WO2012032876A1 - ポリエステル組成物の製造方法 - Google Patents
ポリエステル組成物の製造方法 Download PDFInfo
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- WO2012032876A1 WO2012032876A1 PCT/JP2011/067436 JP2011067436W WO2012032876A1 WO 2012032876 A1 WO2012032876 A1 WO 2012032876A1 JP 2011067436 W JP2011067436 W JP 2011067436W WO 2012032876 A1 WO2012032876 A1 WO 2012032876A1
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/78—Preparation processes
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/02—Polyesters derived from hydroxycarboxylic acids or from polycarboxylic acids and polyhydroxy compounds
- C08G63/12—Polyesters derived from hydroxycarboxylic acids or from polycarboxylic acids and polyhydroxy compounds derived from polycarboxylic acids and polyhydroxy compounds
- C08G63/16—Dicarboxylic acids and dihydroxy compounds
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/02—Polyesters derived from hydroxycarboxylic acids or from polycarboxylic acids and polyhydroxy compounds
- C08G63/12—Polyesters derived from hydroxycarboxylic acids or from polycarboxylic acids and polyhydroxy compounds derived from polycarboxylic acids and polyhydroxy compounds
- C08G63/16—Dicarboxylic acids and dihydroxy compounds
- C08G63/20—Polyesters having been prepared in the presence of compounds having one reactive group or more than two reactive groups
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/78—Preparation processes
- C08G63/80—Solid-state polycondensation
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08K—Use of inorganic or non-macromolecular organic substances as compounding ingredients
- C08K3/00—Use of inorganic substances as compounding ingredients
- C08K3/32—Phosphorus-containing compounds
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08K—Use of inorganic or non-macromolecular organic substances as compounding ingredients
- C08K5/00—Use of organic ingredients
- C08K5/0008—Organic ingredients according to more than one of the "one dot" groups of C08K5/01 - C08K5/59
- C08K5/0066—Flame-proofing or flame-retarding additives
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
- C08L67/00—Compositions of polyesters obtained by reactions forming a carboxylic ester link in the main chain; Compositions of derivatives of such polymers
- C08L67/02—Polyesters derived from dicarboxylic acids and dihydroxy compounds
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08K—Use of inorganic or non-macromolecular organic substances as compounding ingredients
- C08K3/00—Use of inorganic substances as compounding ingredients
- C08K3/32—Phosphorus-containing compounds
- C08K2003/321—Phosphates
- C08K2003/324—Alkali metal phosphate
Definitions
- the present invention relates to a method for producing a polyester composition having good hydrolysis resistance.
- Polyester is excellent in mechanical properties, thermal properties, chemical resistance, electrical properties, and moldability and is used in various applications.
- Patent Document 1 describes a method for producing a polyester containing an alkali metal or alkaline earth metal phosphate.
- Patent Document 2 describes a method for producing a polyester containing an inorganic phosphate, and is used in combination with phosphoric acid in the examples.
- Patent Document 3 describes polyethylene terephthalate containing buffered phosphorus, and is used in combination with a phosphorus compound in the examples.
- a method of polycondensation through an esterification reaction using a dicarboxylic acid as a main raw material (a direct polycondensation method) and a method of performing polycondensation through a transesterification reaction using a dicarboxylic acid ester as a main raw material ( DMT method).
- the DMT method has good dispersibility of particle components and is excellent in terms of suppressing foreign matters, but has a problem that the raw material cost is higher than that of the direct weight method.
- the direct weight method it is possible to carry out the esterification reaction without a catalyst, and since the raw material is inexpensive, it is very excellent in terms of cost. Is higher than that of the DMT method, resulting in a problem that hydrolysis resistance is lowered.
- An object of the present invention is to solve the above-mentioned problems of the prior art and to provide a method for producing a polyester composition suitable for film use having excellent hydrolysis resistance.
- an object of the present invention is to provide a polyester production method in which a dicarboxylic acid component and a diol component are esterified and then a polycondensation reaction, and the diol component is added two or more times between the end of the esterification reaction and the start of the polycondensation reaction.
- This can be solved by a method for producing a polyester composition in which an alkali metal phosphate is added in a state where the amount of COOH end groups of the esterification reaction product is 150 eq / ton or less.
- polyester production method of the present invention it is possible to provide a polyester composition that can control the amount of COOH end groups of the polyester composition and is excellent in hydrolysis resistance.
- the method for producing a polyester composition of the present invention is a polyester production method in which a dicarboxylic acid component and a diol component are esterified and then a polycondensation reaction is performed. It is necessary to add the alkali metal phosphate in a state where the amount of COOH end groups of the esterification reaction product is 150 eq / ton or less.
- dicarboxylic acid component in the present invention various dicarboxylic acid components such as aromatic dicarboxylic acid, chain aliphatic dicarboxylic acid, and alicyclic dicarboxylic acid can be used.
- aromatic dicarboxylic acids are preferred from the viewpoints of mechanical properties, heat resistance, and heat and humidity resistance of the polyester composition.
- terephthalic acid, isophthalic acid, and naphthalenedicarboxylic acid are preferable from the viewpoint of polymerizability and mechanical properties.
- diols can be used as the diol component in the present invention.
- aliphatic diols such as ethylene glycol, 1,2-propanediol, 1,3-propanediol, butanediol, 2-methyl-1,3-propanediol, hexanediol, neopentylglycol
- alicyclic diols Is cyclohexanedimethanol, cyclohexanediethanol, decahydronaphthalene diethanol, decahydronaphthalene diethanol, norbornane dimethanol, norbornane dimethanol, tricyclodecane dimethanol, tricyclodecane ethanol, tetracyclododecane dimethanol, tetracyclododecane diethanol, decalin di Saturated alicyclic primary diols such as methanol and decalindiethanol, 2,6-dihydroxy-9-oxabi
- a diol having a boiling point of 230 ° C. or lower is preferable because it is easily distilled out of the reaction system, and an aliphatic diol is more preferable because of low cost and high reactivity.
- ethylene glycol is particularly preferable from the viewpoint of mechanical properties.
- a method of preliminarily storing an esterification reaction product and adding a slurry of a dicarboxylic acid and a diol to start the esterification reaction It is selected from the viewpoint of improving the handling properties of dicarboxylic acids that are hardly soluble in diols and shortening the reaction time.
- the esterification reaction proceeds without storing the esterification reaction product, a pressurization facility or a catalyst may be required. Also in the present invention, it is desirable to carry out the esterification reaction using the stored esterification reaction product.
- the dicarboxylic acid component and diol component before the start of the esterification reaction is preferably in the range of 1.05 to 1.40.
- the esterification reaction proceeds efficiently, the time cycle can be shortened, and the dimer by-product of the diol component is few, and the heat resistance is maintained. More preferably, they are 1.05 or more and 1.30 or less, More preferably, they are 1.05 or more and 1.20 or less.
- an alkali metal salt, a titanium compound, an ammonium salt or the like may be used as a catalyst.
- thermal decomposition or generation of foreign matters may occur in the polycondensation reaction stage. Therefore, the esterification reaction is preferably carried out without a catalyst. The esterification reaction proceeds sufficiently even in the absence of a catalyst by autocatalysis by the COOH end group.
- the diol component twice or more to the esterification reaction product after the esterification reaction.
- a diol component By adding a diol component to the esterification reaction product, the amount of the COOH end group of the esterification reaction product is controlled, the amount of the COOH end group of the polyester composition after the polycondensation reaction is reduced, and hydrolysis resistance is improved. ing.
- an alkali metal phosphate before the polycondensation reaction, an increase in COOH end groups is suppressed and high hydrolysis resistance is imparted.
- the diol component between the end of the esterification reaction and the start of the polycondensation reaction.
- the diol component When the diol component is added during the polycondensation reaction, it does not efficiently react with the COOH end groups of the esterification reaction product, and thus the effect of reducing the amount of COOH end groups of the finally obtained polyester composition is lowered.
- the esterification reaction using a dicarboxylic acid component and a diol component it is preferably added after the esterification reaction rate reaches 90% or more and until the intrinsic viscosity reaches 0.3.
- the diol When the diol is added under these preferable conditions, the by-production of the diol component dimer is suppressed, heat resistance can be maintained, and the unreacted terephthalic acid hardly remains, so that the amount of COOH end groups increases. It is difficult to keep hydrolysis resistance.
- the diol component needs to be added twice or more.
- the amount of COOH end groups of the esterification reaction product can be efficiently reduced, and the time cycle extended by the addition can be minimized. Further, by minimizing the extension of the time cycle, it can be made 1.3% by weight or less based on the polyester composition from which the dimer content of the diol component can be obtained.
- the diol component is added to the esterification reaction product at a time, the temperature in the reaction system is drastically lowered, and there is a concern about stirring troubles and time cycle delay due to solidification of the esterification reaction product.
- the number of additions is preferably 10 times or less, more preferably 5 times or less. When the number of additions is less than this preferable number, the reduction effect of the COOH end group amount can be maintained without lowering the production efficiency.
- the lower limit of the temperature in the reaction system is preferably 210 ° C. or higher, more preferably 220 ° C. or higher.
- the upper limit of the reaction system temperature is preferably 260 ° C. or less, more preferably 250 ° C. or less.
- the second and subsequent additions of the diol component are preferably performed after the temperature in the reaction system has returned to 230 ° C or higher, more preferably 235 ° C or higher.
- the amount of the diol component added after the esterification reaction is 0.15 to 0.5 times the total dicarboxylic acid component per addition, and the production efficiency and heat resistance are It is preferable from the point, More preferably, it is 0.15-fold mol or more and 0.3-fold mol or less.
- the addition amount per time within this range, the COOH end group of the esterification reaction product can be effectively reduced without impairing the heat resistance, and a polyester composition having good hydrolysis resistance can be obtained. Can be obtained. Moreover, you may change the addition amount for every addition.
- the lower limit of the total amount of the diol component to be added is preferably 0.3 times mol or more, more preferably 0.4 times mol or more, further preferably 0.5 times mol or more with respect to the total dicarboxylic acid component. .
- an upper limit is 1.5 times mole or less, More preferably, it is 1.0 times mole or less, More preferably, it is 0.9 times mole or less.
- the dimer content of the diol component should be 1.3% by weight or less based on the polyester composition. it can.
- the metal compound in the present invention is preferably a metal salt, specifically, a metal chloride salt, a metal acetate metal salt, a metal carbonate salt, etc., among which sodium acetate, calcium acetate, magnesium acetate, manganese acetate, cobalt acetate, acetic acid Metal acetates such as zinc and tin acetate are preferred.
- the lower limit of the addition amount is preferably 1.0 mol / ton or more, more preferably 2.0 mol / ton or more, as a concentration with respect to the obtained polyester composition.
- the upper limit of the addition amount is preferably 3.5 mol / ton or less from the viewpoint of hydrolysis resistance, and more preferably 3.0 mol / ton or less.
- the reactivity of the COOH end of the esterification reaction product and the diol component can be improved, the COOH end can be efficiently reduced, and the polyester composition has good hydrolysis resistance. You can get things.
- the amount of COOH end groups of the resulting polyester composition can be 20 eq / ton or less, A polyester composition having high hydrolysis resistance can be obtained.
- the amount of COOH end groups of the esterification reaction product when adding the alkali metal phosphate is more than 150 eq / ton, the amount of COOH end groups of the resulting polyester composition increases, and sufficient hydrolysis resistance cannot be obtained.
- the lower limit is preferably 10 eq / ton.
- the amount of COOH end groups is 10 eq / ton or more, it is not necessary to add a large amount of diol component over a long period of time, and it is possible to suppress a decrease in heat resistance due to by-production of a dimer of the diol component.
- the diol component may be further added after adding the alkali metal phosphate.
- the alkali metal phosphate in the present invention is not particularly limited, but sodium dihydrogen phosphate, disodium hydrogen phosphate, trisodium phosphate, potassium dihydrogen phosphate, dipotassium hydrogen phosphate, tripotassium phosphate, Examples include lithium dihydrogen phosphate, dilithium hydrogen phosphate, and trilithium phosphate. Among these, sodium dihydrogen phosphate and potassium dihydrogen phosphate are preferable from the viewpoint of hydrolysis resistance.
- the lower limit of the addition amount of the alkali metal phosphate is preferably 0.1 mol / ton or more, more preferably 0.4 mol / ton or more as a concentration with respect to the polyester composition obtained from the viewpoint of hydrolysis resistance.
- the upper limit of the amount added is preferably 7.0 mol / ton or less, more preferably 4.0 mol / ton or less, and still more preferably 2.0 mol / ton or less, from the viewpoints of foreign matter suppression and hydrolysis resistance.
- the alkali metal phosphate As a method for adding the alkali metal phosphate, it is preferable from the viewpoint of hydrolysis resistance that it is previously mixed with a diol component and a phosphorus compound and added. At this time, it is preferable to mix the phosphorus compound in an amount of 0.1-fold mol to 7.5-fold mol with respect to the alkali metal phosphate, more preferably 0.3-fold mol to 5.0-fold mol, more preferably Is 1.0 times mol or more and 2.0 times mol or less. It is possible to control the reaction activity at the time of hydrolysis of the resulting polyester composition by mixing the phosphorus compound in an amount of 0.1 to 7.5 mol with respect to the alkali metal phosphate. A polyester composition having good hydrolyzability can be obtained.
- the lower limit of the addition amount of the phosphorus compound to be mixed with the alkali metal phosphate is preferably 0.1 mol / ton or more as a concentration with respect to the polyester composition obtained from the viewpoint of hydrolysis resistance and heat resistance, more preferably 1.0 mol / ton or more.
- the upper limit of the addition amount is preferably 4.0 mol / ton or less, more preferably 2.5 mol / ton or less, from the viewpoint of hydrolysis resistance.
- a method for adding the alkali metal phosphate it is preferable to add it in advance as a solution or slurry from the viewpoint of suppressing foreign matter.
- a diol compound such as ethylene glycol is preferably used at a concentration of 0.5 wt% or more and 10 wt% or less, more preferably 1 wt% or more and 3 wt% or less.
- the phosphorus compound to be mixed with the alkali metal phosphate is not particularly limited, and examples thereof include phosphoric acid, trimethyl phosphate, trimethyl phosphonoacetate, and dimethyl phenylphosphonate. Among these, phosphoric acid is preferable from the viewpoint of hydrolysis resistance.
- the polymerization catalyst used in the method for producing the polyester composition of the present invention is not particularly limited, and various catalysts can be used.
- an antimony compound such as antimony trioxide, a germanium compound such as germanium dioxide, a titanium compound such as titanium alkoxide, or a composite oxide of aluminum or silica can be used.
- a trifunctional or higher functional copolymer component in the method for producing a polyester composition of the present invention, it is preferable to add a trifunctional or higher functional copolymer component before the start of the polycondensation reaction.
- the tri- or higher functional copolymer component include trimellitic acid, cyclohexanetricarboxylic acid, biphenyltetracarboxylic acid, pyromellitic acid, butanetetracarboxylic acid, and trimer acid obtained by trimerizing long-chain aliphatic carboxylic acid.
- Polyhydric carboxylic acids and anhydrides and esters thereof glycerin, pentaerythritol, dipentaerythritol, trimethylolpropane, ditrimethylolpropane, trihydroxybenzenecarboxylic acid, trihydroxybenzenecarboxylic acid and other polyhydric alcohols, citric acid dihydroxybenzenecarboxylic acid and Examples thereof include polyvalent hydroxycarboxylic acids such as dihydroxynaphthalenecarboxylic acid and anhydrides and esters thereof. In particular, from the viewpoint of film formability, a trifunctional copolymer component is preferable.
- the tri- or higher functional copolymer component it is preferable to add the tri- or higher functional copolymer component until the polycondensation reaction is started, specifically until the intrinsic viscosity reaches 0.3. Since the low molecular weight polyester having an intrinsic viscosity of less than 0.3 has a low viscosity, a trifunctional or higher functional copolymer component can be uniformly reacted. In addition, from the viewpoint of effectively preventing a local reaction from proceeding and causing coarse foreign matters, it is preferable that the addition interval with other additives is 5 minutes or longer.
- the lower limit of the amount of the tri- or higher functional copolymer component added is preferably 0.01 mol% or more, more preferably 0. 0% with respect to the total acid component obtained from the point of hydrolysis resistance after film formation. 05 mol% or more.
- the upper limit of the addition amount is preferably 1.00 mol% or less, more preferably 0.50 mol% or less from the viewpoint of gelation suppression.
- a tri- or higher functional copolymer component As a method for adding a tri- or higher functional copolymer component, it is preferable to add it as an ethylene glycol solution of 0.5% by mass or more and 5% by mass or less from the viewpoint of reactivity and foreign matter suppression.
- ethylene glycol solution By adding it as an ethylene glycol solution in the above range, a tri- or higher functional copolymer component and a polyester low monomer can be reacted uniformly.
- concentration of the tri- or higher functional copolymer component in the ethylene glycol solution is within the above preferred range, the amount of ethylene glycol added to the system is not excessive, the amount of diethylene glycol as a by-product does not increase, and heat resistance In addition, while hydrolysis resistance is maintained, local reactions are unlikely to occur, and coarse foreign matters are hardly generated.
- the temperature in the system is preferably 210 to 260 ° C. so that the esterification reaction product does not solidify.
- 0.27 moles of ethylene glycol is used with respect to terephthalic acid, and a second addition is performed.
- distilling ethylene glycol when the temperature returned to 235 ° C. again, add 0.27 moles of ethylene glycol for the third time and add 0.81 moles of ethylene glycol in three portions. To do.
- the addition amount per addition and the number of additions can be changed.
- the pressure in the polymerization apparatus is gradually reduced from normal pressure to 133 Pa or less to distill ethylene glycol.
- the polymerization temperature may be set low.
- the processing apparatus used the heat processing apparatus PRESER COOKER 306SIII (made by Hirayama Manufacturing Co., Ltd.).
- (4) Content of DEG (diethylene glycol) in the polyester composition Dissolve the polyester composition using monoethanolamine as a solvent, add 1,6-hexanediol / methanol mixed solution to the solution, cool, and add terephthalic acid After summing and centrifugation, the supernatant was measured by gas chromatography (manufactured by Shimadzu Corporation, GC-14A).
- Example 1 While the temperature in the reaction system in which 105 parts by weight of bishydroxyethyl terephthalate (equivalent to 100 parts by weight of polyethylene terephthalate [hereinafter referred to as PET]) was previously charged in an esterification reactor was maintained at 245 to 255 ° C., 86 parts by weight of terephthalic acid and ethylene A slurry consisting of 37 parts by weight of glycol was supplied into the reaction system by a snake pump, and the esterification reaction was advanced to distill water. When the esterification reaction rate reached 95%, the esterification reaction was terminated, and an esterification reaction product having a COOH end group amount of 334 eq / ton was obtained.
- PET polyethylene terephthalate
- polyester compositions obtained in Examples 2 to 7 also had sufficient hydrolysis resistance.
- polyester compositions obtained in Examples 8 and 9 had good hydrolysis resistance similar to that in Example 1.
- Example 10 A polyester composition was obtained in the same manner as in Example 1 except that unreacted ethylene glycol was not distilled when ethylene glycol was added, but was refluxed. This polyester composition had sufficient hydrolysis resistance. The results are shown in Table 3.
- Example 11 A slurry comprising 86 parts by weight of terephthalic acid and 37 parts by weight of ethylene glycol while maintaining the temperature in the reaction system in which 105 parts by weight of bishydroxyethyl terephthalate (equivalent to 100 parts by weight of PET) is previously charged in an esterification reactor at 245 to 255 ° C.
- Example 12 A slurry comprising 86 parts by weight of terephthalic acid and 37 parts by weight of ethylene glycol while maintaining the temperature in the reaction system in which 105 parts by weight of bishydroxyethyl terephthalate (equivalent to 100 parts by weight of PET) is previously charged in an esterification reactor at 245 to 255 ° C. was supplied into the reaction system with a snake pump, and the esterification reaction was advanced to distill water. When the esterification reaction rate reached 95%, the esterification reaction was terminated, and an esterification reaction product having a COOH end group amount of 334 eq / ton was obtained.
- polyester compositions obtained in Examples 13 to 15 had sufficient hydrolysis resistance with no problem even when used for solar cells and the like.
- polyester compositions obtained in Examples 16 to 20 also had sufficient hydrolysis resistance.
- Example 4 shows the results of these examples.
- Examples 21 to 28 A polyester composition was obtained in the same manner as in Example 1, except that the addition amount of the alkali metal phosphate added after the addition and the alkali metal phosphate species were changed.
- polyester compositions obtained in Examples 21 to 25, 27 and 28 had good hydrolysis resistance similar to that of Example 1.
- the polyester composition obtained in Example 26 had sufficient hydrolysis resistance.
- Examples 29 to 37 A polyester composition was obtained in the same manner as in Example 1 except that the phosphorus compound species to be mixed with the alkali metal phosphate, the addition amount of the phosphorus compound, and the phosphorus compound mixing molar ratio (to the alkali metal phosphate) were changed. .
- polyester compositions obtained in Examples 29 and 30 had hydrolysis resistance at a level that was not problematic even when used for solar cell applications.
- polyester compositions obtained in Examples 31 to 33 had good hydrolysis resistance as in Example 1.
- the polyester composition obtained in Example 34 had a level of hydrolysis resistance that caused no problem even when used for solar cell applications.
- polyester compositions obtained in Examples 35 to 37 had sufficient hydrolysis resistance.
- Example 38 A slurry comprising 86 parts by weight of terephthalic acid and 37 parts by weight of ethylene glycol while maintaining the temperature in the reaction system in which 105 parts by weight of bishydroxyethyl terephthalate (equivalent to 100 parts by weight of PET) is previously charged in an esterification reactor at 245 to 255 ° C. was supplied with a snake pump, and the esterification reaction was advanced to distill water. When the esterification reaction rate reached 95%, the esterification reaction was terminated, and an esterification reaction product having a COOH end group amount of 334 eq / ton was obtained.
- Parts (equivalent to 1.7 mol / ton) /1.4 parts by weight of ethylene glycol and 0.02 parts by weight of phosphoric acid (equivalent to 2.0 mol / ton) /0.2 parts by weight of ethylene glycol were added without mixing. .
- the total amount of distilled ethylene glycol was 5.5 parts by weight.
- the pressure in the polymerization apparatus was gradually reduced from normal pressure to 133 Pa or less to distill ethylene glycol.
- the melt viscosity corresponding to an intrinsic viscosity of 0.65 was reached, the reaction was terminated, the inside of the reaction system was brought to normal pressure with nitrogen gas, and the molten polymer was discharged into cold water in the form of a strand from the lower part of the polymerization apparatus. The discharged and solidified polyester strand was cut to obtain a pellet-shaped polyester composition.
- This polyester composition had a level of hydrolysis resistance that would not cause any problems even when used for solar cell applications.
- the results are shown in Table 7. (Comparative Example 4) A polyester composition was obtained in the same manner as in Example 1 except that the metal salt and the alkali metal phosphate were not added.
- Example 39 A slurry comprising 86 parts by weight of terephthalic acid and 37 parts by weight of ethylene glycol while maintaining the temperature in the reaction system in which 105 parts by weight of bishydroxyethyl terephthalate (equivalent to 100 parts by weight of PET) is previously charged in an esterification reactor at 245 to 255 ° C.
- trimellitic anhydride (1 wt% ethylene glycol solution) was added as a copolymerization component.
- the amount of COOH end groups after addition was 45 eq / ton.
- sodium dihydrogen phosphate dihydrate 0.027 parts by weight (equivalent to 1.7 mol / ton) /0.02 parts by weight of phosphoric acid (equivalent to 2.0 mol / ton, compared to alkali metal phosphate 1). 2 times mole) /1.6 parts by weight of ethylene glycol was added.
- the total amount of distilled ethylene glycol was 5.5 parts by weight.
- Example 1 a polyester composition having good hydrolysis resistance was obtained.
- Table 8 shows the properties of the obtained polyester composition.
- Example 40 the amount of trimellitic anhydride added was increased as compared with Example 39, so that the amount of COOH end groups of the polyester composition was reduced, and it had good hydrolysis resistance. .
- polyester compositions obtained in Examples 42 and 43 have sufficient hydrolysis resistance and are at a level that does not cause any problems even when used for solar cell applications.
- the polyester composition obtained in Example 44 had sufficient hydrolysis resistance.
- Example 45 While maintaining the temperature in the reaction system in which 105 parts by weight of bishydroxyethyl terephthalate (equivalent to 100 parts by weight of PET) was previously charged in an esterification reactor at 245 to 255 ° C., 86 parts by weight of terephthalic acid and 0.2 parts by weight of trimellitic anhydride The slurry consisting of 37 parts by weight of ethylene glycol was fed into the reaction system with a snake pump, and the esterification reaction was advanced to distill water. When the esterification reaction rate reached 95%, the esterification reaction was terminated, and an esterification reaction product having a COOH end group amount of 335 eq / ton was obtained.
- the third addition was performed, and a total amount of 26 parts by weight (0.8 times moles of terephthalic acid in 100 parts by weight of PET) of ethylene glycol was added.
- a total amount of 26 parts by weight (0.8 times moles of terephthalic acid in 100 parts by weight of PET) of ethylene glycol was added.
- the COOH end group amount reached 46 eq / ton
- 0.06 part by weight of manganese acetate and 0.03 part by weight of antimony trioxide were added, and 5 minutes later, sodium dihydrogen phosphate dihydrate 0
- a solution of 0.027 parts by weight (equivalent to 1.7 mol / ton) /0.02 parts by weight of phosphoric acid (equivalent to 2.0 mol / ton) /1.6 parts by weight of ethylene glycol was added.
- the total amount of distilled ethylene glycol was 15.1 parts by weight.
- the pressure in the polymerization apparatus was gradually reduced from normal pressure to 133 Pa or less to distill ethylene glycol.
- the melt viscosity corresponding to an intrinsic viscosity of 0.65 was reached, the reaction was terminated, the inside of the reaction system was brought to normal pressure with nitrogen gas, and the molten polymer was discharged into cold water in the form of a strand from the lower part of the polymerization apparatus. The discharged and cooled polyester strand was cut to obtain a polyester composition in the form of pellets.
- Example 46 The polyester composition obtained in Example 45 had sufficient hydrolysis resistance.
- Table 8 A slurry comprising 86 parts by weight of terephthalic acid and 37 parts by weight of ethylene glycol while maintaining the temperature in the reaction system in which 105 parts by weight of bishydroxyethyl terephthalate (equivalent to 100 parts by weight of PET) is previously charged in an esterification reactor at 245 to 255 ° C. was supplied into the reaction system with a snake pump, and the esterification reaction was advanced to distill water. When the esterification reaction rate reached 95%, the esterification reaction was terminated, and an esterification reaction product having a COOH end group amount of 334 eq / ton was obtained.
- the pressure in the polymerization apparatus was gradually reduced from normal pressure to 133 Pa or less to distill ethylene glycol.
- the inside of the reaction system was brought to atmospheric pressure with nitrogen, and 0.1 part by weight of trimellitic anhydride (1 wt% ethylene glycol solution) was added as a copolymerization component. Thereafter, the mixture was stirred for 5 minutes, and the pressure was reduced again to a vacuum to continue the polycondensation reaction.
- the polyester composition obtained in Example 46 had hydrolysis resistance without problems even when used for solar cell applications.
- the amount of COOH end groups can be controlled, and a polyester composition having good hydrolysis resistance can be provided, so that it can be suitably used for a film for solar cells. .
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Abstract
Description
リン酸アルカリ金属塩と混合するリン化合物は特に限定しないが、リン酸、トリメチルホスフェート、トリメチルホスホノアセテート、フェニルホスホン酸ジメチルなどが挙げられる。その中でも、耐加水分解性の観点から、リン酸が好ましい。
(1)固有粘度(IV)
オルトクロロフェノールを溶媒として25℃で測定した。
(2)COOH末端基量
次の文献に記載されたMauriceの方法により測定した。
(3)耐加水分解性評価(ΔCOOH)
ペレット状のポリエステル組成物を155℃、100%RHで4時間加熱処理し、処理前後のCOOH末端基量の差(処理後COOH末端基量-処理前COOH末端基量)を比較した。この時のCOOH末端基量の差(ΔCOOH)が、50eq/ton以下であるとき、良好な耐加水分解性を有していると判断した。
(4)ポリエステル組成物中のDEG(ジエチレングリコール)含有量
モノエタノールアミンを溶媒としてポリエステル組成物を溶解し、該溶液に1,6-ヘキサンジオール/メタノール混合溶液を加えて冷却し、テレフタル酸で中和した後、遠心分離した後に、上澄み液をガスクロマトグラフィ((株)島津製作所製、GC-14A)にて測定した。
(実施例1)
予めエステル化反応装置にビスヒドロキシエチルテレフタレート105重量部(ポリエチレンテレフタレート[以下、PET]100重量部相当)を仕込んだ反応系内の温度を245~255℃に保ちつつ、テレフタル酸86重量部とエチレングリコール37重量部からなるスラリーをスネークポンプにて反応系内に供給し、エステル化反応を進めて水を留出させた。エステル化反応率が95%に到達した段階で、エステル化反応を終了し、COOH末端基量が334eq/tonのエステル化反応物を得た。得られたエステル化反応物105重量部(PET100重量部相当)を留出装置の付いた重合装置に仕込み、酢酸マンガン0.06重量部(2.4mol/ton相当)、三酸化アンチモン0.03重量部(1.0mol/ton相当)、エチレングリコール8.7重量部(PET100重量部中のテレフタル酸に対し0.27倍モル)を同時に添加し、未反応のエチレングリコールを留出させた。系内温度が235℃に復帰した時点でエチレングリコール8.7重量部を再度添加、その後再び未反応のエチレングリコールを留出させながら235℃に温度復帰させ、さらにエチレングリコール8.7重量部を用いて3度目の添加を行い、総量26.1重量部(PET100重量部中のテレフタル酸に対し0.81倍モル)のエチレングリコールを添加した。添加終了後、未反応のエチレングリコールを留出させながら反応系温度が235℃に復帰し、COOH末端基量が48eq/tonとなった時点でリン酸二水素ナトリウム2水和物0.027重量部(1.7mol/ton相当)/リン酸0.02重量部(2.0mol/ton相当、リン酸アルカリ金属塩対比1.2倍モル)/エチレングリコール1.6重量部の溶液を添加した。留出させたエチレングリコールは総量5.5重量部であった。
(実施例2~9、比較例1~3)
添加するエチレングリコールの添加量、添加回数を変更した以外は実施例1と同様にしてポリエステル組成物を得た。
(実施例10)
エチレングリコールを添加する際、未反応のエチレングリコールを留出させず、環流させたこと以外は実施例1と同様にしてポリエステル組成物を得た。このポリエステル組成物は十分な耐加水分解性を有していた。結果を表3に示す。
(実施例11)
予めエステル化反応装置にビスヒドロキシエチルテレフタレート105重量部(PET100重量部相当)を仕込んだ反応系内の温度を245~255℃に保ちつつ、テレフタル酸86重量部とエチレングリコール37重量部からなるスラリーをスネークポンプにて反応系内に供給し、エステル化反応を進めて水を留出させた。エステル化反応率が95%に到達した段階で、エステル化反応を終了し、COOH末端基量が334eq/tonのエステル化反応物を得た。得られたエステル化反応物105重量部(PET100重量部相当)を留出装置の付いた重合装置に仕込み、エチレングリコール8.7重量部(PET100重量部中のテレフタル酸に対し0.27倍モル)を添加、未反応のエチレングリコールを留出させた。系内温度が235℃に復帰した時点でエチレングリコール8.7重量部を再度添加、その後再び未反応のエチレングリコールを留出させながら235℃に温度復帰させ、さらにエチレングリコール8.7重量部を用いて3度目の添加を行い、総量26重量部(PET100重量部中のテレフタル酸に対し0.8倍モル)のエチレングリコールを添加した。添加終了後、COOH末端基量が88eq/tonとなった時点で酢酸マンガン0.06重量部、三酸化アンチモン0.03重量部を添加し、5分後リン酸二水素ナトリウム2水和物0.027重量部(1.7mol/ton相当)/リン酸0.02重量部(2.0mol/ton相当)/エチレングリコール1.6重量部の溶液を添加した。留出させたエチレングリコールは総量15.1重量部であった。
(実施例12)
予めエステル化反応装置にビスヒドロキシエチルテレフタレート105重量部(PET100重量部相当)を仕込んだ反応系内の温度を245~255℃に保ちつつ、テレフタル酸86重量部とエチレングリコール37重量部からなるスラリーをスネークポンプにて反応系内に供給し、エステル化反応を進めて水を留出させた。エステル化反応率が95%に到達した段階で、エステル化反応を終了し、COOH末端基量が334eq/tonのエステル化反応物を得た。得られたエステル化反応物105重量部(PET100重量部相当)を留出装置の付いた重合装置に仕込み、酢酸マンガン0.06重量部(2.4mol/ton相当)、三酸化アンチモン0.03重量部(1.0mol/ton相当)、エチレングリコール8.7重量部(PET100重量部中のテレフタル酸に対し0.27倍モル)を同時に添加し、未反応のエチレングリコールを留出させた。系内温度が225℃に復帰した時点でエチレングリコール8.7重量部を再度添加、その後再び未反応のエチレングリコールを留出させながら225℃に温度復帰させ、さらにエチレングリコール8.7重量部を用いて3度目の添加を行い、総量26.1重量部(PET100重量部中のテレフタル酸に対し0.81倍モル)のエチレングリコールを添加した。添加終了後、未反応のエチレングリコールを留出させながら反応系温度が235℃に復帰し、COOH末端基量が125eq/tonとなった時点でリン酸二水素ナトリウム2水和物0.027重量部(1.7mol/ton相当)/リン酸0.02重量部(2.0mol/ton相当、リン酸アルカリ金属塩対比1.2倍モル)/エチレングリコール1.6重量部の溶液を添加した。留出させたエチレングリコールは総量8.5重量部であった。
(実施例13~20)
エチレングリコールの添加時に同時に添加する金属塩の添加量、金属塩種を変更した以外は、実施例1と同様にしてポリエステル組成物を得た。
(実施例21~28)
添加後に添加するリン酸アルカリ金属塩の添加量、リン酸アルカリ金属塩種を変更した以外は、実施例1と同様にしてポリエステル組成物を得た。
(実施例29~37)
リン酸アルカリ金属塩と混合するリン化合物種、リン化合物の添加量、リン化合物混合モル比(対リン酸アルカリ金属塩)を変更した以外は、実施例1と同様にしてポリエステル組成物を得た。
(実施例38)
予めエステル化反応装置にビスヒドロキシエチルテレフタレート105重量部(PET100重量部相当)を仕込んだ反応系内の温度を245~255℃に保ちつつ、テレフタル酸86重量部とエチレングリコール37重量部からなるスラリーをスネークポンプにて供給し、エステル化反応を進めて水を留出させた。エステル化反応率が95%に到達した段階で、エステル化反応を終了し、COOH末端基量が334eq/tonのエステル化反応物を得た。得られたエステル化反応物105重量部(PET100重量部相当)を留出装置の付いた重合装置に仕込み、酢酸マンガン0.06重量部(2.4mol/ton相当)、三酸化アンチモン0.03重量部(1.0mol/ton相当)、エチレングリコール8.7重量部(PET100重量部中のテレフタル酸に対し0.27倍モル)を同時に添加し、未反応のエチレングリコールを留出させた。系内温度が235℃に復帰した時点でエチレングリコール8.7重量部を再度添加、その後再び未反応のエチレングリコールを留出させながら235℃に温度復帰させ、さらにエチレングリコール8.7重量部を用いて3度目の添加を行い、総量26重量部(PET100重量部中のテレフタル酸に対し0.8倍モル)のエチレングリコールを添加した。添加終了後、未反応のエチレングリコールを留出させながら反応系温度が235℃に復帰し、COOH末端基量が48eq/tonとなった時点でリン酸二水素ナトリウム2水和物0.027重量部(1.7mol/ton相当)/エチレングリコール1.4重量部とリン酸0.02重量部(2.0mol/ton相当)/エチレングリコール0.2重量部の溶液を混合せずに添加した。留出させたエチレングリコールは総量5.5重量部であった。
(比較例4)
金属塩ならびにリン酸アルカリ金属塩を添加しなかった以外は、実施例1と同様にしてポリエステル組成物を得た。
(実施例39)
予めエステル化反応装置にビスヒドロキシエチルテレフタレート105重量部(PET100重量部相当)を仕込んだ反応系内の温度を245~255℃に保ちつつ、テレフタル酸86重量部とエチレングリコール37重量部からなるスラリーをスネークポンプにて反応系内に供給し、エステル化反応を進めて水を留出させた。エステル化反応率が95%に到達した段階で、エステル化反応を終了し、COOH末端基量が334eq/tonのエステル化反応物を得た。得られたエステル化反応物105重量部(PET100重量部相当)を留出装置の付いた重合装置に仕込み、酢酸マンガン0.06重量部(2.4mol/ton相当)、三酸化アンチモン0.03重量部(1.0mol/ton相当)、エチレングリコール8.7重量部(PET100重量部中のテレフタル酸に対し0.27倍モル)を同時に添加し、未反応のエチレングリコールを留出させた。系内温度が235℃に復帰した時点でエチレングリコール8.7重量部を再度添加、その後再び未反応のエチレングリコールを留出させながら235℃に温度復帰させ、さらにエチレングリコール8.7重量部を用いて3度目の添加を行い、総量26.1重量部(PET100重量部中のテレフタル酸に対し0.81倍モル)のエチレングリコールを添加した。添加終了後、未反応のエチレングリコールを留出させながら反応系温度が235℃に復帰したところで、共重合成分として無水トリメリット酸0.01重量部(1重量%のエチレングリコール溶液)を添加した(添加後のCOOH末端基量が45eq/ton)。5分後、リン酸二水素ナトリウム2水和物0.027重量部(1.7mol/ton相当)/リン酸0.02重量部(2.0mol/ton相当、リン酸アルカリ金属塩対比1.2倍モル)/エチレングリコール1.6重量部の溶液を添加した。留出させたエチレングリコールは総量5.5重量部であった。
(実施例40~44)
共重合成分として添加した無水トリメリット酸の添加量を変更した以外は、実施例39と同様にしてポリエステル組成物を得た。
(実施例45)
予めエステル化反応装置にビスヒドロキシエチルテレフタレート105重量部(PET100重量部相当)を仕込んだ反応系内の温度を245~255℃に保ちつつ、テレフタル酸86重量部と無水トリメリット酸0.2重量部、エチレングリコール37重量部からなるスラリーをスネークポンプにて反応系内に供給し、エステル化反応を進めて水を留出させた。エステル化反応率が95%に到達した段階で、エステル化反応を終了し、COOH末端基量が335eq/tonのエステル化反応物を得た。得られたエステル化反応物105重量部(PET100重量部相当)を留出装置の付いた重合装置に仕込み、エチレングリコール8.7重量部(PET100重量部中のテレフタル酸に対し0.27倍モル)を添加、未反応のエチレングリコールを留出させた。系内温度が235℃に復帰した時点でエチレングリコール8.7重量部を再度添加、その後再び未反応のエチレングリコールを留出させながら235℃に温度復帰させ、さらにエチレングリコール8.7重量部を用いて3度目の添加を行い、総量26重量部(PET100重量部中のテレフタル酸に対し0.8倍モル)のエチレングリコールを添加した。添加終了後、COOH末端基量が46eq/tonとなった時点で酢酸マンガン0.06重量部、三酸化アンチモン0.03重量部を添加し、5分後リン酸二水素ナトリウム2水和物0.027重量部(1.7mol/ton相当)/リン酸0.02重量部(2.0mol/ton相当)/エチレングリコール1.6重量部の溶液を添加した。留出させたエチレングリコールは総量15.1重量部であった。
(実施例46)
予めエステル化反応装置にビスヒドロキシエチルテレフタレート105重量部(PET100重量部相当)を仕込んだ反応系内の温度を245~255℃に保ちつつ、テレフタル酸86重量部とエチレングリコール37重量部からなるスラリーをスネークポンプにて反応系内に供給し、エステル化反応を進めて水を留出させた。エステル化反応率が95%に到達した段階で、エステル化反応を終了し、COOH末端基量が334eq/tonのエステル化反応物を得た。得られたエステル化反応物105重量部(PET100重量部相当)を留出装置の付いた重合装置に仕込み、酢酸マンガン0.06重量部(2.4mol/ton相当)、三酸化アンチモン0.03重量部(1.0mol/ton相当)、エチレングリコール8.7重量部(PET100重量部中のテレフタル酸に対し0.27倍モル)を同時に添加し、未反応のエチレングリコールを留出させた。系内温度が235℃に復帰した時点でエチレングリコール8.7重量部を再度添加、その後再び未反応のエチレングリコールを留出させながら235℃に温度復帰させ、さらにエチレングリコール8.7重量部を用いて3度目の添加を行い、総量26.1重量部(PET100重量部中のテレフタル酸に対し0.81倍モル)のエチレングリコールを添加した。添加終了後、未反応のエチレングリコールを留出させながら反応系温度が235℃に復帰し、COOH末端基量が48eq/tonとなった時点でリン酸二水素ナトリウム2水和物0.027重量部(1.7mol/ton相当)/リン酸0.02重量部(2.0mol/ton相当、リン酸アルカリ金属塩対比1.2倍モル)/エチレングリコール1.6重量部の溶液を添加した。留出させたエチレングリコールは総量5.5重量部であった。
Claims (7)
- ジカルボン酸成分とジオール成分とをエステル化反応し、次いで重縮合反応を行うポリエステル製造方法において、エステル化反応終了から重縮合反応開始までの間にジオール成分を2回以上添加し、エステル化反応物のCOOH末端基量を150eq/ton以下とした状態でリン酸アルカリ金属塩を添加するポリエステル組成物の製造方法。
- 添加するジオール成分が一回あたりジカルボン酸成分に対し0.15倍モル以上0.5倍モル以下である請求項1記載のポリエステル組成物の製造方法。
- 添加するジオール成分と共に、金属塩化合物を1.0mol/ton以上3.5mol/ton以下添加する請求項1または2記載のポリエステル組成物の製造方法。
- 添加するリン酸アルカリ金属塩が0.1mol/ton以上7.0mol/ton以下である請求項1~3いずれか1項記載のポリエステル組成物の製造方法。
- リン酸アルカリ金属塩をリン化合物およびジオール成分と混合し、溶液またはスラリーとして添加する請求項1~4いずれか1項記載のポリエステル組成物の製造方法。
- リン化合物をリン酸アルカリ金属塩に対し、0.1倍モル以上7.5倍モル以下混合する請求項5項記載のポリエステル組成物の製造方法。
- ジカルボン酸成分とジオール成分とをエステル化反応し、次いで重縮合反応を行うポリエステル製造方法において、重縮合反応開始までの間に3官能以上の共重合成分を添加する請求項1~6いずれか1項記載のポリエステル組成物の製造方法。
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JP2013203972A (ja) * | 2012-03-29 | 2013-10-07 | Toray Ind Inc | ポリエチレンテレフタレート組成物、その製造方法 |
WO2014045995A1 (ja) * | 2012-09-20 | 2014-03-27 | 東レ株式会社 | ポリエチレンテレフタレート組成物、その製造方法 |
JP2014156528A (ja) * | 2013-02-15 | 2014-08-28 | Toray Ind Inc | ポリエステル組成物の製造方法 |
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Also Published As
Publication number | Publication date |
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MY165613A (en) | 2018-04-18 |
US20130253165A1 (en) | 2013-09-26 |
TW201217428A (en) | 2012-05-01 |
JP5790506B2 (ja) | 2015-10-07 |
EP2615123A4 (en) | 2016-12-07 |
US9273182B2 (en) | 2016-03-01 |
CN103189415B (zh) | 2015-04-15 |
CN103189415A (zh) | 2013-07-03 |
KR20140009117A (ko) | 2014-01-22 |
KR101783293B1 (ko) | 2017-09-29 |
EP2615123B9 (en) | 2019-11-13 |
JPWO2012032876A1 (ja) | 2014-01-20 |
EP2615123B1 (en) | 2019-07-17 |
TWI523886B (zh) | 2016-03-01 |
EP2615123A1 (en) | 2013-07-17 |
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