning when the contents of residual Sn or monomers are large. Generation of fluffs was observed during drawing and pilling was observed during dyeing, respectively, to make the quality of the filament poor. The quality of the fiber in Comparative Example 3-3 was poor since the tensile strength was low and generation of fluffs was observed due to low viscosity and molecular weight (Mw and Mn) of the polymer. The quality of the fiber in Comparative Example 3-4 was also poor since the viscosity and molecular weight (Mw and Mn) of the polymer was so high that the spinning temperature was forced to be elevated, thereby causing large decrease of viscosity during spinning, and generating fluffs during drawing and pilling during dyeing. While Comparative example 3-5 shows the polymer having similar properties as the polymer in Example 1 except the presence/absence of the branched structure, the fiber obtained from the polymer having the branched structure in Comparative Example 3-5 generated fluffs during drawing and dye affinity was poor. In Comparative Examples 3-7 and 3-8, and in Examples 3-1 and 3-2, heat-setting after drawing was applied using a roller heater in the examples and using a plate heater in the comparative examples for the comparative purposes. The drawing points in the filament are not fixed in the filament heat-set using the plate heater, inert and irregular dying are not improved by changing the set temperature, and the filament was irregularly dyed to make the filament quality poor. Dye affinity was good, on the contrary, in the filament prepared by roller heater setting without arising irregular dying. Comparative Example No.3- 1 2 3 4 5 6 7 8 Sn Content (ppm) 62 18 16 15 19 21 16 16 Relative Viscosity of Polymer (ηrel) 2.94 2.92 2.50 4.02 3.04 3.05 3.05 3.05 Monomer Content (% by weight) 0.24 1.02 0.25 0.24 0.26 0.27 0.24 0.24 Mw/10 4 13.5 14.4 10.0 23.8 14.8 14.5 14.8 14.8 Mn /10 4 6.6 7.0 5.0 12.1 7.6 7.1 7.6 7.6 Branched Structure Non Non Non Non Yes Non Non Non L-isomer (mol%) 95.5 98.2 97.6 97.0 99.0 92.6 98.6 98.6 Spinning Temperature (°C) 230 230 230 245 230 230 230 230 Rate of Decrease of Viscosity during Spinning (%) 18 10 16 15 6 3 4 4 Draw magnification factor 1.7 1.7 1.7 1.7 1.7 1.7 1.7 1.7 roller heater (1) °C 110 110 110 110 110 110 110 110 roller heater (2) °C 135 135 135 135 135 135 - plate heater °C - - - - - - 135 115 Tensile strength (cN/dtex) 2.65 3.34 2.83 3.55 3.51 2.67 4.52 4.55 Elongation (%) 26.3 27.6 26.8 30.2 29.6 30.3 30.3 30.5 Contraction ratio in boiling water (%) 11.2 10.2 10.2 10.3 10.2 30.5 9.6 15.0 inert (U%) 1.78 1.23 1.83 1.82 1.54 1.56 3.80 2.50 Uneven fiber (%) ±6 ±5 ±5 ±6 ±5 ±5 ±15 ±10 Fluffs × × × × × dye affinity × × × × × × × × Example No.3- 1 2 Sn Content (ppm) 16 16 Relative Viscosity of Polymer (ηrel) 3.05 3.05 Monomer Content (% by weight) 0.24 0.24 Mw/10 4 14.8 14.8 Mn/10 4 7.6 7.6 Branched Structure Non Non L-isomer (mol%) 98.6 98.6 Spinning Temperature (°C) 230 230 Rate of Decrease of Viscosity during Spinning (%) 4 4 Draw magnification factor 1.7 1.7 roller heater (1) °C 110 110 roller heater (2) °C 135 150 plate heater °C ― ― Tensile strength (cN/dtex) 4.54 4.57 elongation (%) 28.7 27.6 Contraction ratio in boiling water (%) 9.6 8.0 inert (U%) 1.20 1.19 uneven fiber (%) ±5 ±5 Fluffs dye affinity Brief Description of the Drawings Fig. 1 schematically illustrates the drawing process according to the present invention; and Fig. 2 schematically illustrates the conventional drawing process. Reference Numerals 1 roller heater 2 roller heater 10 non-drawn fiber 20 drawn fiber 21 roller heater 22 plate heater 23 cold roller The present invention provides a multifilament, which can be used for the production of a textile product being excellent in work efficiency and having excellent properties of the fiber comprising polylactic acid that is free from practical problems for industrial production, and a process for producing the multifilament.

Claims: A multifilament comprising a synthetic resin, said synthetic resin being a linear polylactic acid resin containing 98 mol% or more of the L-isomer, 0 to 30 ppm of Sn content and 0 to 0.5% by weight of monomer content with a relative viscosity ηrel of 2.7 to 3.9. A multifilament according to claim 1 having a tensile strength of 3.9 cN/dtex or more, a contraction ratio in boiling water of 12% or less, a birefringence Δn of 0.030 or more, and a thermal stress peak temperature of 85°C or more. A polylactic acid multifilament according to claim 1 or 2 having an inert of 3.0 or less and a contraction ratio in boiling water of 12% or less. A process for producing a polylactic acid multifilament comprising the steps of: spinning the polylactic acid defined in claim 1 at a speed of 3,000 m/min or more and 5,000 m/min or less; drawing by 1.3 times or more at a draw temperature of 100° C to 125° C; and heat-setting at a temperature of 125°C to 150°C. A process for producing a polylactic acid multifilament comprising the steps of spinning the polylactic acid defined in claim 1, drawing the resulting multifilament between a roller heater (1) and roller heater (2) followed by heat-setting with the roller heater (2).

Inventors: KAJIYAMA HIROSHI, OGURA TOICHI, UEDA HIDEO, YOSHIDA HIROJI, KAJIYAMA, HIROSHI, OGURA, TOICHI, UEDA, HIDEO, YOSHIDA, HIROJI
Applicants: KANEBO LTD, KANEBO LIMITED
Application year: 2000
Main classification: C08G63
IPC codes: D01F6, D04H3, D01F8, D02G1, D02J1, D02G3, C08G63