WO2014045717A1 - ブロック共重合体の製造方法 - Google Patents
ブロック共重合体の製造方法 Download PDFInfo
- Publication number
- WO2014045717A1 WO2014045717A1 PCT/JP2013/070753 JP2013070753W WO2014045717A1 WO 2014045717 A1 WO2014045717 A1 WO 2014045717A1 JP 2013070753 W JP2013070753 W JP 2013070753W WO 2014045717 A1 WO2014045717 A1 WO 2014045717A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- resin
- block copolymer
- polylactic acid
- screw extruder
- twin
- Prior art date
Links
Classifications
-
- 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
- C08G63/91—Polymers modified by chemical after-treatment
- C08G63/912—Polymers modified by chemical after-treatment derived from hydroxycarboxylic acids
-
- 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
Definitions
- the present invention relates to a block copolymer composed of a polylactic acid-based resin and a resin having at least one hydroxyl group in the molecule, as production conditions thereof, a polylactic acid-based resin, a resin having at least one hydroxyl group in the molecule, and The transesterification catalyst is melted at normal pressure.
- the polylactic acid-based resin has been attracting attention because it is compatible with both of them and is relatively advantageous in terms of cost.
- the flexibility is insufficient.
- applications such as agricultural multi-films, shopping bags, packaging wrap films and stretch films, use of polylactic acid copolymers and addition of plasticizers Flexibility by is being considered.
- the polylactic acid block copolymer can be used as a flexible resin by mixing it alone or with a polylactic acid resin.
- the block copolymer when mixed with a polylactic acid resin, can function as a plasticizer.
- a plasticizer comprising a polylactic acid-polyether block copolymer described in Patent Document 1 has a conventional polylactic acid because the polylactic acid segment contributes to preventing exudation and the polyether segment contributes to plasticization of polylactic acid. Compared to plasticizers for plastic resins, it has a feature of excellent bleed-out resistance.
- these polylactic acid block copolymers are produced by opening lactide, which is a cyclic dimer of lactic acid, starting from a hydroxyl group of a resin having at least one hydroxyl group in the molecule. Those that polymerize are common.
- a polylactic acid resin and a resin having at least one hydroxyl group in the molecule are melted, and then a transesterification catalyst is added and transesterification is performed under reduced pressure.
- a known method for producing a polylactic acid block copolymer is known.
- the present invention solves such a conventional problem, and thereby obtains a method for producing a specific block copolymer with little residual lactide.
- a polylactic acid resin, a resin having at least one hydroxyl group in the molecule (hereinafter, a resin having at least one hydroxyl group in the molecule is referred to as a resin (A)), and a transesterification catalyst at normal pressure
- a block copolymer of polylactic acid resin and resin (A) (hereinafter referred to as polylactic acid resin) characterized by melting (hereinafter, melting at normal pressure is referred to as normal pressure / melting step)
- a method for producing a block copolymer with a resin (A) is referred to as a block copolymer).
- Polylactic acid wherein the block copolymer produced by the method described in (2) is directly introduced from a twin screw extruder 1 into another twin screw extruder and mixed with a polylactic acid resin.
- a twin screw extruder 1 For producing a mixture of a resin and a block copolymer.
- the block copolymer produced by the method according to (2) is charged with a polylactic acid resin from the side feeder of the same twin-screw extruder as that produced the block copolymer.
- a block copolymer with little residual lactide can be obtained.
- the block copolymer obtained by the present invention can be used as a flexible resin for molded articles such as films, alone or mixed with a polylactic acid resin, and a plasticizer having bleed-out resistance for a polylactic acid resin. Can also be suitably used.
- the present invention relates to a polylactic acid-based resin, a resin having at least one hydroxyl group in the molecule (hereinafter, a resin having at least one hydroxyl group in the molecule is referred to as a resin (A)), and a transesterification catalyst at normal pressure.
- a resin having at least one hydroxyl group in the molecule is referred to as a resin (A)
- Block copolymer of polylactic acid resin and resin (A) hereinafter referred to as polylactic acid resin
- characterized by melting at a normal pressure hereinafter referred to as normal pressure / melting step
- a resin (A) block copolymer is referred to as a block copolymer).
- polylactic acid resin In the present invention, a polylactic acid resin is used as a raw material for producing the block copolymer.
- the polylactic acid-based resin is a polymer having an L-lactic acid unit and / or a D-lactic acid unit as main constituent components.
- the main component means that the ratio of lactic acid units is the maximum in 100 mol% of all monomer units in the polymer, and preferably 70% of lactic acid units in 100 mol% of all monomer units. ⁇ 100 mol%.
- the poly-L-lactic acid in the present invention refers to those in which the content of L-lactic acid units is more than 50 mol% and not more than 100 mol% in 100 mol% of all lactic acid units in the polymer.
- the poly D-lactic acid in the present invention refers to those having a D-lactic acid unit content of more than 50 mol% and not more than 100 mol% in 100 mol% of all lactic acid units in the polymer.
- the polylactic acid resin in the present invention does not include those obtained by block copolymerization of the resin (A).
- resin (A) and polylactic acid-type resin are copolymerized, this is called a block copolymer.
- Poly L-lactic acid changes in the crystallinity of the resin itself depending on the content ratio of the D-lactic acid unit. That is, if the content ratio of D-lactic acid units in poly-L-lactic acid increases, the crystallinity of poly-L-lactic acid decreases and approaches amorphous, and conversely the content ratio of D-lactic acid units in poly-L-lactic acid. As the amount decreases, the crystallinity of poly-L-lactic acid increases. Similarly, the crystallinity of the resin itself of poly D-lactic acid varies depending on the content ratio of L-lactic acid units.
- the content ratio of the L-lactic acid unit in the poly L-lactic acid used in the present invention or the content ratio of the D-lactic acid unit in the poly D-lactic acid used in the present invention can be arbitrarily adjusted.
- L-lactic acid units are 90 to 100 mol%, or D-lactic acid units are 90 to 100 mol%, based on 100 mol% of all lactic acid units.
- the L-lactic acid unit is 95 to 100 mol%, or the D-lactic acid unit is 95 to 100 mol%.
- the block copolymer obtained in the present invention is used as a plasticizer for a crystalline polylactic acid resin
- a co-crystal is formed between the polylactic acid resin and the polylactic acid segment of the block copolymer.
- the content ratios of L-lactic acid and D-lactic acid are preferably the same as described above.
- the resin is low. Since it is preferably crystalline or amorphous, L-lactic acid units and D-lactic acid units are preferably 10 to 90 mol% in 100 mol% of all lactic acid units.
- the crystalline polylactic acid resin in the present invention is measured with a differential scanning calorimeter (DSC) at a temperature rising rate of 20 ° C./min after leaving the polylactic acid resin to stand for 1 hour under heating at 100 ° C.
- DSC differential scanning calorimeter
- it means a polylactic acid resin in which the heat of crystal melting derived from the polylactic acid component is observed.
- the amorphous polylactic acid resin referred to in the present invention means a polylactic acid resin that does not exhibit a melting point when measured in the same manner.
- the polylactic acid resin used in the present invention may be randomly copolymerized with other monomer units other than lactic acid.
- Other monomers include ethylene glycol, propylene glycol, butanediol, heptanediol, hexanediol, octanediol, nonanediol, decanediol, 1,4-cyclohexanedimethanol, neopentyl glycol, glycerin, pentane Glycol compounds such as erythritol, bisphenol A, polyethylene glycol, polypropylene glycol and polytetramethylene glycol, oxalic acid, adipic acid, sebacic acid, azelaic acid, dodecanedioic acid, malonic acid, glutaric acid, cyclohexanedicarboxylic acid, terephthalic acid , Isophthalic acid, phthalic acid, na
- the copolymerization amount of the other monomer units as described above is preferably 0 to 30 mol%, preferably 0 to 10 mol%, based on 100 mol% of the whole monomer units in the polylactic acid resin polymer. More preferably. In addition, it is preferable to select the component which has biodegradability among the above-mentioned monomer units according to a use.
- the mass average molecular weight of the polylactic acid-based resin used in the present invention is preferably 5,000 to 1,000,000 from the viewpoint of the molecular weight of the block copolymer after the reaction and the handleability at the time of melting. More preferably, it is from 1,000 to 500,000, and most preferably from 100,000 to 300,000.
- the mass average molecular weight in this invention means the molecular weight which measured with the good solvent, such as hexafluoroisopropanol, by gel permeation chromatography (GPC), and was calculated by the polymethylmethacrylate conversion method.
- the method for producing the polylactic acid resin used in the present invention can be obtained by a method of directly dehydrating condensation of lactic acid and other raw materials, or a method of ring-opening polymerization of lactide and other cyclic ester intermediates.
- lactic acid or lactic acid and hydroxycarboxylic acid are preferably subjected to azeotropic dehydration condensation in the presence of an organic solvent, particularly a phenyl ether solvent, and particularly preferably a solvent distilled by azeotropic distillation.
- a polymer having a high molecular weight can be obtained by polymerizing by a method in which water is removed from the solvent and the solvent is brought into a substantially anhydrous state and returned to the reaction system.
- a high molecular weight polymer can be obtained by subjecting a cyclic ester intermediate such as lactide to ring-opening polymerization under reduced pressure using a catalyst such as tin octoate.
- a method for adjusting the conditions for removing moisture and low molecular weight compounds during heating and refluxing in an organic solvent, a method for suppressing the depolymerization reaction by deactivating the catalyst after completion of the polymerization reaction, and a method for heat-treating the produced polymer Can be used to obtain a polymer with a small amount of lactide.
- resin (A) is used as a manufacturing raw material of a block copolymer.
- the ester exchange reaction proceeds from the hydroxyl group of the resin (A) to the ester bond between the lactic acid unit and the lactic acid unit in the polylactic acid resin, at least one resin (A) is present in the molecule. It is important that the resin has two hydroxyl groups.
- the resin (A) is a resin having at least one hydroxyl group in the molecule other than the polylactic acid resin.
- the resin (A) examples include a polyester resin other than a polylactic acid resin, a polyether resin, a polyacetal resin, and the like as a resin containing a hydroxyl group at a molecular terminal. Further, as a resin containing a hydroxyl group in the side chain, polyvinyl alcohol resin, ethylene-vinyl alcohol copolymer resin, polysaccharide, esterified product of polysaccharide, etherified product of polysaccharide, deoxyhalide of polysaccharide, polysaccharide Examples thereof include oxides and hydroxyl group-modified polyolefin resins. In order to impart flexibility to the polylactic acid-based resin, the glass transition temperature of the resin (A) is preferably ⁇ 70 to 50 ° C., more preferably ⁇ 70 to 40 ° C.
- the resin (A) is a polyester-based resin other than the polylactic acid-based resin and / or poly It is preferably an ether resin, more preferably a polyether resin, and further preferably a polyalkylene glycol resin.
- polyalkylene glycol resin is polyethylene glycol, polypropylene glycol, polytetramethylene glycol, polyethylene glycol / polypropylene glycol copolymer, and among these, polyethylene glycol is most preferred. Since polyethylene glycol is flexible and has high affinity with the polylactic acid resin, the block copolymer of the polylactic acid resin and polyethylene glycol is excellent in flexibility and plasticization efficiency of the polylactic acid resin.
- the mass average molecular weight of the resin (A) used in the present invention is 1,000 to 1,000,000 from the viewpoint of the molecular weight and flexibility of the block copolymer after the reaction and the handling property at the time of melting. It is preferably 5,000 to 500,000, more preferably 5,000 to 100,000, and most preferably 5,000 to 30,000.
- Transesterification catalyst In the present invention, it is important to melt the polylactic acid resin, the resin (A), and the transesterification catalyst at normal pressure. That is, in the present invention, the block copolymer is produced by a transesterification method, and it is important to use a transesterification catalyst at that time.
- the transesterification catalyst in the present invention is not particularly limited, and examples thereof include metals, metal salts, sulfur acids, and nitrogen-containing basic compounds.
- metals include manganese, magnesium, titanium, zinc, iron, aluminum, cerium, calcium, barium, cobalt, lithium, sodium, potassium, cesium, lead, strontium, tin, antimony, germanium, yttrium, lanthanum, indium, Zirconium etc. are mentioned.
- metal salt examples include metal organic acid salt, metal nitrate, metal phosphate, metal borate, metal halide salt, metal hydroxide salt and the like.
- organic acids include carboxylic acid, sulfur acid, carbonic acid, phenol and the like.
- sulfur acids examples include sulfuric acid, sulfonic acid compounds, sulfinic acid compounds, and sulfenic acid compounds.
- nitrogen-containing basic compounds examples include quaternary amine salts, tertiary amines, secondary amines, primary amines, pyridines, imidazoles, ammonia and the like.
- the transesterification catalyst in the present invention is preferably a metal salt from the viewpoint of dispersibility in the resin, the degree of decomposition and molecular weight reduction of the resin, and the effect as a catalyst, and the metal organic acid salt and / or metal More preferred is a halide salt.
- organic acid salts of metals and / or metals is preferably a salt of an organic acid having a C 0-10 alkyl group and a metal (metal organic acid salt) and / or a metal halide salt.
- an alkyl group having 0 carbon atoms means that there is no alkyl group in the molecule.
- the block copolymer obtained in the present invention is an ester used in the present invention, considering the possibility of being used for agricultural and forestry applications and applications requiring biodegradability such as garbage bags and compost bags.
- the exchange catalyst is preferably one that is highly safe to living organisms.
- the transesterification catalyst is preferably a metal organic acid salt and / or a metal halide salt. Examples thereof include a salt of an organic acid having a number of 0 to 10 alkyl groups and a metal (organic organic acid salt), or a metal halide salt shown below.
- a salt of an organic acid having an alkyl group having 0 to 10 carbon atoms and a metal which are particularly preferable as a metal organic acid salt, include, for example, a carboxylic acid having 1 to 10 carbon atoms having no hydroxyl group.
- particularly preferred metal halide salts are metal halides selected from, for example, magnesium, titanium, tin, zinc, iron, aluminum, calcium, and potassium.
- two or more different transesterification catalysts can be used in combination.
- Method for producing block copolymer of polylactic acid resin and resin (A) In the method for producing a block copolymer of the present invention, a raw material polylactic acid resin, resin (A), and transesterification catalyst are supplied to a reactor and melted at normal pressure (through a normal pressure / melting step). ).
- a block copolymer is produced by performing a transesterification reaction between the polylactic acid resin and the resin (A).
- the transesterification referred to here means that a hydroxyl group, a carboxylic acid group, or another ester bond is allowed to act on a certain ester bond to cause an exchange with a hydroxyl group or a carboxylic acid group in the ester bond. Is a reaction that forms another type of ester bond.
- the main object of the present invention is to introduce an ester bond between the polylactic acid resin and the resin (A) by allowing the hydroxyl group of the resin (A) to act on the ester bond of the polylactic acid resin. To do.
- the melting temperature in the normal pressure / melting process varies depending on the type of reactor, the melting point of the polylactic acid resin, the melting point of the resin (A), the viscosity of the polylactic acid resin, and the viscosity of the resin (A).
- the temperature in the normal pressure / melting step is preferably 150 to 250 ° C., more preferably 180 to 240 ° C.
- the polylactic acid-type resin and resin (A) to be used are fully dried beforehand and it is preferable to reduce a moisture content.
- the water content of both the polylactic acid resin and the resin (A) is preferably 1,200 ppm (mass basis) or less, more preferably 500 ppm (mass basis) or less, and 200 ppm (mass basis) or less. Is more preferable.
- the charging mass ratio between the polylactic acid resin and the resin (A) is not particularly limited, but a preferable range is 95: 5 to 5:95 by mass ratio.
- the charged mass ratio of the polylactic acid resin and the resin (A) is 95: 5 to 50:50. It is preferable that the ratio is 90:10 to 60:40.
- the charged mass ratio of the polylactic acid resin to the resin (A) is preferably 80:20 to 5:95, and 75: More preferably, it is 25 to 10:90, and further preferably 70:30 to 30:70.
- the amount of transesterification catalyst added varies depending on the type of reactor, reaction temperature, reaction time, reaction atmosphere, etc., but is 0.001 to 5 with respect to 100 parts by mass of the total of the polylactic acid resin and the resin (A).
- the range is preferably in the range of parts by mass, and more preferably in the range of 0.005 to 1 part by mass. If the amount of the transesterification catalyst added is in the range of 0.001 to 5 parts by mass with respect to 100 parts by mass in total of the polylactic acid resin and the resin (A), coloring of the resulting block copolymer and reduction in molecular weight And the generation of lactide can be kept to a minimum.
- the normal pressure in the present invention means that the atmospheric pressure in the normal pressure / melting step is within the range of 5 ⁇ 10 4 to 1.5 ⁇ 10 5 Pa, and is 7 ⁇ 10 4 to 1.3 ⁇ 10 5 Pa. Is preferable, and more preferably 9 ⁇ 10 4 to 1.1 ⁇ 10 5 Pa.
- the reactor is preferably placed in an inert gas atmosphere in order to suppress hydrolysis and oxidative degradation of the resin.
- the reactor used for the normal pressure / melting process is not particularly limited, and examples of the batch reactor include a test tube with a stirrer, a vertical or horizontal tank reactor, or a kneader.
- examples of the continuous reactor include a single screw extruder, a twin screw extruder, and other multi-screw extruders. In a multi-screw extruder of two or more axes, the screw rotation direction may be the same or different.
- the reactor in the normal pressure / melting step is preferably a continuous reactor, and more preferably a twin screw extruder. That is, the normal pressure / melting step is preferably performed in a continuous reactor, particularly in a twin-screw extruder.
- twin-screw extruder not only the melting of the polylactic acid resin and the resin (A) proceeds rapidly, but also the distribution mixing and dispersion mixing of the resins proceed efficiently, so the ester bond of the polylactic acid resin and the resin (A) The probability of collision with a hydroxyl group increases, and as a result, their transesterification proceeds in a short time.
- the normal pressure / melting step is preferably performed in a twin-screw extruder, but the screw configuration of such a twin-screw extruder is to ensure the resin residence time and kneading force necessary for the reaction. It is preferable to use a kneading disk having an opposite direction, the screw diameter is preferably 10 to 400 mm, and the L / D is preferably 20 to 200.
- the atmospheric pressure is measured at the vent hole.
- the time required for the normal pressure / melting step is preferably 30 minutes to 5 hours when a batch reactor having low kneading properties is used.
- the normal pressure / melting process time corresponds to the residence time of the resin in the reactor, which is preferably 5 to 30 minutes. More preferably, it is 5 to 15 minutes.
- the block copolymer obtained by the production method of the present invention can further improve its storage stability by deactivating the remaining transesterification catalyst.
- the quenching agent used for such purposes include amino acids, phenols, hydroxycarboxylic acids, diketones, amines, oximes, phenanthrolines, pyridine compounds, dithio compounds, diazo compounds, thiols, porphyrins,
- the coordination atom include nitrogen-containing phenols and phosphorus compounds such as carboxylic acid, phosphoric acid, phosphoric acid ester, phosphoric acid metal salt, phosphorous acid, phosphorous acid ester, and phosphorous acid metal salt.
- deactivators can be used alone or in combination. Among these deactivators, phosphorus compounds are more preferable, and phosphoric acid crystals or phosphorous acid crystals having a purity of 98% by mass or more are more preferable from the viewpoint of hydrolysis resistance of the polylactic acid resin.
- a method for adding a deactivator in the case of a batch reactor, there is a method in which the reactor is stopped once after the transesterification reaction is completed, and the reactor is operated again after adding the deactivator.
- a continuous reactor represented by a twin screw extruder there is a method of adding a quencher from a side feeder of the extruder.
- the addition amount of the deactivator is preferably 0.01 to 10 parts by mass, more preferably 0.1 to 5 parts by mass with respect to 1 part by mass of the transesterification catalyst added in the production process.
- the mass average molecular weight of the block copolymer obtained in the present invention in the case where the present block copolymer is the main component of the molded product, in order to satisfy practical mechanical properties, its mass average molecular weight Is preferably 10,000 to 1,000,000, and more preferably 50,000 to 500,000. Further, when the present block copolymer is used as an additive such as a plasticizer, its mass average molecular weight is preferably 1,000 to 500,000 in order to exhibit softening and bleed-out resistance. 5,000 to 100,000, more preferably 5,000 to 50,000.
- the block copolymer obtained in the present invention can be used in combination with a polylactic acid resin.
- the block copolymer in this case can also function as a plasticizer for the polylactic acid resin.
- the block copolymer obtained in the present invention in order to disperse the block copolymer in the polylactic acid resin, the polylactic acid resin and the block copolymer are used.
- the polymer may be melt-kneaded, or the polylactic acid resin and the block copolymer may be dissolved in a good solvent such as chloroform, and the resin may be volatilized or the resin precipitated in a poor solvent.
- the content ratio of the polylactic acid resin and the block copolymer is 100% by mass in total of the block copolymer and the polylactic acid resin.
- the polymer is preferably contained in an amount of 3 to 70% by mass, more preferably 5 to 60% by mass, and even more preferably 5 to 50% by mass. If the content rate of a block copolymer is in said range, the softness
- the block copolymer is used as a plasticizer for a polylactic acid-based resin
- other thermoplastic resins in addition to the polylactic acid-based resin and the block copolymer, other thermoplastic resins, general particles and additives are contained in the resin composition. You may mix.
- the normal pressure / melting step for producing the block copolymer is preferably performed in a twin screw extruder (hereinafter, the twin screw extruder is referred to as the twin screw extruder 1) as described above. Furthermore, when producing a mixture of a polylactic acid resin and a block copolymer, such as using a block copolymer as a plasticizer for a polylactic acid resin, the block copolymer produced in the twin screw extruder 1 is used.
- twin-screw extruder 2 A twin-screw extruder 2 is referred to as the twin-screw extruder 2
- a method for producing a mixture of a polylactic acid resin and a block copolymer, which is characterized by mixing with a polylactic acid resin, is preferred. That is, when producing a mixture of a polylactic acid-based resin and a block copolymer, the block copolymer produced by the twin-screw extruder 1 is used in a twin-screw extruder 2 using a polymer tube or the like in a molten state.
- the term “directly” means that when the block copolymer is introduced from the twin-screw extruder 1 into the twin-screw extruder 2, the block polymer is kept in the twin-screw extruder 1 from the twin-screw extruder 1 while maintaining the glass transition temperature or higher. It means introducing into the extruder 2. For example, when the block copolymer is taken out from the twin-screw extruder 1 and introduced into the twin-screw extruder 2 in a state where the block copolymer is at a glass transition temperature or lower, it is directly referred to here.
- the block copolymer has a plurality of glass transition temperatures
- the mass average molecular weight of the block copolymer may be small and the glass transition temperature may be low, and such a block copolymer is difficult to chip. There is a possibility. In such a case, it is necessary to cool and solidify the obtained block copolymer once, and then to perform pulverization. On the other hand, if the block copolymer obtained by using the twin screw extruder 1 is directly introduced into the twin screw extruder 2 and mixed with the polylactic acid resin in the twin screw extruder 2, The cooling and pulverization time and labor described above are omitted, which is preferable.
- the screw configuration, screw diameter, L / D, and residence time of the twin screw extruder 1 and the twin screw extruder 2 are the same as the preferred screw configuration, screw diameter, L / D, and residence time of the twin screw extruder described above. It is preferable. Moreover, the twin screw extruder 1 and the twin screw extruder 2 may have the same configuration.
- twin-screw extruder 1 in which the block copolymer is produced needs to be at normal pressure for the reasons described above.
- the range of normal pressure is the same as described above.
- the pressure in the twin screw extruder 2 does not necessarily need to be a normal pressure, and can be reduced.
- the same biaxial extrusion as that in which the block copolymer was produced is performed on the block copolymer produced by a twin screw extruder.
- the block copolymer and the polylactic acid resin are mixed in the same twin-screw extruder as that produced the block copolymer by introducing the polylactic acid resin from the side feeder of the machine.
- a preferable screw configuration of the twin-screw extruder used in the present method is to put a kneading disk in front of the side feeder into which the polylactic acid resin is charged.
- the screw diameter, L / D and residence time are preferably the same as the preferred screw diameter, L / D and residence time of the twin screw extruder described above.
- the extrusion temperature is preferably 200 to 280 ° C. near the kneading disk, and the catalyst amount is preferably 0.05 to 5 parts by mass. This is because the block copolymer is mainly produced in this method from the point of the main feeder of the twin screw extruder to the point of the side feeder into which the polylactic acid resin is put, that is, a part of the twin screw extruder. This is because it is necessary to efficiently advance the reaction in this portion. Moreover, it is preferable to add a deactivator at the same time when putting the polylactic acid resin from the side feeder.
- the block copolymer is mainly produced from the point of the main feeder of the twin-screw extruder to the point of the side feeder into which the polylactic acid resin is put.
- the range of normal pressure is the same as described above.
- the atmospheric pressure is not necessarily a normal pressure in the section, and can be reduced.
- the polylactic acid resin used in the mixture of the polylactic acid resin and the block copolymer can be the same resin as the polylactic acid resin described above as a raw material for the block copolymer.
- the composition containing the block copolymer obtained in the present invention includes known antioxidants, crystal nucleating agents, UV stabilizers, anti-coloring agents, matting agents, deodorants, flame retardants, weathering agents, charging agents.
- Additives such as inhibitors, ion exchangers, tackifiers, antifoaming agents, color pigments, dyes, lubricants, foaming agents, and other resins may be used as necessary.
- the addition amount of these additives is not particularly limited as long as the effects achieved in the present invention are not impaired, but the additive is added to 100% by mass of the composition containing the block copolymer. Is preferably 0.01 to 30% by mass, more preferably 0.01 to 20% by mass, and still more preferably 0.01 to 10% by mass.
- the block copolymer obtained in the present invention preferably has a residual lactide content of 1.00% by mass or less, more preferably 0.70% by mass or less. More preferably, it is 0.50% by mass or less.
- the block copolymer obtained by this invention has one peak derived from a polymer in the GPC elution curve. Is preferably present (unimodal). When the polylactic acid-based resin and the resin (A) remain, there are two (bimodal) peaks derived from the polymer in the GPC elution curve.
- TmA0 and TmA defined below TmA0-TmA is preferably 7.0 ° C. or higher, and more preferably 9.0 ° C. or higher.
- TmA0 Melting peak temperature derived from the resin (A), read from the DSC temperature rising chart of the resin (A) alone.
- TmA Melting peak temperature derived from the resin (A) segment, read from the DSC temperature rising chart of the block copolymer.
- the resulting sheet exhibits a sufficient flexibility, so that its tensile elastic modulus is 100 to 1,000 MPa. It is preferable.
- the tensile modulus is more preferably 100 to 950 MPa, and further preferably 100 to 900 MPa.
- the sheet containing the block copolymer and the polylactic acid resin needs to prevent the block copolymer from coming out of the polylactic acid resin, that is, its bleed-out resistance.
- the hot water extraction rate of the sheet is preferably in the following range. That is, the mass reduction rate when the sheet is treated for 1 hour in distilled water boiled at 1 atm is preferably 5.0% or less, and more preferably 3.0% or less.
- Elastic modulus (MPa) Stress-strain measurement was performed using TENSILON UCT-100 manufactured by Orientec Co., Ltd. Using the first linear part of the stress-strain curve, the stress difference between the two points on the straight line was the same as the strain difference between the two points. And the tensile modulus was calculated. Specifically, a strip-like sample having a length of 150 mm and a width of 10 mm is cut out from the breath sheet, and measured according to the method defined in JIS K 7127 (1999) at an initial tensile chuck distance of 50 mm and a tensile speed of 200 mm / min. It was. Moreover, the measurement was performed 5 times and the average value was calculated.
- Hot water extraction rate was measured as an index of bleed-out resistance.
- the mass before processing was measured for a press sheet that had been conditioned for 1 day or more in an atmosphere of a temperature of 23 ° C. and a humidity of 65% RH. Next, the sheet was immersed in distilled water boiled at 1 atm for 1 hour, and after conditioning again under the same conditions as before the treatment, the mass after the treatment was measured. And the hot water extraction rate was computed by the following formula.
- Hot water extraction rate (mass%) (mass before treatment ⁇ mass after treatment) ⁇ 100 / mass before treatment (4)
- GPC The mass average molecular weight was measured by gel permeation chromatography (GPC) and calculated by a polymethyl methacrylate conversion method.
- the calculation of the mass average molecular weight is performed only when there is only one polymer-derived peak in the elution curve of the obtained sample (unimodal), and it is derived from the polylactic acid resin and the resin (A). This was not carried out in the case of having peaks derived from two polymers (bimodal) or having peaks derived from more polymers.
- GPC measurement was performed using a Waters 2695 model, a WATERS differential refractometer 2414 model was used as the detector, a WATERS MODEL 510 was used as the pump, and two Shodex HFIP-806Ms were connected in series to the column. Used.
- Measurement conditions were a flow rate of 0.5 mL / min, a column temperature of 40 ° C., hexafluoroisopropanol added with 5 mM sodium trifluoroacetate as a solvent, and 0.2 mL of a solution having a sample concentration of 0.1% by mass was injected.
- Polylactic acid resin (4032D) Poly L-lactic acid, “4032D” manufactured by Natureworks, mass average molecular weight 200,000, D-form content 1.4 mol%, melting point 166 ° C. A product dried in advance at 100 ° C. for 5 hours while reducing the pressure in a vacuum oven was used.
- the mass average molecular weight was measured using Waters 2695 manufactured by Nippon Waters Co., Ltd., using polymethyl methacrylate as a standard, a column temperature of 40 ° C., and a hexafluoroisopropanol solvent.
- tin (II) 2-ethylhexanoate manufactured by Wako Pure Chemical Industries, Ltd.
- P-TSA sulfur acid
- p-toluenesulfonic acid manufactured by Wako Pure Chemical Industries, Ltd.
- Example 1 40 parts by mass of 4032D, 60 parts by mass of PEG6000S and 0.5 parts by mass of Mg chloride were added to a test tube equipped with a stirrer and stirred at 200 ° C. in a nitrogen atmosphere at a pressure of 1.0 ⁇ 10 5 Pa. The sample A was melted for 4 hours, cooled and solidified. The obtained sample A was subjected to lactide content, mass average molecular weight, and DSC measurement.
- sample A 30 parts by mass of sample A, 20 parts by mass of 4032D, and 50 parts by mass of 4060D were weighed and added to a test tube equipped with a stirrer, and stirred at 240 ° C. in a nitrogen atmosphere at a pressure of 1.0 ⁇ 10 5 Pa.
- the sample B was melted for 1 hour, cooled and solidified.
- the obtained sample B was pulverized, dried in a vacuum oven under reduced pressure at 50 ° C. for 7 hours, and pressurized at 220 ° C. to obtain an isotropic press sheet having a thickness of 200 ⁇ m.
- the elastic modulus and hot water extraction rate of the obtained press sheet were measured.
- Example 2 and Comparative Example 1 samples were obtained in the same manner as in Example 1 except that the composition and melting temperature of the raw materials charged into the test tube were changed as shown in Tables 1 and 2.
- Comparative Examples 2 to 3 the composition and melting temperature of the raw material charged into the test tube were changed as shown in Table 2, and when obtaining Sample A, the air pressure in the test tube was changed to 1.0 ⁇ using a vacuum pump. A sample was obtained in the same manner as in Example 1 except that 10 3 Pa was used.
- sample A 30 parts by mass of sample A, 20 parts by mass of 4032D, and 50 parts by mass of 4060D were weighed and added to a test tube equipped with a stirrer, and stirred at 240 ° C. in a nitrogen atmosphere at a pressure of 1.0 ⁇ 10 5 Pa.
- the sample B was melted for 1 hour, cooled and solidified.
- the obtained sample B was pulverized, dried in a vacuum oven under reduced pressure at 50 ° C. for 7 hours, and pressurized at 220 ° C. to obtain an isotropic press sheet having a thickness of 200 ⁇ m.
- the elastic modulus and hot water extraction rate of the obtained press sheet were measured.
- Table 1 and Table 2 show the physical properties of the obtained samples.
- 4032 parts of 4032D, 60 parts by weight of PEG6000S, and 0.5 parts by weight of Mg chloride are weighed and blended, put into the twin screw extruder 1 and melted and kneaded at a screw speed of 200 rpm and a feed rate of 10 kg / h. did.
- the vent hole which exists in the point of L / D 20 measured from the screw front-end
- tip of the twin-screw extruder 1 was made into the open state.
- the atmospheric pressure at the point was 1.0 ⁇ 10 5 Pa.
- 67 parts by mass of 4032D and 167 parts by mass of 4060D were weighed and blended, and charged into the twin-screw extruder 2 and melted and kneaded at a screw rotational speed of 200 rpm and a feed amount of 23.3 kg / h.
- sample C was obtained by cooling and solidifying the resin discharged from the die of the twin screw extruder 2. The obtained sample C was pulverized, dried in a vacuum oven under reduced pressure at 50 ° C. for 7 hours, and pressurized at 220 ° C. to obtain an isotropic press sheet having a thickness of 200 ⁇ m. The elastic modulus and hot water extraction rate of the obtained press sheet were measured.
- Example 12 and Comparative Example 9 samples were obtained in the same manner as in Example 11 except that the composition of the raw materials charged into the twin screw extruders 1 and 2 was changed as shown in Table 3. The physical properties of the obtained sample are shown in Table 3.
- 4032D, 40 parts by weight of PEG6000S, 60 parts by weight of PEG6000S, and 0.5 parts by weight of Mg chloride are weighed and blended, put into the main hopper of a twin screw extruder and melted at a screw speed of 200 rpm and a feed rate of 10 kg / h. -Kneaded.
- the vent hole which exists in the point of L / D 20 measured from the screw front-end
- tip of the twin-screw extruder 1 was made into the open state.
- the atmospheric pressure at the point was 1.0 ⁇ 10 5 Pa.
- the sample A was melted and kneaded at a screw speed of 50 rpm and a feed rate of 10 kg / h, discharged from the die, cooled and solidified to obtain sample A.
- the temperature setting of GT-40 was 80 ° C. at the bottom of the hopper and 200 ° C. thereafter.
- the vent hole in the middle was opened.
- the atmospheric pressure at the point was 1.0 ⁇ 10 5 Pa.
- the obtained sample A was subjected to lactide content, mass average molecular weight, and DSC measurement.
- sample A 30 parts by mass of sample A, 20 parts by mass of 4032D, and 50 parts by mass of 4060D were weighed and added to a test tube equipped with a stirrer, and stirred at 240 ° C. in a nitrogen atmosphere at a pressure of 1.0 ⁇ 10 5 Pa.
- the sample B was melted for 1 hour, cooled and solidified.
- the obtained sample B was pulverized, dried in a vacuum oven under reduced pressure at 50 ° C. for 7 hours, and pressurized at 220 ° C. to obtain an isotropic press sheet having a thickness of 200 ⁇ m.
- the elastic modulus and hot water extraction rate of the obtained press sheet were measured.
- Comparative Example 12 a sample was obtained in the same manner as in Example 16 except that the composition of the raw material charged into GT-40 was changed as shown in Table 5.
- Comparative Example 13 a sample was obtained in the same manner as in Example 16 except that the vent hole of GT-40 was connected to a vacuum pump and the atmospheric pressure at the point was set to 3.0 ⁇ 10 3 Pa.
- Table 5 shows the physical properties of the obtained sample.
- a block copolymer with little residual lactide can be obtained.
- the block copolymer obtained by the present invention can be used as a flexible resin for molded articles such as films, alone or mixed with a polylactic acid resin, and a plasticizer having bleed-out resistance for a polylactic acid resin. Can also be suitably used.
Landscapes
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Biological Depolymerization Polymers (AREA)
- Polyesters Or Polycarbonates (AREA)
- Other Resins Obtained By Reactions Not Involving Carbon-To-Carbon Unsaturated Bonds (AREA)
Abstract
Description
(1) ポリ乳酸系樹脂、分子内に少なくとも一つの水酸基を有する樹脂(以下、分子内に少なくとも一つの水酸基を有する樹脂を、樹脂(A)という)、及びエステル交換触媒を、常圧にて溶融すること(以下、常圧にて溶融することを、常圧・溶融工程という)を特徴とする、ポリ乳酸系樹脂と樹脂(A)とのブロック共重合体(以下、ポリ乳酸系樹脂と樹脂(A)とのブロック共重合体を、ブロック共重合体という)の製造方法。
(2)
前記常圧・溶融工程が、二軸押出機(以下、該二軸押出機を、二軸押出機1という)内にて行われることを特徴とする、(1)に記載のブロック共重合体の製造方法。
(3)
前記樹脂(A)が、ポリアルキレングリコール樹脂であることを特徴とする、(1)または(2)に記載のブロック共重合体の製造方法。
(4)
前記エステル交換触媒が、金属の有機酸塩および/または金属のハロゲン化物塩であることを特徴とする、(1)~(3)のいずれかに記載のブロック共重合体の製造方法。
(5)
(2)に記載の方法により製造したブロック共重合体を、二軸押出機1内から別の二軸押出機内に直接導入して、ポリ乳酸系樹脂と混合することを特徴とする、ポリ乳酸系樹脂とブロック共重合体の混合物の製造方法。
(6)
(2)に記載の方法により製造したブロック共重合体に対して、該ブロック共重合体を製造したのと同一の二軸押出機のサイドフィーダーからポリ乳酸系樹脂を投入することで、該ブロック共重合体を製造したのと同一の二軸押出機内で該ブロック共重合体とポリ乳酸系樹脂を混合することを特徴とする、ポリ乳酸系樹脂とブロック共重合体の混合物の製造方法。
本発明では、ブロック共重合体の製造原料としてポリ乳酸系樹脂を使用する。ポリ乳酸系樹脂とは、L-乳酸ユニットおよび/またはD-乳酸ユニットを主たる構成成分とする重合体である。ここで、主たる構成成分とは、重合体中の単量体ユニット全体100mol%中において乳酸ユニットの割合が最大であることを意味し、好ましくは全単量体ユニット100mol%中、乳酸ユニットが70~100mol%である。
本発明では、ブロック共重合体の製造原料として樹脂(A)を使用する。本発明では、ポリ乳酸系樹脂中の乳酸ユニット-乳酸ユニット間のエステル結合に対して、樹脂(A)の水酸基を起点にエステル交換反応を進行させるため、樹脂(A)は分子内に少なくとも一つの水酸基を有する樹脂であることが重要である。但し、樹脂(A)は、ポリ乳酸系樹脂以外の分子内に少なくとも一つの水酸基を有する樹脂である。なお、樹脂(A)は用途によっては生分解性を有する樹脂を選択することが好ましい。
本発明は、ポリ乳酸系樹脂、樹脂(A)、及びエステル交換触媒を、常圧にて溶融することが重要である。つまり本発明では、ブロック共重合体の製造をエステル交換法にて行うが、その際にエステル交換触媒を使用することが重要となる。
本発明のブロック共重合体の製造方法は、原料であるポリ乳酸系樹脂、樹脂(A)、およびエステル交換触媒を反応器に供給し、常圧にて溶融する(常圧・溶融工程を経る)ことを特徴とする。
本発明で得られるブロック共重合体は、ポリ乳酸系樹脂と併用することができる。この場合のブロック共重合体は、ポリ乳酸系樹脂の可塑剤として機能することも可能となる。このように本発明で得られるブロック共重合体をポリ乳酸系樹脂の可塑剤として使用する場合、ポリ乳酸系樹脂中にブロック共重合体を分散させるためには、ポリ乳酸系樹脂とブロック共重合体とを溶融混練してもよいし、クロロホルム等の良溶媒中にポリ乳酸系樹脂とブロック共重合体とを溶解させ、溶媒を揮発または貧溶媒中に樹脂を析出させてもよい。
[測定および評価方法]
実施例中に示す測定や評価は次に示すとおりの条件で行った。
(株)オリエンテック製TENSILON UCT-100を用いて応力-歪み測定を行い、応力-歪み曲線の最初の直線部分を用いて、直線上の2点間の応力差を同じ2点間の歪み差で除し、引張弾性率を計算した。具体的には、ブレスシートから長さ150mm、幅10mmの短冊状サンプルを切り出し、初期引張チャック間距離50mm、引張速度200mm/分で、JIS K 7127(1999)に規定された方法に従って測定を行った。また、測定は5回行い、その平均値を算出した。
生成したサンプルを塩化メチレンに溶解し、1g/20mlに濃度調整した後にアセトン60mlを追加し、さらに超音波攪拌しながらシクロヘキサン320mlを滴下することによりポリマー成分を析出させた。析出物を遠心分離および孔径0.45μmのPTFEフィルターにより除去し、試料液を作製した。この試料液を、ガスクロマトグラフGC-17A(島津製作所社製)を用いて、カラム:DB-17MS型(J&W社製)、カラム温度:80~250℃、10℃/分、キャリアーガス:Heの条件にて分析を行った。また、あらかじめ濃度を変更したラクチド単体の試料液を用いて検量線を作成し、この検量線を利用して試料のラクチド量(質量%)を求めた。
耐ブリードアウト性の指標として熱水抽出率を測定した。あらかじめ、温度23℃、湿度65%RHの雰囲気下で1日以上調湿したプレスシートについて、処理前の質量を測定した。次に、1気圧下で沸騰した蒸留水中にシートを1時間浸漬処理し、再度処理前と同様の条件で調湿した後に、処理後の質量を測定した。そして、下記の式により熱水抽出率を算出した。
熱水抽出率(質量%)=(処理前の質量-処理後の質量)×100/処理前の質量
(4)GPC
質量平均分子量は、ゲルパーミエーションクロマトグラフィー(GPC)により測定を行い、ポリメチルメタクリレート換算法により計算した。なお、質量平均分子量の計算は、得られたサンプルの溶出曲線中に高分子由来のピークが一つのみ存在する(単峰性)場合のみ行い、ポリ乳酸系樹脂および樹脂(A)に由来する二つの高分子由来のピークを有する(二峰性)場合、またはそれ以上の高分子由来のピークを有する場合には行わなかった。GPCの測定はWaters社製2695型を用いて行い、検出器にWATERS社示差屈折計2414 型を用い、ポンプにWATERS社MODEL510を用い、カラムにShodex HFIP-806Mを2本直列に接続したものを用いて行った。測定条件は、流速0.5mL/min、カラム温度40℃とし、溶媒に5mMトリフルオロ酢酸ナトリウム添加のヘキサフルオロイソプロパノールを用い、試料濃度0.1質量%の溶液を0.2mL注入した。
セイコーインスツル(株)製示差走査熱量計RDC220を用い、生成したサンプル5mgをアルミニウム製受皿にセットし、25℃から昇温速度20℃/分で220℃まで昇温、220℃のまま5分間溶融保持したのち、25℃まで急冷した。そして、その昇温過程についてのチャートから、樹脂(A)セグメントに由来する融解ピーク温度TmA(℃)を読み取った。また、未反応の樹脂(A)をサンプルとして、上記と同様の方法により樹脂(A)の融解ピーク温度TmA0(℃)を求め、TmA0-TmAを算出した。
(4032D)
ポリL-乳酸、Natureworks製“4032D”、質量平均分子量200,000、D体含有量1.4mol%、融点166℃。予め真空オーブン中で減圧しながら100℃、5時間の条件にて乾燥したものを使用した。
ポリL-乳酸、Natureworks製“4060D”、質量平均分子量200,000、D体含有量12.0mol%、融点なし。予め真空オーブン中で減圧しながら50℃、7時間の条件にて乾燥したものを使用した。
(PEG6000S)
ポリエチレングリコール、三洋化成工業製“PEG6000S”、質量平均分子量8,000、TmA0は64.0℃。予め真空オーブン中で減圧しながら30℃、7時間の条件にて乾燥したものを使用した。
ポリブチレンアジペート・テレフタレート、BASF製“Ecoflex F Blend C1200” 、質量平均分子量60,000、TmA0は120.2℃。予め真空オーブン中で減圧しながら80℃、7時間の条件にて乾燥したものを使用した。
(酢酸Mg)
金属塩(金属の有機酸塩)として、酢酸マグネシウム四水和物(和光純薬工業製)を用いた。
金属塩(金属のハロゲン化物塩)として、塩化マグネシウム六水和物(和光純薬工業製)を用いた。
金属塩(金属の有機酸塩)として、2-エチルヘキサン酸スズ(II)(和光純薬工業製)を用いた。
硫黄酸として、p-トルエンスルホン酸(和光純薬工業製)を用いた。
4032Dを40質量部、PEG6000Sを60質量部、塩化Mgを0.5質量部秤量して攪拌装置付きの試験管に加え、気圧1.0×105Paの窒素雰囲気中において攪拌しながら200℃で4時間溶融し、冷却・固化してサンプルAを得た。得られたサンプルAのラクチド量、質量平均分子量、およびDSC測定を行った。
4032Dを40質量部、PEG6000Sを60質量部、塩化Mgを0.5質量部秤量してブレンドし、日本製鋼所製二軸押出機TEX30α(L/D=35、スクリュー径=30mm)に投入してスクリュー回転数200rpm、フィード量10kg/hにて溶融・混練を行い、口金から吐出させて冷却・固化してサンプルAを得た。なお、TEX30αの温度設定はホッパー下部から第一混練部の手前(スクリュー先端から計測してL/D=25の地点)までを80℃、第一混練部以降を200℃とした。また、スクリュー先端から計測してL/D=20の地点に存在するベント孔は開放状態とした。該地点における気圧は1.0×105Paであった。得られたサンプルAのラクチド量、質量平均分子量、およびDSC測定を行った。
二軸押出機1として日本製鋼所製TEX30α(L/D=35、スクリュー径=30mm)、二軸押出機2として日本製鋼所製TEX44α(L/D=38、スクリュー径=44mm)を使用し、二軸押出機1から吐出された樹脂が二軸押出機2の途中(スクリュー先端から計測してL/D=18の地点)にサイドフィードされるように装置を構成した。
得られたサンプルの物性を表3に示した。
二軸押出機として日本製鋼所製TEX30α(L/D=35、スクリュー径=30mm)を使用し、二軸押出機の途中(スクリュー先端から計測してL/D=18の地点)にサイドフィーダーを設置した。
得られたサンプルの物性を表4に示した。
4032Dを40質量部、PEG6000Sを60質量部、塩化Mgを0.5質量部秤量してブレンドし、プラスチック工学研究所製単軸押出機GT-40(L/D=28、スクリュー径=40mm)に投入してスクリュー回転数50rpm、フィード量10kg/hにて溶融・混練を行い、口金から吐出させて冷却・固化してサンプルAを得た。なお、GT-40の温度設定はホッパー下部を80℃、以降を200℃とした。また、途中のベント孔は開放状態とした。該地点における気圧は1.0×105Paであった。得られたサンプルAのラクチド量、質量平均分子量、およびDSC測定を行った。
Claims (6)
- ポリ乳酸系樹脂、分子内に少なくとも一つの水酸基を有する樹脂(以下、分子内に少なくとも一つの水酸基を有する樹脂を、樹脂(A)という)、及びエステル交換触媒を、常圧にて溶融すること(以下、常圧にて溶融することを、常圧・溶融工程という)を特徴とする、ポリ乳酸系樹脂と樹脂(A)とのブロック共重合体(以下、ポリ乳酸系樹脂と樹脂(A)とのブロック共重合体を、ブロック共重合体という)の製造方法。
- 前記常圧・溶融工程が、二軸押出機(以下、該二軸押出機を、二軸押出機1という)内にて行われることを特徴とする、請求項1に記載のブロック共重合体の製造方法。
- 前記樹脂(A)が、ポリアルキレングリコール樹脂であることを特徴とする、請求項1または2に記載のブロック共重合体の製造方法。
- 前記エステル交換触媒が、金属の有機酸塩および/または金属のハロゲン化物塩であることを特徴とする、請求項1~3のいずれかに記載のブロック共重合体の製造方法。
- 請求項2に記載の方法により製造したブロック共重合体を、二軸押出機1内から別の二軸押出機内に直接導入して、ポリ乳酸系樹脂と混合することを特徴とする、ポリ乳酸系樹脂とブロック共重合体の混合物の製造方法。
- 請求項2に記載の方法により製造したブロック共重合体に対して、該ブロック共重合体を製造したのと同一の二軸押出機のサイドフィーダーからポリ乳酸系樹脂を投入することで、該ブロック共重合体を製造したのと同一の二軸押出機内で該ブロック共重合体とポリ乳酸系樹脂を混合することを特徴とする、ポリ乳酸系樹脂とブロック共重合体の混合物の製造方法。
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN201380046383.XA CN104619745B (zh) | 2012-09-24 | 2013-07-31 | 嵌段共聚物的制造方法 |
KR1020157005412A KR20150063367A (ko) | 2012-09-24 | 2013-07-31 | 블록 공중합체의 제조 방법 |
JP2013535192A JP6119608B2 (ja) | 2012-09-24 | 2013-07-31 | ブロック共重合体の製造方法 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2012209177 | 2012-09-24 | ||
JP2012-209177 | 2012-09-24 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2014045717A1 true WO2014045717A1 (ja) | 2014-03-27 |
Family
ID=50341043
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2013/070753 WO2014045717A1 (ja) | 2012-09-24 | 2013-07-31 | ブロック共重合体の製造方法 |
Country Status (3)
Country | Link |
---|---|
JP (1) | JP6119608B2 (ja) |
KR (1) | KR20150063367A (ja) |
WO (1) | WO2014045717A1 (ja) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN112469766A (zh) * | 2019-03-26 | 2021-03-09 | 株式会社Lg化学 | 三嵌段共聚物及其制备方法 |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
KR102241367B1 (ko) | 2018-01-05 | 2021-04-15 | 주식회사 엘지화학 | 블록 공중합체 |
WO2020197148A1 (ko) * | 2019-03-26 | 2020-10-01 | 주식회사 엘지화학 | 트리블록 공중합체 및 이의 제조 방법 |
KR102494714B1 (ko) * | 2020-04-08 | 2023-02-06 | 재단법인대구경북과학기술원 | 생분해성 고분자 조성물의 제조방법 및 이로부터 제조되는 생분해성 필름 |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2002516910A (ja) * | 1997-10-03 | 2002-06-11 | マクロメド・インコーポレーテッド | 逆熱的ゲル化特性を有する生分解性低分子量トリブロックポリ(ラクチド−co−グリコリド)−ポリエチレングリコールコポリマー |
JP2003040990A (ja) * | 2001-07-31 | 2003-02-13 | Dainippon Ink & Chem Inc | ポリヒドロキシカルボン酸系共重合体の製造方法 |
JP2004231773A (ja) * | 2003-01-30 | 2004-08-19 | Dainippon Ink & Chem Inc | ポリ乳酸共重合体の製造方法 |
JP2004250663A (ja) * | 2002-08-21 | 2004-09-09 | Dainippon Ink & Chem Inc | 成形用樹脂及びその製造方法 |
JP2010202768A (ja) * | 2009-03-03 | 2010-09-16 | Nihon Univ | オリゴオレフィン−ポリエステル系又はポリカーボネート系ブロック共重合体 |
-
2013
- 2013-07-31 JP JP2013535192A patent/JP6119608B2/ja active Active
- 2013-07-31 KR KR1020157005412A patent/KR20150063367A/ko not_active Application Discontinuation
- 2013-07-31 WO PCT/JP2013/070753 patent/WO2014045717A1/ja active Application Filing
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2002516910A (ja) * | 1997-10-03 | 2002-06-11 | マクロメド・インコーポレーテッド | 逆熱的ゲル化特性を有する生分解性低分子量トリブロックポリ(ラクチド−co−グリコリド)−ポリエチレングリコールコポリマー |
JP2003040990A (ja) * | 2001-07-31 | 2003-02-13 | Dainippon Ink & Chem Inc | ポリヒドロキシカルボン酸系共重合体の製造方法 |
JP2004250663A (ja) * | 2002-08-21 | 2004-09-09 | Dainippon Ink & Chem Inc | 成形用樹脂及びその製造方法 |
JP2004231773A (ja) * | 2003-01-30 | 2004-08-19 | Dainippon Ink & Chem Inc | ポリ乳酸共重合体の製造方法 |
JP2010202768A (ja) * | 2009-03-03 | 2010-09-16 | Nihon Univ | オリゴオレフィン−ポリエステル系又はポリカーボネート系ブロック共重合体 |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN112469766A (zh) * | 2019-03-26 | 2021-03-09 | 株式会社Lg化学 | 三嵌段共聚物及其制备方法 |
CN112469766B (zh) * | 2019-03-26 | 2022-12-06 | 株式会社Lg化学 | 三嵌段共聚物及其制备方法 |
Also Published As
Publication number | Publication date |
---|---|
KR20150063367A (ko) | 2015-06-09 |
JP6119608B2 (ja) | 2017-04-26 |
JPWO2014045717A1 (ja) | 2016-08-18 |
CN104619745A (zh) | 2015-05-13 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
Anderson et al. | Toughening polylactide | |
JP5867084B2 (ja) | ポリ乳酸系フィルム | |
JP5620061B2 (ja) | ポリ乳酸ブロック共重合体の製造方法 | |
Spinella et al. | Polylactide/poly (ω-hydroxytetradecanoic acid) reactive blending: A green renewable approach to improving polylactide properties | |
WO2008004490A1 (fr) | Composition de polyester aliphatique et son procédé de fabrication | |
JP5867406B2 (ja) | 生分解性フィルム | |
JPWO2013038770A1 (ja) | フィルム | |
JP5207274B2 (ja) | 生分解性樹脂組成物 | |
JP2008174691A (ja) | 芳香族ポリエステル系樹脂組成物およびその製造方法 | |
JP6119608B2 (ja) | ブロック共重合体の製造方法 | |
JP5250178B2 (ja) | ステレオコンプレックスポリ乳酸、その製造方法、組成物および成形品 | |
JP2008239645A (ja) | ポリ乳酸系樹脂組成物及びその製造方法、並びに成形品 | |
JPWO2008120821A1 (ja) | ポリ乳酸組成物 | |
JP4493993B2 (ja) | 生分解性ポリエステル樹脂組成物、成形物及び農業用マルチフィルム | |
JP2010150385A (ja) | ポリ乳酸樹脂組成物 | |
JP5033396B2 (ja) | ポリ乳酸組成物 | |
JP5129950B2 (ja) | ステレオコンプレックスポリ乳酸組成物 | |
JP5129945B2 (ja) | ステレオコンプレックスポリ乳酸組成物 | |
JP5424262B2 (ja) | ヒドロキシカルボン酸重合体 | |
JP5341478B2 (ja) | ポリ乳酸系樹脂成形品の製造方法 | |
CN104619745B (zh) | 嵌段共聚物的制造方法 | |
JP2013159747A (ja) | ポリ乳酸系フィルム | |
JP5007032B2 (ja) | ステレオコンプレックスポリ乳酸組成物 | |
JP5129944B2 (ja) | ポリ乳酸組成物 | |
JPH09296102A (ja) | 生分解性乳酸系ポリマー組成物 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
ENP | Entry into the national phase |
Ref document number: 2013535192 Country of ref document: JP Kind code of ref document: A |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 13839405 Country of ref document: EP Kind code of ref document: A1 |
|
ENP | Entry into the national phase |
Ref document number: 20157005412 Country of ref document: KR Kind code of ref document: A |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
122 | Ep: pct application non-entry in european phase |
Ref document number: 13839405 Country of ref document: EP Kind code of ref document: A1 |