WO2006090708A1 - ポリエステルの連続的製造方法、ポリエステルプレポリマー粒状体及びポリエステル - Google Patents
ポリエステルの連続的製造方法、ポリエステルプレポリマー粒状体及びポリエステル Download PDFInfo
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- WO2006090708A1 WO2006090708A1 PCT/JP2006/303081 JP2006303081W WO2006090708A1 WO 2006090708 A1 WO2006090708 A1 WO 2006090708A1 JP 2006303081 W JP2006303081 W JP 2006303081W WO 2006090708 A1 WO2006090708 A1 WO 2006090708A1
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/78—Preparation processes
- C08G63/82—Preparation processes characterised by the catalyst used
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/78—Preparation processes
- C08G63/82—Preparation processes characterised by the catalyst used
- C08G63/826—Metals not provided for in groups C08G63/83 - C08G63/86
-
- 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
-
- 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
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/78—Preparation processes
- C08G63/82—Preparation processes characterised by the catalyst used
- C08G63/85—Germanium, tin, lead, arsenic, antimony, bismuth, titanium, zirconium, hafnium, vanadium, niobium, tantalum, or compounds thereof
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
- Y10T428/00—Stock material or miscellaneous articles
- Y10T428/29—Coated or structually defined flake, particle, cell, strand, strand portion, rod, filament, macroscopic fiber or mass thereof
- Y10T428/2982—Particulate matter [e.g., sphere, flake, etc.]
Definitions
- Polyester continuous production method polyester prepolymer particles and polyester
- the present invention is a continuous production method of a polyester, and a production intermediate of the method, a relatively low molecular weight polyester pellet polymer suitable for solid-phase polycondensation, and solid-phase polycondensation thereof. It relates to the resulting polyester.
- the present invention relates to a continuous production method in which a melt polycondensation reaction apparatus is simplified and polyester can be produced at a high speed.
- Polyesters typified by polyethylene terephthalate are excellent in mechanical properties, thermal properties, electrical properties, etc., and are therefore widely used in molded products such as fibers and films, sheets, and bottles for various uses. Demand is also expanding.
- High molecular weight polyesters used as container materials for bottles and the like are usually melt polycondensed through diesterification and Z or transesterification reaction between dicarboxylic acid and Z or its ester-forming derivative and diol. It is produced by solid phase polycondensation.
- a relatively high molecular weight polyester polymer is obtained by melt polycondensation, and this is produced by solid phase polycondensation.
- a relatively high molecular weight polyester prepolymer In the final stage of the melt polycondensation to obtain the above, a horizontal plug flow reactor equipped with complicated stirring blades is used. Also, the solid phase polycondensation reaction usually takes a long time of over 10 hours.
- a polyester prepolymer having a relatively low molecular weight is obtained by melt polycondensation.
- a method for producing a polyester for use in the phase polycondensation process has also been proposed (see, for example, Patent Document 1). However, even in this case, it is still insufficient in that a relatively long solid phase polycondensation time is required.
- Patent Document 2 the solid-phase polycondensation rate depends on the catalyst amount and the carboxyl terminal group content of the prepolymer. Change the feed ratio of terephthalic acid and ethylene glycol in the polymerization reaction, add an excess of ethylene glycol to the initial charge at a later stage of the reaction, or apply a partial vacuum to the polycondensation process
- this method is difficult to apply to a continuous production method of polyester and is always satisfactory in terms of polymerization rate. It was hard to do anything.
- antimony compounds, germanium compounds, titanium compounds and the like have long been known as catalysts for proceeding with polycondensation reactions, and tungsten catalysts such as tungsten salts have been used as catalysts with high polycondensation reaction rates.
- tungsten catalysts such as tungsten salts have been used as catalysts with high polycondensation reaction rates.
- Patent Document 3 There are known compounds (for example, see Patent Document 3).
- tungsten compound is used as a catalyst, the polymerization rate is still insufficient from the viewpoint of more efficient production.
- the polycondensation reaction mainly proceeds by two kinds of reactions, ie, an esterification reaction between a carboxylic acid and an alcohol, and an ester exchange reaction (alcohol exchange reaction) between an ester bond and an alcohol.
- an esterification reaction between a carboxylic acid and an alcohol ie, an esterification reaction between a carboxylic acid and an alcohol
- an ester exchange reaction alcohol exchange reaction
- Patent Document 1 Japanese Patent Publication No. 10-512608
- Patent Document 2 JP-A-55-133421
- Patent Document 3 Japanese Patent Publication No. 44-19554
- the present invention makes it possible to produce a high-molecular-weight, high-quality polyester having practicality as a container material or the like in a relatively short solid-phase polycondensation time without using a complicated melt polycondensation reaction apparatus.
- the purpose of the present invention is to provide a method for producing polyester efficiently at low cost.
- the inventors of the present invention have a relatively low molecular weight by melt polycondensation.
- two or more catalysts having a specific relationship within a specific range of catalyst activity ratios are produced by the polyester production process.
- the inventors have found that the solid-phase polycondensation rate is improved by adding them in a specific order to specific stages of the present invention, and the present invention has been reached.
- the gist of the present invention is as follows: (a) an esterification step in which an oligomer is obtained by subjecting a dicarboxylic acid component containing terephthalic acid as a main component to a diol component containing ethylene glycol as a main component; (b) A melt polycondensation step for obtaining a polyester prepolymer by subjecting the obtained oligomer to a melt polycondensation reaction; (c) a granulation step for obtaining a polyester prepolymer particle by granulating the obtained polyester prepolymer; (d) In the method of continuously producing a polyester having a solid phase polycondensation step of obtaining a polyester by subjecting the polyester prepolymer granules to a solid phase polycondensation reaction, the catalyst satisfies at least the following (1) to (3): The two types of catalyst 1 and catalyst 2 are sequentially added to any two different places prior to the granulation step (c), and the polyester obtained in step (
- Continuous polyester polyester characterized in that the solid viscosity of the prepolymer granules is 0.18 dLZg or more and 0.35 dLZg or less, and the intrinsic viscosity of the polyester obtained in the solid phase polycondensation step (d) is 0.70 dLZg or more.
- Activity ratio (K1) of catalyst 1 is 0.5 or more
- the activity ratio (K2) of catalyst 2 is less than 0.6
- the catalyst activity ratio is an indicator of the ratio of the esterification reaction catalyst activity to the total of the esterification reaction catalyst activity and transesterification catalyst activity of the catalyst, and is defined by the method described in the specification.
- Another gist is that the intrinsic viscosity is 0.18 dLZg or more and 0.35 dLZg or less, the terminal carboxyl group concentration is 30 equivalents Zton or less, the average particle size is 0.1 mm or more and 2.0 mm or less, and the tandane element and antimony element. Further, the present invention resides in a polyester prepolymer polymer characterized in that it contains at least one element selected from germanium and titanium. The invention's effect
- the method for continuously producing the polyester of the present invention comprises: (a) esterification of an oligomer by an esterification reaction of a dicarboxylic acid component having terephthalic acid as a main component and a diol component having ethylene glycol as a main component. Step, (b) a melt polycondensation step in which the obtained oligomer is subjected to a melt polycondensation reaction to obtain a polyester prepolymer, and (c) a granulation step in which the obtained polyester prepolymer is granulated to obtain a polyester prepolymer particle.
- step (D) a solid phase polycondensation step of obtaining a polyester by subjecting the obtained polyester prepolymer particles to a solid phase polycondensation reaction, usually prior to the step (a), A slurrying step of mixing the dicarboxylic acid component and the diol component to obtain a slurry; Also, between the slurrying step and step (a), a slurry transfer step for transferring the slurry to the esterification step, and between steps (a) and (b), the oligomer obtained in step (b) is melted. An oligomer transfer step for transferring to the condensation step, and a prepolymer transfer step for transferring the obtained polyester prepolymer to the granulation step between steps (c) and (d).
- each said transfer process connects each process before and behind with piping, and transfers the mixture and Z or a product (henceforth abbreviated to a product hereafter) of a previous process to a subsequent process continuously. It is done by.
- the pre-process, transfer process and post-process are installed in a low order and the product of the pre-process is transferred using the difference in height, and the pre-process is relative to the post-process. Examples include a method of transferring the product using a pressure difference between the preceding and succeeding steps in the transfer process and a method of transferring the product of the previous process by installing a pump in the subsequent process.
- the method power to transfer using a pump is preferable because it is possible to accurately control the transfer amount and speed of the product in the previous step.
- Insoluble impurities and particles In order to remove large-diameter precipitates, a filter or the like can be installed in the transfer process.
- the dicarboxylic acid component containing terephthalic acid as the main component is a dicarboxylic acid component in which 95 mol% or more is a terephthalic acid component with respect to the total dicarboxylic acid component used in the production of the polyester. Preferably, it is 97 mol% or more.
- the content of the terephthalic acid component is less than the above range, the heat resistance as a molded body such as a heat-resistant bottle tends to be inferior when the obtained polyester is formed into a molded body.
- the diol component containing ethylene glycol as the main component means that the ethylene glycol component is 95% or more, preferably 97 mol% or more, based on the total diol components used in producing the polyester.
- dicarboxylic acid components other than terephthalic acid for example, phthalic acid, isophthalic acid, dib-mouthed moisophthalic acid, sodium sulfoisophthalate, phenylenedicarboxylic acid, 4,4'-diphenyldicarboxylic acid 4,4'-diphenyl ether dicarboxylic acid, 4,4, -diphenyl ketone dicarboxylic acid, 4,4'-diphenylethane dicarboxylic acid, 4, 4, -diphenylsulfone dicarboxylic acid, 2, 6— Aromatic dicarboxylic acids such as naphthalenedicarboxylic acid, alicyclic dicarboxylic acids such as hexahydroterephthalic acid, hexahydroisophthalic acid, and succinic acid, glutaric acid, adipic acid, pimelic acid, suberic acid, and azelaic acid And alipha
- diol components other than ethylene glycol include, for example, trimethylene glycol, tetramethylene glycol, pentamethylene glycol, hexamethylene glycol, otamethylene glycol, decamethylene glycol, neopentyl glycol, 2-Ethyl-2-butyl-1,3-propanediol, polyethylene glycol, polytetramethylene ether glycol and other aliphatic diols, 1,2-cyclohexanediol, 1,4-cyclohexanediol, 1,1-cyclohexane Cyclohexane methylol, 1,4-cyclohexanedimethylol, cycloaliphatic diols such as 2,5-norbornane dimethylol, and xylylene glycol, 4,4, -dihydroxybiphenyl, 2,2-bis (4'-hydroxyphenol) propa , 2, 2-bis (4 '- beta-
- Trifunctional or higher compounds such as polycarboxylic acids such as trimellitic acid and pyromellitic acid and their anhydrides, and trimethylolmethane, trimethylolethane, trimethylolpropane, pentaerythritol, glycerol, hexanetriol, etc.
- polycarboxylic acids such as trimellitic acid and pyromellitic acid and their anhydrides
- trimethylolmethane trimethylolethane
- trimethylolpropane pentaerythritol
- glycerol glycerol
- hexanetriol hexanetriol
- Activity ratio (K1) of catalyst 1 is 0.5 or more
- the catalyst activity ratio is defined below.
- the catalyst activity ratio ( ⁇ ) is an index of the ratio of esterification reaction catalyst activity to the sum of esterification reaction catalyst activity and transesterification reaction catalyst activity, and is calculated by the following formula.
- AVO, TEVO, AV1, and TEV1 are respectively defined as follows.
- AVO Terminal carboxy group concentration of the 0th minute sample
- TEV1 Total end group concentration of the 20th minute sample
- the catalyst concentration of the raw material oligomer is adjusted for each catalyst type so that the intrinsic viscosity in the 20th minute falls within the range of 0.18 to 0.28 dLZg. Note that it is practically difficult to adjust the intrinsic viscosity to a single value, and the fluctuation of the catalyst activity ratio defined in the present invention due to slight fluctuation of the value is considered to be negligible.
- the inherent viscosity allowed as follows was set to 0.18 to 0.28 dLZg.
- TEV equivalent Zton
- Mn (Intrinsic viscosity (dL / g) X 10000/7. 55 ) (1 / . 685)
- TEV (equivalent Zton) 2 X 1000 X 1000 / Mn
- Mn is the number average molecular weight.
- AV equivalent Zton
- At least two kinds of catalyst 1 and catalyst 2 are sequentially added to any two different places prior to the granulation step (c), so that at least catalyst 1 and catalyst 2 are added to the granulation step (c).
- any different point forces of the preceding process are also added in this order, that is, as long as catalyst 1 is added to the process upstream of the point where catalyst 2 is added, the same process, e.g. It may be added at different positions or at different steps.
- catalyst 1 is added to the esterification step (a), and catalyst 2 is added to the step of transferring the oligomer obtained in the esterification step (a) to the melt polycondensation step (b) or subsequent steps. Is preferred.
- the activity ratio K1 of the catalyst 1 is a force of 0.5 or more, preferably 0.55 or more, more preferably 0.60 or more, and particularly preferably 0.65 or more.
- the activity ratio K2 of catalyst 2 is less than 0.6, but is preferably less than 0.55.
- the lower limit is usually 0.2, and preferably 0.3.
- the activity ratio K2 of the catalyst 2 is related to the transesterification activity effective for the solid phase polycondensation reaction, and if K2 is 0.6 or more, the solid phase polycondensation reaction rate is decreased, which is not preferable.
- the activity ratio K1 of the catalyst 1 and the activity ratio K2 of the catalyst 2 need to satisfy the relationship of Kl> K2.
- the feature of the present invention that the reaction rate in the solid phase polycondensation step is high is not exhibited, which is not preferable.
- the catalyst 1 is not particularly limited as long as it has an activity ratio K1 of 0.5 or more and satisfies ⁇ 1> ⁇ 2, and examples thereof include tungsten compounds and titanium compounds. A composite is preferred.
- Tungsten compounds include, for example, nortungstic acid, metatungstic acid, tandastanoic acid, key tungstic acid, phosphotungstic acid and their salts.
- salts include ammonium salt, sodium salt, potassium salt. And alkali metal salts.
- metatungstate ammonium, paratungstate ammonium, sodium tandastenate, and tungstic acid are preferred, with metatungstate ammonium and paratungstate ammonium being particularly preferred. is there.
- titanium compounds include tetra- ⁇ -propyl titanate, tetra-i-propyl titanate, tetra-n-butyl titanate, tetra-n-butyl titanate tetramer.
- Tetra-alkoxy titanates such as tetra-t-butyl titanate, acetyl-tri-titanate, i-propyl titanate, titanium acetate, titanium oxalate, titanium salt, titanium tetra-butyl titanate and tetra-n-butyl titanate are preferred. Gu tetra-n-butyl titanate is particularly preferred.
- the amount of catalyst 1 used cannot be generally specified depending on the type of catalyst, but the concentration of the metal element derived from catalyst 1 in the obtained polyester may be appropriately selected from 0.5 ppm by weight to 500 ppm by weight.
- the lower limit of the concentration is preferably 1 ppm by weight, and the upper limit is preferably 300 ppm by weight, more preferably 200 ppm by weight, and particularly preferably 100 ppm by weight.
- the concentration of the metal element is the total concentration of the different metal elements.
- the catalyst 2 is not particularly limited as long as it has an activity K2 of less than 0.6 and satisfies K1> K2.
- germanium compounds and antimony compounds are preferably used. It is done.
- germanium compound examples include germanium dioxide, germanium tetroxide, germanium hydroxide, germanium oxalate, germanium tetraethoxide, germanium tetra- ⁇ -butoxide, and among these, germanium diacid germanium is preferable.
- antimony compound examples include diantimony trioxide, antimony pentoxide, antimony acetate, and methoxyantimony. Among them, diantimony triacid is preferable.
- Each of catalyst 1 and catalyst 2 may be a single compound or a combination of two or more compounds. Further, it may be a combination of the one or more catalyst components and one or more other promoter components. Furthermore, the catalyst 2 may be a promoter component. Examples of the promoter component include alkali metal compounds, alkaline earth metal compounds, and silicon compounds.
- Catalyst 2 is preferably a combination of a titanium compound and one or more promoter components. Among them, titanium element and silicon element, titanium element and magnesium element, or titanium element, magnesium element, and phosphorus element. Catalysts containing these three elements are preferred.
- Titanium compounds in this case include tetra- ⁇ -propyl titanate, tetra-i-propyl titanate, tetra-n-butyl titanate, tetra-n-butyl titanate tetramer, tetra-t-butyl titanate, titanium acetate, titanium oxalate, potassium potassium succinate, titanium oxalate
- titanium acetate titanium oxalate
- potassium potassium succinate titanium oxalate
- titanium oxalate examples include tan sodium, potassium titanate, sodium titanate, salt-titanium, salt-titanium monosalt-aluminum mixture, among others, tetra n-propyl titanate, tetra i propyl titanate, tetra n butyl titanate, etc. Titanium alkoxide is preferred Yes.
- Co-catalyst components include methoxyester compounds such as tetramethoxysilane, tetraisopropoxysilane, tetrabutyloxysilane, tetraphenoxysilane, and tetrabenzyloxysilane; Siloxane compounds such as carboxylate, disiloxane, trisiloxane, dimethyldisiloxane, hexamethyldisiloxane, silanol compounds such as silanol, silanediol and phenolsilanetriol, silanolate compounds such as sodium toluenesilanol, Alternatively, a silicon compound such as a polyalkoxysiloxane compound which is a hydrolyzate of a carboxylic acid ester compound, or a magnesium compound such as magnesium acetate can be used.
- methoxyester compounds such as tetramethoxysilane, tetraisopropoxysilane,
- the catalyst 2 a combination of an alkali metal compound and Z or an alkaline earth metal compound and a phosphorus compound is preferable, but a catalyst containing a magnesium element and a phosphorus element is preferable!
- the alkali metal compound and Z or alkaline earth metal compound in this case include lithium acetate, sodium acetate, potassium acetate, potassium hydroxide, magnesium acetate, magnesium hydroxide, magnesium alkoxide, magnesium carbonate, calcium hydroxide. , Calcium acetate, calcium carbonate and the like.
- Phosphorus compounds include orthophosphoric acid, orthophosphoric alkyl ester, ethyl acyl phosphate, monoethyl acyl phosphate, jetyl acid phosphate, dibutyl phosphate, triethylene glycol acid phosphate, phosphorous acid, alkyl phosphite.
- esters include esters
- magnesium acetate with ethyl acid phosphate and Z or dibutyl phosphate is preferred.
- the amount of catalyst 2 used cannot be generally specified depending on the type of catalyst, but the concentration of metal element derived from catalyst 2 in the resulting polyester is usually 1 weight ⁇ ! Appropriately selected from ⁇ 500 ppm by weight.
- the lower limit of the concentration is preferably 5 ppm by weight, and the upper limit is preferably 300 ppm by weight, more preferably 250 ppm by weight.
- the concentration of the metal element is the total concentration of the different metal elements.
- a phosphorus compound or the like as a stabilizer may be used as long as the catalysts 1 and 2 are used.
- the polyester obtained in the melt polycondensation step (b) is used.
- the intrinsic viscosity of the ester prepolymer is 0.18 dLZg or more and 0.35 dLZg or less.
- the lower limit is preferably 0.19 dLZg, more preferably 0.20 dLZg, and the upper limit is preferably 0.33 dLZg, preferably 0.32 dLZg. If it is less than the lower limit, it is disadvantageous in that the time required for the reaction of the solid phase polycondensation process, which is a subsequent process, is increased.If the upper limit is exceeded, the polycondensation reactor in the melt polycondensation process is plug flowable. Therefore, a complicated and expensive facility such as a horizontal reactor having the above is required, which is not suitable for the purpose of the present invention.
- the terminal carboxyl group concentration of the polyester prepolymer is preferably 30 equivalents Zton or less, more preferably 20 equivalents Zton or less. If it is too large, the solid phase polycondensation rate tends to be slow.
- the lower limit is preferably as small as possible, and is therefore 0 equivalent Zton.
- the average particle size of the polyester prepolymer granules to be subjected to the solid phase polycondensation step is usually 0.1 mm or more and 2. Omm or less.
- the lower limit is preferably 0.15 mm, more preferably 0.2 mm, and the upper limit is preferably 1.5 mm, more preferably 1.3 mm. If it is too small, the solid-phase polycondensation rate is fast, but it is in powder form, so handling properties such as transfer and weighing will be remarkably inferior. If it is too large, the specific surface area of the granule may be reduced, and the solid phase polycondensation rate may be reduced.
- the intrinsic viscosity obtained according to the above is 0.18 dLZg or more and 0.35 dLZg or less, the terminal carboxyl group concentration is 30 equivalents Zton or less, the average particle size is 0.1 mm or more and 2.0 mm or less.
- Polyester prepolymer particles characterized by containing at least one element selected from tungsten element, antimony element, germanium element, titanium element force derived from the continuous production of the polyester of the present invention Useful as an intermediate product of the process.
- the intrinsic viscosity of the polyester obtained through the solid phase polycondensation step (d) of the present invention is 0.70d.
- LZg or more preferably 0.75 dLZg or more.
- the upper limit is usually 1.10 dL / g, preferably 1. OOdLZg or less. If it is less than the lower limit, the mechanical strength of a molded product such as a bottle made from this is inferior, which is not preferable. On the other hand, if the upper limit is exceeded, the melt viscosity is too high during molding of the molded body, which may cause molding defects.
- the method for continuously producing a polyester according to the present invention comprises the steps of selecting a catalyst and supplying the catalyst, and adjusting the reaction temperature, reaction pressure, reaction time, etc.
- the production is carried out according to a known polyester production method except that the intrinsic viscosity of the granular material and the intrinsic viscosity of the polyester obtained in the solid phase polycondensation step are as described above.
- a raw material slurry is usually prepared by mixing a dicarboxylic acid component and a diol component.
- the raw material slurry is prepared by mixing a dicarboxylic acid component containing terephthalic acid as a main component, a diol component containing ethylene glycol as a main component, a copolymerization component used as necessary, and the like with the mole of the diol component relative to the dicarboxylic acid component.
- the prepared raw material slurry is transferred to an esterification step equipped with one or a plurality of esterification reaction tanks and subjected to an esterification reaction under normal pressure to pressure and under heating to reduce the polyester low molecular weight.
- the oligomer is a body (esterification step (a)).
- reaction conditions in the esterification reaction in the case of a single esterification reaction tank, a temperature and pressure of about 240 to 290 ° C are usually set to 0 to 4001 ⁇ 1 ⁇ 20 (0 to 413 ⁇ 47 «11 2 G
- the reaction time (residence time) is about 1 to 10 hours with stirring.
- the reaction temperature in the first stage esterification reactor is usually 240 to 270. C, preferably 245-265.
- the pressure is usually 5 to 300 kPaG (0.05 to 3 kgZcm 2 G), preferably 10 to 200 kPaG (0.1 to 2 kgZcm 2 G), and the reaction temperature in the final stage is usually 250 to 290.
- C preferably 255-280.
- pressure is usually 0 to 150 kPaG (0 to: L 5 kgZcm 2 G), preferably 0 to 130 kPaG (0 to: L 3 kg / cm 2 G). Where kPaG is the relative pressure to atmospheric pressure in kPa.
- the esterification ratio of the oligomer as the esterification reaction product (the ratio of the esterified by reacting with the diol component out of the total carboxyl groups of the raw dicarboxylic acid component) is 90% or more. 94% or more is more preferable.
- melt polycondensation step (b) the obtained oligomer is transferred to a melt polycondensation step equipped with a polycondensation reaction tank and subjected to a melt polycondensation reaction under reduced pressure and heating.
- the melt polycondensation can be usually carried out in a single reaction tank of a complete mixing type equipped with a stirring blade.
- the horizontal plug flow type second stage and third stage equipped with a stirring blade that has been widely used in the past are used.
- the melt polycondensation process which does not require a single stage polycondensation reaction tank, is simplified and equipment costs are reduced.
- the reaction conditions in the melt polycondensation are a temperature of 260 to 290 ° C, preferably 270 to 280 ° C, and a pressure of 100 to 0. OlkPaA, preferably 50 to 0. lkPaA.
- the reaction time ⁇ residence time> is adjusted so that the intrinsic viscosity of the polyester prepolymer particles obtained by granulating the polyester prepolymer obtained in the melt polycondensation step in the granulation step described below is within the range of the present invention. Although it varies depending on the temperature and pressure, it is usually about 0.5 to 3 hours.
- the polyester prepolymer obtained by the melt polycondensation is usually extracted in a strand form from an outlet provided at the bottom of the polycondensation reaction tank, and is cooled with water or cooled with water, and then cut with a cutter. Prebolimer granules.
- the outlet force provided at the bottom of the polycondensation reaction tank can be cooled by discharging into water, and it has a rotating shaft in a direction substantially parallel to the discharge direction and is installed adjacent to the tip of the outlet. Cut into polyester pellets. Or it can also grind
- polyester prepolymer particles obtained in the granulation step (c) are fluidized for 0.5 to 12 hours in a known method, for example, in an inert gas stream at 120 to 180 ° C, if necessary. After crystallization and drying treatment, solid phase polycondensation reaction is performed (solid phase polycondensation reaction step (d)) G
- the lower limit of the temperature is usually 200 ° C, preferably 205 ° C, more preferably 208 ° C, and the upper limit of the temperature is 5 ° C higher than the melting point of the polyester. It is carried out in an inert gas atmosphere at a temperature lower than the melting point, preferably 8 ° C lower than the melting point, more preferably 10 ° C lower than the melting point.
- the melting point of the polyester is the DSC curve when the polyester is heated to 300 ° C at a rate of 0 ° C to 20 ° CZ using a differential scanning calorimeter in a nitrogen stream.
- Inert gas is oxygen concentration of 0.1% by volume or less.
- the gas is preferably 0.05% by volume or less and does not substantially react with the polyester.
- Examples of the gas that does not substantially react with the polyester include nitrogen, helium, neon, argon, xenon, carbon dioxide and the like, and nitrogen is preferably used mainly from the viewpoint of economy.
- the solid-phase polycondensation temperature is too low, the solid-phase polycondensation rate decreases, which is not preferable. If the solid phase polycondensation temperature is too high, the polyester particles are fused during solid phase polycondensation, which is not preferable.
- the average particle size of the polyester prepolymer particles is 1. Omm or less, solid phase polycondensation is preferably performed in a fluidized bed.
- the solid phase polycondensation time is usually about 1 to 50 hours as long as it is set according to the target intrinsic viscosity so that the intrinsic viscosity of the obtained polyester is 0.70 dlZg or more.
- the average particle size after the solid phase polycondensation usually matches the average particle size of the prepolymer before the solid phase polycondensation.
- the polyester obtained by the production method of the present invention can be formed into a bottle used for beverages or the like by stretch blow molding after forming a preform by injection molding or extrusion molding. Moreover, it can be made into a bottle by direct blow molding.
- the polyester obtained by the production method of the present invention can be used for various uses such as packaging materials by forming into a film or sheet by extrusion molding or stretch molding. It can also be made into fibers by extrusion and stretch molding.
- IV ((1 + 4KH r? Sp). ⁇ 5 — 1) / (2KHC)
- 7? SP 7? Z 7 ⁇ 0— 1
- ⁇ is the drop time of the sample solution
- 7? 0 is the drop time of the solvent only
- C is the sample solution concentration (g / dL)
- ⁇ is Haggins' constant.
- KH adopted 0.33.
- the dissolution conditions of the sample were 120 ° C for 30 minutes when the sample was a prepolymer, and 140 ° C for 30 minutes for the polyester after solid phase polycondensation.
- 0.3 g of the sample crushed in the mortar is precisely weighed into an Erlenmeyer flask, and 0.5 ml of a 0.5 N KOH ethanol solution is added with a whole pipette to this, and further 10 ml of pure water is added, and a reflux condenser is set.
- the sample was hydrolyzed by heating at reflux for 2 hours on a plate heater with a surface temperature of 200 ° C with occasional stirring.
- the sample solution at this time is transparent.
- titration was carried out with 0.5N aqueous hydrochloric acid using phenolphthalein as an indicator.
- 0.5N KOH ethanol solution and 0.5N hydrochloric acid aqueous solution were prepared and standardized by the method of JIS K8006. Also, phenolphthalein was used in which lg was dissolved in 90 ml of ethanol and the volume was adjusted to 100 ml with pure water. Titration was also performed in a blank state where no sample was placed under the same conditions.
- Esterification rate (%) ⁇ (SV-AV) / SV ⁇ X 100
- Terminal carboxyl group concentration (A— B) X 0.1 X f / W
- A is the amount of 0.1N sodium hydroxide in benzyl alcohol solution required for titration (1)
- B is the amount of 0.1N caustic soda in benzyl alcohol solution required for titration 1
- W is the amount of the polyester resin sample (g)
- f is the titer of benzyl alcohol solution of 0.1N sodium hydroxide solution.
- the titer (f) of 0.1N sodium hydroxide in benzyl alcohol solution was obtained by taking 5 ml of methanol into a test tube, adding 1-2 drops of ethanol red ethanol solution as an indicator, and adding 0.1N water. Titrate with 0.4 ml of sodium oxide in benzyl alcohol to the color change point, then take 0.2 ml of 0.1N hydrochloric acid solution of known titer as a standard solution, and hold again. Titrate to discoloration with sodium benzyl alcohol solution. (The above operations were carried out under dry nitrogen gas blowing.) The titer (f) was calculated by the following equation.
- Titer (f) 0. Titer of IN aqueous hydrochloric acid solution X O. Sample volume of 1N aqueous hydrochloric acid solution 1) Titration of Z0.IN sodium hydroxide in benzyl alcohol solution ( ⁇ 1)
- the average particle size was defined as the value obtained when the cumulative percentage in the cumulative distribution curve prepared by the dry sieving method described in JIS K0069 was 50%.
- the “catalytic activity ratio (K)” is an index of the ratio of the esterification reaction catalytic activity to the total of the esterification reaction catalytic activity and the transesterification reaction catalytic activity.
- AVO, TEVO, AV1, and TEV1 are defined as follows.
- the room temperature power is raised to 270 ° C over 90 minutes with stirring, and 30 ° C at 270 ° C.
- add the catalyst of interest and gradually reduce the pressure from atmospheric pressure to 1.33 kPaA (10 torr) over 10 minutes with stirring, and perform the melt polycondensation reaction.
- AVO Terminal carboxy group concentration of the 0th minute sample
- TEV0 Total end group concentration of the 0th minute sample
- TEV1 Total end group concentration of the 20th minute sample
- the catalyst concentration of the raw material oligomer is adjusted for each catalyst type so that the intrinsic viscosity in the 20th minute falls within the range of 0.18 to 0.28 dLZg.
- TEV equivalent Zton
- Mn (Intrinsic viscosity (dL / g) X 10000/7. 55 ) (1 / . 685)
- TEV (equivalent Zton) 2 X 1000 X 1000 / Mn
- AV equivalent Zton
- the esterification ratio of this oligomer was 91.9%, the terminal carboxyl group concentration was 834 equivalents Z ton, and the total terminal group concentration was 1620 equivalents Zton.
- Ethanol was distilled off under reduced pressure until the content was 322.2 g.
- 389.25 g of ethylene glycol was added under normal pressure of nitrogen and mixed for 15 minutes to prepare a uniform solution.
- low boiling point substances were removed by treating under reduced pressure of 1.33 kPa (10 Torr) for 40 minutes to obtain a pale yellow polycondensation catalyst solution (titanium-magnesium-phosphorus synthesis catalyst) 508. Og ⁇ of this solution was 5.4, and it was stable as a homogeneous solution.
- the concentrations of titanium, magnesium, and phosphorus were 2.6 ppm, 1.4 ppm, and 0.9 ppm, respectively.
- the metatungstate ammoxidation was prepared using as a catalyst 1 at the same time - ⁇ beam ethylene glycol solution: from the gas phase portion of the first S. Terui spoon reactor (concentration 1.1 wt 0/0 as tungsten atom), obtained 80 as tungsten against polyester An amount of ppm by weight was continuously added, the esterification reaction was carried out while distilling off the water generated from the separation column (Esterig process), and the water was continuously extracted and transferred to the second esterification reactor. In the second esterification reactor, the esterification reaction was carried out at a temperature of 260 ° C, a pressure of 5 kPaG, and a residence time of 1.5 hours!
- the reaction is performed at a pressure of 2.5 kPaA, a temperature of 273 ° C and a residence time of 1.0 hour in the polycondensation tank (melt polycondensation process), and the resulting polyester prepolymer is extracted through a pipe (prepolymer transfer) Step) Take out and solidify by cooling.
- the solidified polymer is pulverized with a sample mill (SK-M2 type, manufactured by Kyoritsu Riko Co., Ltd.) and divided into sieves V so that the JIS standard opening 350 ⁇ m passes but 150 ⁇ m does not pass.
- a prepolymer granule having an average particle size of 0.25 mm was obtained (granulation step).
- Table 1 shows the catalyst activity ratio of Catalysts 1 and 2, the obtained polyester prepolymers, and the physical properties of the polyester after solid-phase polycondensation. [0073] (Example 2)
- Example 1 an ethylene glycol solution of orthophosphoric acid: (concentration 1.6 by weight 0/0 as phosphorus atom), second Esuterui spoon reactor mosquito also the transfer pipe into the polycondensation tank Sansani ⁇ Ni The same procedure as in Example 1 was conducted, except that an amount of 12 ppm by weight as phosphorus was continuously added to the obtained polyester from a location upstream from the location where antimony was added. The results are shown in Table 1.
- Example 1 the titanium-silica mixed catalyst prepared above instead of the ethylene glycol solution of diantimony triacid was added in an amount of 16 ppm by weight as titanium and 46 ppm by weight as silica based on the polyester obtained.
- the procedure was the same as Example 1 except that the addition was continuously performed. The results are shown in Table 1.
- Example 3 instead of an ethylene glycol solution of ammonium metatungstate, an ethylene glycol solution of tetra-n-butyl titanate (concentration: 0.15% by weight as titanium atom) was used as titanium with respect to the obtained polyester. The same operation as in Example 3 was conducted except that an amount of 4 ppm by weight was continuously added. The results are shown in Table 1.
- Example 1 was carried out in the same manner as Example 1 except that the ethylene glycol solution of diantimony trioxide was added to the gas phase part of the second ester-acid reactor. Table the results
- Example 1 The same procedure as in Example 1 was performed except that the addition site of the ethylene glycol solution of diantimony trioxide in Example 1 was replaced with a pre-polymer extraction pipe after the melt polycondensation reaction. The results are shown in Table 1.
- Example 6 instead of an ethylene glycol solution of ammonium metatungstate, an ethylene glycol solution of tetra-n-butyl titanate (concentration: 0.15% by weight as titanium atom) was used as titanium with respect to the obtained polyester. 8 ppm by weight Continuously it has ⁇ Ka ⁇ ethylene glycol solution of magnesium acetate acid tetrahydrate in place of the ethylene glycol solution of Sansani ⁇ two antimony (concentration: 0.
- magnesium acetate E chill acid phosphate mixed exchange catalyst Warini of magnesium acetate tetrahydrate ethylene glycol solution (concentration: 0.030 wt 0/0 as a magnesium atom)) and dibutyl phosphate Ethylene Amount of 4 ppm by weight for magnesium and 5 ppm by weight for phosphorus with respect to the polyester prepolymer from which a mixed solution (magnesium acetate dibutyl phosphate mixed catalyst) of glycol solution (concentration: 0.040% by weight as phosphorus atom) is obtained was carried out in the same manner as in Example 7 except that was continuously added. The results are shown in Table 1.
- Example 7 the amount of tetra-butyl titanate added in the ethylene glycol solution added to the first ester tank was changed to 4 wt ppm as titanium with respect to the obtained polyester, and magnesium acetate was added.
- titanium, magnesium, and polyester prepolymers that can be used to obtain an ethylene glycol diluted solution (concentration: 0.020% by weight as titanium atom) of the titanium magnesium phosphorus synthesis catalyst prepared above.
- the same operation as in Example 7 was conducted except that amounts of 4 ppm by weight, 2 ppm by weight, and 3 ppm by weight were successively added as phosphorus. The results are shown in Table 1.
- Example 1 The same procedure as in Example 1 was carried out except that no ethylene glycol solution of diantimony triacid was added. The results are shown in Table 1.
- Example 2 The same procedure as in Example 2 was conducted except that no ethylene glycol solution of ammonium metatungstate was added. The results are shown in Table 1.
- Example 1 the place where the ethylene glycol solution of ammonium metatungstate was added was replaced by the place where the ethylene glycol solution of triantimony trioxide was added in Example 1, and the ethylene glycol solution of diantimony trioxide was added.
- the same procedure as in Example 1 was carried out except that the addition site was changed to the addition site of the ethylene glycol solution of ammonium metatandastate in Example 1. The results are shown in Table 1.
- Example 1 was carried out in the same manner as Example 1 except that the ethylene glycol solution of diantimony triacid was changed to an ethylene glycol solution of tetra-n-butyl titanate.
- the catalyst activity ratio of the catalyst component corresponding to catalyst 2 is high, the solid phase polycondensation reaction rate was low.
- TiZsi Titanium-silica mixed catalyst
- Mg / DBP Magnesium acetate dibutyl phosphate mixed catalyst
- Ti / Mg / P Titanium Magnesium Phosphorus synthesis catalyst
- MSP transfer pipe Transfer pipe from the second esterification tank to the melt polycondensation tank
- a high-molecular-weight, high-quality polyester having utility as a packaging material such as bottles and films can be produced in a relatively short solid-phase polycondensation time without using a complicated melt polycondensation reaction apparatus. , Can contribute to improving polyester productivity
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- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Polyesters Or Polycarbonates (AREA)
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
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EP06714221.6A EP1854820B1 (en) | 2005-02-25 | 2006-02-21 | Process for continuous production of polyester, polyester prepolymer granule and polyester |
US11/817,190 US20090011236A1 (en) | 2005-02-25 | 2006-02-21 | Process for Continuous Production of Polyester, Polyester Prepolymer Granule and Polyester |
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JP2005051460 | 2005-02-25 | ||
JP2005-051460 | 2005-02-25 |
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WO2006090708A1 true WO2006090708A1 (ja) | 2006-08-31 |
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PCT/JP2006/303081 WO2006090708A1 (ja) | 2005-02-25 | 2006-02-21 | ポリエステルの連続的製造方法、ポリエステルプレポリマー粒状体及びポリエステル |
Country Status (6)
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US (1) | US20090011236A1 (ja) |
EP (1) | EP1854820B1 (ja) |
KR (1) | KR20070108385A (ja) |
CN (1) | CN101128508A (ja) |
TW (1) | TW200704672A (ja) |
WO (1) | WO2006090708A1 (ja) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2008016466A2 (en) * | 2006-07-28 | 2008-02-07 | Eastman Chemical Company | Multiple feeds of catalyst metals to a polyester production process |
Families Citing this family (6)
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KR20080036640A (ko) | 2005-09-01 | 2008-04-28 | 미쓰비시 가가꾸 가부시키가이샤 | 폴리에스테르의 제조 방법 |
US8563677B2 (en) | 2006-12-08 | 2013-10-22 | Grupo Petrotemex, S.A. De C.V. | Non-precipitating alkali/alkaline earth metal and aluminum solutions made with diols having at least two primary hydroxyl groups |
DE102012003417A1 (de) * | 2012-02-17 | 2013-08-22 | Uhde Inventa-Fischer Gmbh | Verfahren zur Herstellung eines hochmolekularen, heteroaromatischen Polyesters oder Copolyesters |
SG10201913407TA (en) | 2015-11-20 | 2020-03-30 | Globalwafers Co Ltd | Manufacturing method of smoothing a semiconductor surface |
CN111423566B (zh) * | 2019-12-31 | 2023-03-28 | 浙江东太新材料有限公司 | 钛基聚酯复合材料的制备方法 |
CN113896869B (zh) * | 2021-12-10 | 2022-04-19 | 江苏新视界先进功能纤维创新中心有限公司 | 在连续聚合装置上制备色相品质良好的环保pet聚酯的方法 |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
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US6160085A (en) * | 1998-05-06 | 2000-12-12 | Mitsubishi Chemical Corporation | Polyester and process for its production |
JP2001172373A (ja) * | 1999-12-17 | 2001-06-26 | Toyobo Co Ltd | ポリエステル樹脂、それからなる中空成形体、シ−ト状物及び延伸フイルム |
JP2004224932A (ja) * | 2003-01-23 | 2004-08-12 | Mitsubishi Rayon Co Ltd | ポリエステル樹脂組成物およびその製造方法 |
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TWI311995B (en) * | 2002-08-05 | 2009-07-11 | Mitsubishi Chemical Corporatio | Polyester resin and its production process |
JP4167159B2 (ja) * | 2002-10-02 | 2008-10-15 | 三菱化学株式会社 | ポリエステル樹脂の製造方法 |
JP2004285350A (ja) * | 2003-03-04 | 2004-10-14 | Toyobo Co Ltd | ポリエステル樹脂の製造方法および得られたポリエステル樹脂、ポリエステル樹脂組成物 |
-
2006
- 2006-02-21 CN CNA2006800059206A patent/CN101128508A/zh active Pending
- 2006-02-21 KR KR1020077019432A patent/KR20070108385A/ko not_active Application Discontinuation
- 2006-02-21 US US11/817,190 patent/US20090011236A1/en not_active Abandoned
- 2006-02-21 EP EP06714221.6A patent/EP1854820B1/en not_active Expired - Fee Related
- 2006-02-21 WO PCT/JP2006/303081 patent/WO2006090708A1/ja active Application Filing
- 2006-02-24 TW TW095106316A patent/TW200704672A/zh unknown
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6160085A (en) * | 1998-05-06 | 2000-12-12 | Mitsubishi Chemical Corporation | Polyester and process for its production |
JP2001172373A (ja) * | 1999-12-17 | 2001-06-26 | Toyobo Co Ltd | ポリエステル樹脂、それからなる中空成形体、シ−ト状物及び延伸フイルム |
JP2004224932A (ja) * | 2003-01-23 | 2004-08-12 | Mitsubishi Rayon Co Ltd | ポリエステル樹脂組成物およびその製造方法 |
Non-Patent Citations (1)
Title |
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See also references of EP1854820A4 * |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2008016466A2 (en) * | 2006-07-28 | 2008-02-07 | Eastman Chemical Company | Multiple feeds of catalyst metals to a polyester production process |
WO2008016466A3 (en) * | 2006-07-28 | 2008-04-10 | Eastman Chem Co | Multiple feeds of catalyst metals to a polyester production process |
Also Published As
Publication number | Publication date |
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CN101128508A (zh) | 2008-02-20 |
EP1854820A1 (en) | 2007-11-14 |
EP1854820B1 (en) | 2014-06-11 |
EP1854820A4 (en) | 2010-04-07 |
TW200704672A (en) | 2007-02-01 |
US20090011236A1 (en) | 2009-01-08 |
KR20070108385A (ko) | 2007-11-09 |
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