WO2021117795A1 - ポリアリーレンスルフィド、その精製方法および製造方法 - Google Patents
ポリアリーレンスルフィド、その精製方法および製造方法 Download PDFInfo
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- WO2021117795A1 WO2021117795A1 PCT/JP2020/045955 JP2020045955W WO2021117795A1 WO 2021117795 A1 WO2021117795 A1 WO 2021117795A1 JP 2020045955 W JP2020045955 W JP 2020045955W WO 2021117795 A1 WO2021117795 A1 WO 2021117795A1
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- pas
- polyarylene sulfide
- carbon atoms
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- porous particles
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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
- C08G75/00—Macromolecular compounds obtained by reactions forming a linkage containing sulfur with or without nitrogen, oxygen, or carbon in the main chain of the macromolecule
- C08G75/02—Polythioethers
- C08G75/0204—Polyarylenethioethers
- C08G75/025—Preparatory processes
- C08G75/0259—Preparatory processes metal hydrogensulfides
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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
- C08G75/00—Macromolecular compounds obtained by reactions forming a linkage containing sulfur with or without nitrogen, oxygen, or carbon in the main chain of the macromolecule
- C08G75/02—Polythioethers
- C08G75/0204—Polyarylenethioethers
- C08G75/0277—Post-polymerisation treatment
- C08G75/0281—Recovery or purification
Definitions
- the present invention relates to a method for purifying polyarylene sulfide (hereinafter, may be abbreviated as PAS) and a method for producing it. More specifically, it is possible to reduce the corrosiveness to the manufacturing equipment and the mold at the time of molding as compared with the conventional purification method using various strong acids (hydrochloric acid, sulfuric acid, etc.), and to improve the quality of PAS. Regarding possible purification methods and manufacturing methods. Another object of the present invention is to provide PAS suitable as a material for a wide range of applications such as various molding materials, films, fibers, electric / electronic parts, automobile parts, and paints.
- PAS polyarylene sulfide
- Typical polyphenylene sulfides among PAS are usually N-methyl-2-pyrrolidone, N, N-dimethylacetamide, as described in Patent Document 1 and the like.
- Alkali metal sulfide typified by sodium sulfide, or alkali metal sulfide typified by sodium hydroxide and water typified by sodium hydroxide in a relatively highly polar organic solvent such as N-methyl- ⁇ -caprolactam. It can be obtained by a method of reacting an alkali metal oxide with a polyhalo aromatic compound typified by p-dichlorobenzene or the like (see Patent Document 1).
- the polymerization reaction is usually carried out under high temperature pressurization and alkaline conditions, and as the polymerization reaction progresses, sodium chloride is produced, and the so-called crude reaction products after the polymerization reaction include at least PAS and alkali metal halides.
- Ar is an aryl group having a halogen atom
- R 1 represents a hydrogen atom or an alkyl group having 1 to 3 carbon atoms or a cyclohexyl group
- R 2 represents an alkylene group having 3 to 5 carbon atoms
- X represents a hydrogen atom or an alkali metal atom.
- a compound represented by a -NR 1 R 2 COOX group may be referred to as a carboxyalkylamino group (hereinafter, may be referred to as a carboxyalkylamino group-containing compound).
- By-products typified by such as are contained.
- X represents a hydrogen atom or an alkali metal atom.
- This compound is abbreviated as “CP-MABA", and particularly when X is a hydrogen atom, "CP-MABA (" Hydrogen type) ”, the case of alkali metal atom may be abbreviated as“ CP-MABA (alkali metal salt type) ”, and in particular, when X is a sodium atom, it may be abbreviated as“ CP-MABA (Na salt type) ”).
- the crude reaction product after the polymerization reaction is taken out into a suitable container, and the solvent contained therein is suitable by a suitable means (vacuum distillation method, centrifugation method, screw decanter method, vacuum filtration method, pressure filtration method, etc.). Depending on the method (selectable method), it can be separated and recovered (here, this operation is referred to as "desolvation") and reused, or if necessary, further purified and reused.
- a suitable means vacuum distillation method, centrifugation method, screw decanter method, vacuum filtration method, pressure filtration method, etc.
- the mixture containing PAS (hereinafter referred to as crude PAS) contained in the crude reaction product is generally repeatedly washed with water and filtered, and mainly salt or salt or the like.
- PAS can be obtained by removing impurities such as alkaline substances and then drying.
- PAS thus obtained is used in fibers, films, paints, compounds for injection molding materials, fiber-reinforced composite materials, etc. because of its excellent chemical resistance, electrical properties, and mechanical properties.
- PAS having excellent reactivity with epoxy silane and functional group-containing elastomer (hereinafter, simply referred to as "reactivity") by increasing the amount of carboxy group at the end of the polymer chain is desired.
- the problems to be solved by the present invention are a method for purifying PAS having excellent reactivity and a slow crystallization rate, and a method for producing PAS having excellent reactivity and a slow crystallization rate including the step. , And to provide PAS which is excellent in reactivity and has a slow crystallization rate.
- the inventors of the present application made the mixture containing the crude PAS porous by contacting with a specific organic solvent and water, and then the porous crude PAS, water and carbon dioxide.
- the residual by-products typified by the carboxyalkylamino group-containing compound to a specific content by a purification method in which gas or carbonated water is brought into contact
- PAS having excellent reactivity and a slow crystallization rate is obtained.
- the present invention is a step of obtaining a mixture containing crude PAS by desolving a crude reaction product containing PAS obtained by reacting a polyhalo aromatic compound with a sulfide agent in an organic polar solvent.
- It has a step (3) of contacting with water, and has
- the step (2) includes a step of contacting with an oxygen atom-containing solvent having 1 to 3 carbon atoms (2Ss) and a step of contacting with water (2Sw) at least once.
- the proportion of the compound (1) represented by the following structural formula (1) contained in the porous particles after the step (3) is in the range of more than 1000 [ppm] to 3000 [ppm] or less. PAS purification method.
- Ar is an aryl group having a halogen atom
- R 1 represents a hydrogen atom or an alkyl group having 1 to 3 carbon atoms or a cyclohexyl group
- R 2 represents an alkylene group having 3 to 5 carbon atoms
- X represents a hydrogen atom or an alkali metal atom
- the present invention also relates to a method for producing PAS, which comprises a step of purifying PAS by the purification method described above.
- the present invention is a porous particle having a specific surface area of 10 [m 2 / g] or more.
- PAS characterized in that the ratio of the content of the compound (1) represented by the following structural formula (1) is in the range of more than 1000 [ppm] to 3000 [ppm] or less.
- Ar is an aryl group having a halogen atom
- R 1 represents a hydrogen atom or an alkyl group having 1 to 3 carbon atoms or a cyclohexyl group
- R 2 represents an alkylene group having 3 to 5 carbon atoms
- X represents a hydrogen atom or an alkali metal atom
- a method for purifying PAS having excellent reactivity and a slow crystallization rate a method for producing PAS having excellent reactivity and a slow crystallization rate including the step, and reactivity. It is possible to provide PAS which is excellent in quality and has a slow crystallization rate.
- the purification method of the present invention is a step of obtaining a mixture containing crude PAS by desolving a crude reaction product containing PAS obtained by reacting a polyhalo aromatic compound with a sulfidizing agent in an organic polar solvent. It has (1).
- PAS is usually obtained by reacting at least one polyhaloaromatic compound with at least one sulfidizing agent under appropriate polymerization conditions in an organic polar solvent typified by N-methyl-2-pyrrolidone or the like. It is synthesized.
- the polyhaloaromatic compound used in the present invention is, for example, a halogenated aromatic compound having two or more halogen atoms directly bonded to an aromatic ring, and specifically, p-dichlorobenzene, o-.
- Dihalo-aromatic compounds such as dibrom benzophenone, dichlorodiphenyl ether, dibrom diphenyl ether, dichlorodiphenyl sulfide, dibrom diphenyl sulfide, dichlorobiphenyl, dibrombiphenyl and
- a polyhaloaromatic compound having three or more halogen substituents in one molecule may be used as a branching agent, if desired.
- polyhalo aromatic compounds include 1,2,4-trichlorobenzene, 1,3,5-trichlorobenzene, 1,4,6-trichloronaphthalene and the like.
- polyhaloaromatic compounds having a functional group having an active hydrogen such as an amino group, a thiol group and a hydroxyl group
- a functional group having an active hydrogen such as an amino group, a thiol group and a hydroxyl group
- 2,6-dichloroaniline and 2,5-dichloroaniline 2,6-dichloroaniline and 2,5-dichloroaniline.
- 2,4-Dichloroaniline, 2,3-dichloroaniline and other dihaloanilines 2,3,4-trichloroaniline, 2,3,5-trichloroaniline, 2,4,6-trichloroaniline, 3, Trihaloanilines such as 4,5-trichloroaniline; dihaloaminodiphenyl ethers such as 2,2'-diamino-4,4'-dichlorodiphenyl ether, 2,4'-diamino-2', 4-dichlorodiphenyl ether And compounds in which the amino group is replaced with a thiol group or a hydroxyl group in a mixture thereof and the like are exemplified.
- active hydrogen-containing polyhalo in which the hydrogen atom bonded to the carbon atom forming the aromatic ring in these active hydrogen-containing polyhaloaromatic compounds is replaced with another inactive group, for example, a hydrocarbon group such as an alkyl group.
- Aromatic compounds can also be used.
- the active hydrogen-containing dihaloaromatic compound is preferable, and dichloroaniline is particularly preferable.
- Examples of the polyhaloaromatic compound having a nitro group include mono- or dihalonitrobenzenes such as 2,4-dinitrochlorobenzene and 2,5-dichloronitrobenzene; 2-nitro-4,4'-dichlorodiphenyl ether and the like.
- the alkali metal sulfide used in the present invention includes lithium sulfide, sodium sulfide, rubidium sulfide, cesium sulfide, and mixtures thereof.
- Such alkali metal sulfides can be used as hydrates, aqueous mixtures or anhydrides.
- the alkali metal sulfide can also be derived by the reaction between the alkali metal hydroxide and the alkali metal hydroxide.
- alkali metal hydroxide may be added in order to react with the alkali metal hydrosulfide and the alkali metal thiosulfate which are usually present in a trace amount in the alkali metal sulfide.
- organic polar solvent used in the present invention examples include N-methyl-2-pyrrolidone, formamide, acetamide, N-methylformamide, N, N-dimethylacetamide, 2-pyrrolidone, N-methyl- ⁇ -caprolactam and ⁇ -caprolactam.
- Nitriles; ketones such as methylphenylketone and mixtures thereof can be mentioned.
- the polymerization conditions of the above-mentioned sulfidizing agent and the polyhalo aromatic compound are generally a temperature of 200 to 330 ° C., and the pressure is substantially the same as that of the polymerization solvent and the polyhalo aromatic compound which is a polymerization monomer.
- the range should be such that it is retained in the liquid layer, and is generally selected from the range of 0.1 to 20 MPa, preferably 0.1 to 2 MPa.
- the reaction time varies depending on the temperature and pressure, but is generally in the range of 10 minutes to 72 hours, preferably 1 hour to 48 hours.
- the present invention also includes a form obtained by reacting the crude reaction product in the presence of a sulfidizing agent and an organic polar solvent while continuously or intermittently adding a polyhalo aromatic compound and an organic polar solvent. To do.
- the crude reaction product containing PAS obtained by the polymerization reaction is used by an appropriate means (vacuum distillation method, centrifugation method, screw decanter method, vacuum filtration method, pressure filtration method, etc.). Can be selected) to "desolvent" to separate and remove the organic protic solvent, after which a mixture containing crude PAS can be obtained.
- the degree of separation and removal of the organic polar solvent is not particularly limited, but the ratio of solid content (solid content concentration) in the mixture is preferably 40 parts by mass or more, more preferably 50 parts by mass with respect to 100 parts by mass of the mixture. More than parts, more preferably 55 parts by mass or more.
- the upper limit is not limited, but is preferably 100 parts by mass or less, more preferably less than 100 parts by mass, and further preferably 99 parts by mass or less.
- the purification method of the present invention subsequently comprises the step (2) of purifying the mixture containing the crude PAS into porous particles having a specific surface area of 30 [m 2 / g] or more.
- the step (2) includes a step of contacting with an oxygen atom-containing solvent having 1 to 3 carbon atoms (2Ss) and a step of contacting with water (2Sw) at least once.
- the step (2Ss) is a step of using an oxygen atom-containing solvent having 1 to 3 carbon atoms to bring it into contact with a mixture containing crude PAS for cleaning.
- the temperature at which the oxygen atom-containing solvent having 1 to 3 carbon atoms is added is not particularly limited, but is preferably 10 ° C. or higher, more preferably 20 ° C. or higher, preferably 90 ° C. or lower, and more preferably 70 ° C. or lower.
- the amount of the solvent used for one washing is not particularly limited, but is preferably 20 parts by mass or more, more preferably 50 parts by mass or more, and further preferably 100 parts by mass or more with respect to 100 parts by mass of PAS. Therefore, it is preferably 5000 parts by mass or less, more preferably 1800 parts by mass or less, and further preferably 600 parts by mass or less.
- the step (2Sw) is a step of adding an appropriate amount of water to the mixture obtained in the previous step (1) and containing at least crude PAS, contacting the mixture, and washing the mixture.
- the temperature at which water is added is not particularly limited, but is preferably in the range of 10 ° C. or higher, more preferably 20 ° C. or higher, preferably 120 ° C. or lower, more preferably 100 ° C. or lower, still more preferably 80 ° C. or lower. .. After washing, it is preferably solid-liquid separated by filtration or the like to form a cake-like product.
- the amount of water used for one washing is not particularly limited, but is preferably from 20 parts by mass or more, more preferably 50 parts by mass or more, and further preferably 100 parts by mass or more with respect to 100 parts by mass of PAS. It is preferably 10000 parts by mass or less, more preferably 5000 parts by mass or less, and further preferably 2000 parts by mass or less.
- the order of the steps (2Ss) and the step (2Sw) is not particularly limited, and the step (2Sw) of contacting the mixture containing the crude PAS with water to wash the mixture is performed. Then, the mixture containing the crude PAS may be washed by contacting it with an oxygen atom-containing solvent having 1 to 3 carbon atoms (2Ss), or after performing the step (2Ss), the step (2Ss) may be performed. 2Sw) may be performed. Each step can also be carried out collectively or alternately, any one or more times. After performing the step (2Ss) or the step (2Sw) and before performing the next step, the water used for washing or the oxygen atom-containing solvent having 1 to 3 carbon atoms should be removed by solid-liquid separation. Is preferable.
- examples of the oxygen atom-containing solvent having 1 to 3 carbon atoms to be brought into contact with the mixture containing crude PAS include at least one selected from the group consisting of alcohol-based solvents and ketone-based solvents.
- alcohol-based solvents also referred to as alcohol solvents
- examples of alcohol-based solvents include methyl alcohol, ethyl alcohol, n-propyl alcohol, isopropyl alcohol, n-butyl alcohol, isobutyl alcohol, t-butyl alcohol, ethylene glycol, propylene glycol, trimethylolpropane, and benzyl.
- Alcohols with 10 or less carbon atoms such as alcohols; 2-methoxyethyl alcohol, 2-ethoxyethyl alcohol, 1-methoxy-2-propyl alcohol, 1-ethoxy-2-propyl alcohol, 3-methoxy-1-butyl alcohol , 2-Isopropoxyethyl alcohols and other alcohols with 10 or less carbon atoms containing ether bonds; 3-hydroxy-2-butanone and other alcohols with 10 or less carbon atoms; methyl hydroxyisobutyrate and the like
- An example is an alcohol containing such an ester group and having 10 or less carbon atoms.
- ketone solvent also referred to as a ketone solvent
- examples of the ketone solvent include acetone, methyl ethyl ketone, cyclohexanone, ⁇ -butyl lactone and N-methylpyrrolidinone.
- a monohydric alcohol having 10 or less carbon atoms because the residual carboxyalkylamino group-containing compound can be efficiently removed, and further, a monohydric alcohol having 3 or less carbon atoms is preferable. preferable.
- the step (2Ss) may be carried out after preparing an aqueous solution obtained by adding water to an oxygen atom-containing solvent having 1 to 3 carbon atoms and lowering the concentration.
- the concentration of the oxygen atom-containing solvent having 1 to 3 carbon atoms in the aqueous solution is not particularly limited, but is preferably in the range of 90 parts by mass or less with respect to 100 parts by mass of the aqueous solution. It is more preferably in the range of 85 parts by mass or less, preferably in the range of 25 parts by mass or more, and more preferably in the range of 45 parts by mass or more.
- the step of contacting the crude PAS with an oxygen atom-containing solvent having 1 to 3 carbon atoms (2Ss) and the step of contacting the crude PAS with water (2Sw) are repeated once or a plurality of times, respectively.
- the crude PAS has a specific surface area of 30 [m 2 / g] or more, preferably 43 [m 2 / g] or more, more preferably 60 [m 2 / g] or more, and preferably 200 [m 2 / g] or less. , More preferably, porous particles in the range of 120 [m 2 / g] or less.
- the crude PAS is a porous particle having such a range of specific surface area because the carboxyalkylamino group-containing compound in the crude PAS can be easily reduced to a desired range.
- the purification method of the present invention subsequently includes a step (3) of bringing the obtained porous particles into contact with carbonated water.
- the conditions for bringing the porous particles obtained in the previous step (2) into contact with carbonated water are preferably 10 ° C. or higher, more preferably 20 ° C. or higher, preferably 100 ° C. or lower, more preferably. Is in the range up to 80 ° C. and the pressure (gauge pressure) is smaller than 0.1 MPa, preferably in the range of 0.05 MPa or less, and more preferably under atmospheric pressure.
- the amount of carbonated water used for contact with the porous particles is also not particularly limited, but the porous particles can be brought into good contact with the carbonated water, and the purification efficiency becomes more preferable. Therefore, the porous particles With respect to 100 parts by mass, preferably 50 parts by mass or more, more preferably 100 parts by mass or more, further preferably 200 parts by mass or more, preferably 2000 parts by mass or less, more preferably 1000 parts by mass or less, still more preferably 800 parts by mass. It is in the range of parts by mass or less.
- one of the advantages of the present invention is that when the purification method using carbonated water of the present invention is used, there is almost no corrosion on metals under normal purification temperature conditions (100 ° C. or lower), and the current apparatus can be used.
- a relatively inexpensive material having SUS304 level corrosion resistance can withstand corrosion, so there is only an advantage in equipment cost due to the material aspect of the equipment compared to other acids.
- one of the advantages of the present invention is that when other acids remain in the PAS (particularly chlorine ions and sulfate ions tend to remain in the polymer), mold corrosion during molding and deterioration of the physical properties of the molded product are deteriorated.
- the purification method using carbonated water of the present invention it is easy to remove even in the washing step which is a later step, and it decomposes and scatters from the PAS even in the drying step, so that it is like other acids. Mold corrosion and deterioration of the physical properties of molded products are unlikely to occur.
- one of the advantages of the present invention is that when a strong acid other than carbonated water is used, a large amount of water and a large number of washings are required after washing with the strong acid in order to remove the acid remaining in the PAS.
- the amount of water used after washing with carbonated water is small and the number of washings can be reduced. It can be said that it is a suitable method not only in terms of process capacity but also in terms of environmental measures.
- carbon dioxide gas is blown into a closed container or device, and the PAS is contacted in an aqueous solution in which the solubility of carbonic acid is controlled by controlling the pressure and temperature in the system for an appropriate time or longer (for example, 5 minutes or longer).
- It is a purification method characterized by converting a molecular end from a basic type end (SNa type end) to an acidic type end (SH type end), and the SNa group existing at the molecular chain end of PAS is converted into an SH group. , Affinity with other resins increases.
- the concentration of carbon dioxide (derived carbonate ion) in carbonated water depends on the solubility of carbon dioxide in water, and more specifically follows Henry's law at its temperature and pressure.
- carbon dioxide gas may be bubbled or press-fitted into water in an open container, a closed container, or a pipe, or continuously using a hollow fiber membrane module or the like. Carbon dioxide gas may be dissolved in water.
- the solid content concentration in the system when the carbonated water of the present invention is brought into contact with the porous particles for purification is preferably a ratio of 1 to 50% by weight.
- the PAS particles are in good contact with the carbonated water, and the purification efficiency is preferable, which is more preferable.
- the amount of carbonated water required for purification is also not particularly limited, but may be preferably 50 parts by mass or more, more preferably 100 parts by mass or more, still more preferably 200 parts by mass or more, based on 100 parts by mass of PAS. It may be preferably in the range of 10000 parts by mass or less, more preferably 5000 parts by mass or less, and further preferably 2000 parts by mass or less. If the amount of carbonated water is within this range, the PAS particles are in good contact with the carbonated water, and the purification efficiency is preferable, which is more preferable.
- the contact between the carbonated water and the porous particles of PAS can be performed in an open container having a stirring blade inside the container and a filter for filtration at the bottom. It is not necessary to carry out in a container having a closed type or a container having a mixing function that can be closed, but of course, it can be carried out in such a container.
- a crude reaction product containing PAS obtained by reacting a polyhaloaromatic compound with a sulfide agent in an organic polar solvent is desolved, and then the organic solvent is used.
- the present invention relates to a method for purifying PAS, which comprises contacting PAS with a specific surface area of 30 [m 2 / g] or more, and bringing the obtained porous particles into contact with carbonated water. is there.
- one of the other aspects of the present invention relates to a method for producing PAS, which comprises a step of purifying PAS by the purification method. That is, in the invention relating to the method for producing the PAS, the crude PAS is prepared by desolving the crude reaction product containing the PAS obtained by reacting the polyhalo aromatic compound with the sulfide agent in an organic polar solvent. A step of obtaining a mixture containing the crude PAS, a step of purifying the mixture containing the crude PAS to form the crude PAS into porous particles having a specific surface area of 30 [m 2 / g] or more, the obtained porous particles and carbonated water.
- the step (3) of contacting includes a step of contacting with an oxygen atom-containing solvent having 1 to 3 carbon atoms (2Ss) and a step of contacting with water (2Sw) at least once.
- the proportion of the compound (1) represented by the structural formula (1) contained in the porous particles after the step (3) is in the range of more than 1000 [ppm] to 3000 [ppm] or less in the PAS. It is characterized by being.
- the PAS obtained through the purification method or the production method of the present invention may be dried as it is, or may be further washed with water or an organic solvent as appropriate, then solid-liquid separated and dried.
- Drying is performed by heating to a temperature at which a solvent such as water evaporates. Drying may be carried out under vacuum, in air or in an inert atmosphere such as nitrogen.
- the PAS obtained through the above-mentioned purification method or production method of the present invention (sometimes simply referred to as "purified PAS") has the following characteristics. That is, The purified PAS of the present invention has a specific surface area of 10 [m 2 / g] or more, preferably 15 [m 2 / g] or more, more preferably 20 [m 2 / g] or more, and preferably 180. Porous particles in the range of [m 2 / g] or less, more preferably 150 [m 2 / g] or less, still more preferably 100 [m 2 / g] or less, and particularly preferably 50 [m 2 / g] or less. Is.
- the ratio of the content of the compound (1) represented by the structural formula (1) is more than 1000 [ppm], preferably 1100 [ppm] to 3000 in the PAS on a mass basis. It is in the range of [ppm] or less, preferably 2000 [ppm] or less.
- the purified PAS of the present invention tends to have a slow crystallization rate.
- the crystallization rate is not particularly limited, but the isothermal crystallization rate is preferably 4 [minutes] or more, more preferably 5 [minutes] or more, 9 [minutes] or less, preferably 8 [minutes] or less.
- the range is up to.
- the isothermal crystallization temperature is the temperature at which the sample is melted at 350 ° C./3 minutes using a differential scanning calorimetry device and then rapidly cooled from 350 ° C. to 240 ° C. (210 ° C./min). It is a measured value when it was held at 240 ° C.) for 15 minutes.
- the PAS obtained through the purification method or production method of the present invention can be used as it is for various molding materials as in the conventional case, but can be thickened by heat treatment in air or oxygen-enriched air or under reduced pressure. Therefore, after performing such a thickening operation as necessary, it may be used for various molding materials and the like.
- This heat treatment temperature varies depending on the treatment time and the atmosphere to be treated, and therefore cannot be unconditionally specified, but it is usually preferably performed at 180 ° C. or higher. If the heat treatment temperature is less than 180 ° C., the thickening rate is very slow and the productivity is poor, which is not preferable.
- the heat treatment may be carried out in a molten state at a temperature equal to or higher than the melting point of the polymer using an extruder or the like. However, it is preferable to carry out the process at a melting point of 100 ° C. or lower because of the possibility of deterioration of the polymer or workability.
- the PAS obtained by the present invention can be mixed with a filler or other resin, melt-kneaded, directly or once molded into pellets, and then various types such as injection molding, extrusion molding, compression molding, and blow molding, as in the conventional case.
- a filler or other resin melt-kneaded, directly or once molded into pellets, and then various types such as injection molding, extrusion molding, compression molding, and blow molding, as in the conventional case.
- the melt processing method it is possible to obtain a molded product having excellent heat resistance, molding processability, dimensional stability and the like.
- the filler include a fibrous filler and an inorganic filler.
- a ring agent can be contained.
- the following synthetic resin and elastomer can be mixed and used. Examples of these synthetic resins include polyester, polyamide, polyimide, polyetherimide, polycarbonate, polyphenylene ether, polysulphon, polyethersulphon, polyetheretherketone, polyetherketone, polyarylene, polyethylene, polypropylene, polytetrafluorinated ethylene, and the like.
- Examples thereof include polydifluorinated ethylene, polystyrene, ABS resin, epoxy resin, silicone resin, phenol resin, urethane resin, liquid crystal polymer and the like, and examples of the elastomer include polyolefin rubber, fluororubber, silicone rubber and the like.
- the molded product obtained by melt-molding the PAS of the present invention or the resin composition containing the same is excellent in heat resistance, dimensional stability, etc. like the PPS obtained by the conventional method.
- Injection molding of electrical and electronic parts such as goods, automobile parts such as lamp reflectors and various electrical parts, interior materials such as various buildings, aircraft and automobiles, and precision parts such as OA equipment parts, camera parts and clock parts.
- -It can be widely used as a compression molded product or an extrusion molded / drawn molded product such as fiber, film, sheet, pipe, etc.
- the crystallization rate is slower than the PPS obtained by the conventional method, it is possible to delay the solidification of the gate portion and apply pressure to the thick portion at the time of injection molding, thereby eliminating the conventional filling shortage. , It is possible to prevent a decrease in strength. From this, it is particularly suitable for a large-sized or thick-walled molded product, preferably an injection-molded product.
- a large-sized or thick-walled molded product preferably an injection-molded product.
- sample preparation CP-MABA in the filtrate was prepared and measured by adding the mobile phase as it was.
- Dilute hydrochloric acid was added to the aqueous solution to adjust the pH of the aqueous solution to 1 or less.
- CP-MABA became a hydrochloride and remained in the aqueous solution, so chloroform was added to the aqueous solution to extract p-chlorophenol as a by-product.
- the chloroform phase in which p-chlorophenol was dissolved was discarded.
- the degree of increase in viscosity was calculated as a magnification from the ratio of the melt viscosity V6 after the addition / the melt viscosity V6 before the addition. The larger the degree of increase in viscosity, the higher the reactivity and the better.
- the resin component discharge amount is 30 kg / hr
- the screw rotation speed is 220 rpm
- the set resin temperature is set to 320 ° C.
- melt-kneading is performed, and the strand-shaped material discharged from the discharge port is cut.
- PPS compound pellets were obtained.
- the pellets were supplied to an injection molding machine (SE75D-HP) manufactured by Sumitomo Heavy Industries, which was set to a cylinder temperature of 310 ° C., and injection molding was performed under the following conditions. That is, using a washer mold having 40 cavities, the minimum molding conditions were set as long as the cavity (C1) at the position closest to the primary sprue was completely filled.
- AA From 100% by mass or less to 90% by mass or more
- B From less than 80% by mass to 70% by mass or more
- C From less than 70% by mass Range of 60% by mass or more
- D Range of less than 60% by mass
- the DCB distilled by azeotrope during dehydration was separated by a decanter and returned to the kettle at any time, and the anhydrous sodium sulfide composition was dispersed in the kettle after the dehydration was completed. Further, the internal temperature was cooled to 160 ° C., NMP 47.492 kg (479 mol) was charged, and the temperature was raised to 185 ° C. When the pressure reached 0.00 MPa, the valve connected to the rectification column was opened, and the temperature was raised to an internal temperature of 200 ° C. over 1 hour. At this time, cooling and valve opening were controlled so that the rectification tower outlet temperature was 110 ° C. or lower.
- the distilled steam of DCB and water was condensed by a condenser, separated by a decanter, and the DCB was returned to the kettle.
- the amount of distilled water was 179 g.
- the internal temperature was raised from 200 ° C. to 230 ° C. over 3 hours, stirred for 1 hour, then raised to 250 ° C. and stirred for 1 hour, and after the reaction was completed, the internal temperature of the autoclave was raised from 250 ° C. to 235 ° C.
- the mixture was cooled to room temperature and sampled to obtain a crude PPS mixture of NV 55%.
- Example 1 400 g of the crude PPS mixture obtained in Synthesis Example 1 and 422 g of an aqueous methanol solution (“Reagent Special Grade” manufactured by Fujifilm Wako Pure Chemical Industries, Ltd.) are placed in a flask, stirred and mixed at 40 ° C. for 30 minutes, and the slurry is filtered under reduced pressure with a Kiriyama funnel. Then, it was compacted from the top, and 422 g of an 80 wt% aqueous methanol solution (80 parts by mass of "Reagent Special Grade” manufactured by Fujifilm Wako Pure Chemical Industries, Ltd. plus 20 parts by mass of water) was poured and filtered in several times. ..
- an aqueous methanol solution (“Reagent Special Grade” manufactured by Fujifilm Wako Pure Chemical Industries, Ltd.)
- the cake prepared by filtration was transferred to a beaker, crushed into powder with a spatula, 422 g of water at 20 ° C. was poured therein, and the cake was stirred and mixed for 30 minutes.
- the slurry was filtered under reduced pressure with a Kiriyama funnel, compacted from above, and 422 g of water at 20 ° C. was poured from above in several portions and filtered.
- the cake was transferred to a beaker, 634 g of carbonated water was poured therein, and the mixture was stirred and mixed for 1 hour.
- the slurry was filtered under reduced pressure with a Kiriyama funnel, compacted from above, and 442 g of carbonated water was poured from above in several portions and filtered.
- the filtered cake was transferred to a vat, crushed into powder with a spatula, and dried at 120 ° C. for 4 hours to obtain purified PPS.
- the obtained purified PPS was measured. The results are shown in Table 1.
- Example 2 400 g of the crude PPS mixture obtained in Synthesis Example 1 and 422 g of an aqueous methanol solution (“Reagent Special Grade” manufactured by Fujifilm Wako Pure Chemical Industries, Ltd.) are placed in a flask, stirred and mixed at 40 ° C. for 30 minutes, and the slurry is filtered under reduced pressure with a Kiriyama funnel. Then, it was compacted from the top, and 422 g of a 50 wt% aqueous methanol solution (50 parts by mass of "Reagent Special Grade” manufactured by Fujifilm Wako Pure Chemical Industries, Ltd. plus 50 parts by mass of water) was poured and filtered in several times. ..
- an aqueous methanol solution (“Reagent Special Grade” manufactured by Fujifilm Wako Pure Chemical Industries, Ltd.)
- the cake prepared by filtration was transferred to a beaker, crushed into powder with a spatula, 442 g of water at 20 ° C. was poured therein, and the cake was stirred and mixed for 30 minutes.
- the slurry was filtered under reduced pressure with a Kiriyama funnel, compacted from above, and 422 g of water at 20 ° C. was poured from above in several portions and filtered.
- the cake was transferred to a beaker, 634 g of carbonated water was poured therein, and the mixture was stirred and mixed for 1 hour.
- the slurry was filtered under reduced pressure with a Kiriyama funnel, compacted from above, and 442 g of carbonated water was poured from above in several portions and filtered.
- the filtered cake was transferred to a vat, crushed into powder with a spatula, and dried at 120 ° C. for 4 hours to obtain purified PPS.
- the obtained purified PPS was measured. The results are shown in Table 1.
- Example 3 400 g of the crude PPS mixture obtained in Synthesis Example 1 and 422 g of an aqueous methanol solution (“Reagent Special Grade” manufactured by Fujifilm Wako Pure Chemical Industries, Ltd.) are placed in a flask, stirred and mixed at 40 ° C. for 30 minutes, and the slurry is filtered under reduced pressure with a Kiriyama funnel. Then, it was compacted from the top, and 422 g of a 30 wt% aqueous methanol solution (30 parts by mass of "Reagent Special Grade” manufactured by Fujifilm Wako Pure Chemical Industries, Ltd. plus 70 parts by mass of water) was poured and filtered in several times. ..
- an aqueous methanol solution (“Reagent Special Grade” manufactured by Fujifilm Wako Pure Chemical Industries, Ltd.)
- the cake prepared by filtration was transferred to a beaker, crushed into powder with a spatula, 442 g of water at 20 ° C. was poured therein, and the cake was stirred and mixed for 30 minutes.
- the slurry was filtered under reduced pressure with a Kiriyama funnel, compacted from above, and 422 g of water at 20 ° C. was poured from above in several portions and filtered.
- the cake was transferred to a beaker, 643 g of carbonated water was poured into the beaker, and the cake was stirred and mixed for 1 hour.
- the slurry was filtered under reduced pressure with a Kiriyama funnel, compacted from above, and 442 g of carbonated water was poured from above in several portions and filtered.
- the cake prepared by filtration was transferred to a vat, crushed into powder with a spatula, and dried at 120 ° C. for 4 hours to obtain purified PPS.
- the obtained purified PPS was measured. The results are shown
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Abstract
Description
前記工程(2)が、炭素原子数1~3の酸素原子含有溶媒と接触させる工程(2Ss)と、水と接触させる工程(2Sw)とをそれぞれ少なくとも1回ずつ行う工程を有し、
工程(3)後の多孔質粒子中に含まれる下記構造式(1)で表される化合物(1)の割合が、1000〔ppm〕超から、3000〔ppm〕以下の範囲であることを特徴とするPASの精製方法。
下記構造式(1)で表される化合物(1)の含有量の割合が、1000〔ppm〕超から、3000〔ppm〕以下の範囲であることを特徴とするPAS
前記工程(2)が、炭素原子数1~3の酸素原子含有溶媒と接触させる工程(2Ss)と、水と接触させる工程(2Sw)とをそれぞれ少なくとも1回ずつ行う工程を有し、
工程(3)後の前記多孔質粒子中に含まれる前記構造式(1)で表される化合物(1)の割合が、該PAS中に1000〔ppm〕超から、3000〔ppm〕以下の範囲であることを特徴とする。
本発明の精製PASは、比表面積が、10〔m2/g〕以上、好ましくは15〔m2/g〕以上、より好ましくは20〔m2/g〕以上であり、そして、好ましくは180〔m2/g〕以下、より好ましくは150〔m2/g〕以下、さらに好ましくは100〔m2/g〕以下、特に好ましくは50〔m2/g〕以下までの範囲の多孔質粒子である。
(1)PPS中のCP-MABAの抽出:NaOH0.05%水溶液をPPSに対して、20倍を入れて、200℃に昇温して30分加熱し、固液分離することで、PPS樹脂中のCP-MABAをろ液に抽出した。
得られたろ液中のCP-MABA濃度は、(1)で作製したろ液サンプルのHPLC測定を行い、下記の方法で作製した標準サンプルと同じ保持時間のピーク面積と検量線とから液中の濃度を求め、算出した。
ろ液中のCP-MABAは、そのまま移動相を加えて調製し測定した。
48%NaOH水溶液83.4g(1.0モル)とN-メチル-2-ピロリドン297.4g(3.0モル)を、撹拌機付き耐圧容器に仕込み、230℃で3時間撹拌した。この撹拌が終了した後、温度230℃のままバルブを開き、放圧し、N-メチル-2-ピロリドンの蒸気圧程度である230℃において0.1MPaまで圧力を低下させ、水を留去した。その後、再び密閉し200℃程度まで温度を低下させた。
よく攪拌した溶液から、1mlをサンプリングし、そこにHPLCの移動相を9ml加え、ろ液を測定サンプルとした。測定サンプルのHPLC測定を行い、下記の方法で作成した標準サンプルと同じ保持時間のピーク面積と検量線とから液中の濃度を求めた。HPLC測定条件は以下の通り。
装置名:株式会社 島津製作所製「高速液体クロマトグラム Prominence」
カラム:株式会社 島津ジーエルシー製
「Phenomenex Luna 5u C18(2) 100A」
検出器:DAD (Diode Array Detector)
データ処理:株式会社 島津製作所製「LCsolution」
測定条件:カラム温度40℃
移動相:メタノール/酢酸水溶液1vol%=6/4(vol比)
流速 :1.0ml/分
比表面積の測定には株式会社 島津製作所製トライスターII3020を使用した。得られたPPSの多孔質粒子(試料)をセルに入れた後、脱気した後ヘリウム置換、冷却し、窒素置換させることによって比表面積を測定した。
サンプル4mgを示差走査熱量測定装置(パーキンエルマー製「Diamond DSC」)を用いて、350℃/3分溶融させた後、350℃から240℃に急冷却(210℃/分)し、冷却した温度(240℃)で15分間保持した時の等温結晶化速度を測定した。得られた等温結晶化速度を「Tmax@240℃」と表示した。
得られたPPSの多孔質粒子を小型粉砕機で粉砕した後、日本工業規格Z8801の目開き0.5mmの試験用篩いを用いて篩った。篩いを通過したPPS樹脂100質量部に対し、3-グリシドキシプロピルトリメトキシシラン0.5質量部を配合し、均一に混合した後に溶融粘度V6(島津製作所製フローテスター、CFT-500Dを用い、300℃、荷重:1.96×106Pa、L/D=10(mm)/1(mm)にて、6分間保持した後に測定した値)を測定した。添加後の溶融粘度V6/添加前の溶融粘度V6の比から粘度上昇度を倍率として算出した。粘度上昇度が大きいほど反応性が高く、優れていることを示す。
実施例1~4ないし比較例1、2で得られた精製PPS65質量部、住友化学株式会社製オレフィン系熱可塑性エラストマー「ボンドファースト-E」5質量部をタンブラーで均一に混合した。その後、ベント付き2軸押出機(日本製鋼所、TEX30α)の投入口(トップフィーダ)に前記配合材料を投入し、サイドフィーダから、ガラス繊維(チョップドストランド、繊維径10μm、繊維長3mm、エポキシ樹脂集束剤)30質量部を投入して、樹脂成分吐出量30kg/hr、スクリュー回転数220rpm、設定樹脂温度を320℃に設定して溶融混練し、吐出口より吐出したストランド状物をカットしてPPSコンパウンドのペレットを得た。
続いて、上記のペレットをシリンダー温度310℃に設定した住友重機製射出成形機(SE75D-HP)に供給し、次の条件下で射出成形した。すなわち、40個分のキャビティーを有するワッシャー金型を用いて、一次スプルーに最も近い位置のキャビティー(C1)が完全に充填される限りで最低の成形条件とした。他の成形条件は75トン成形機、シリンダー温度320℃、金型温度140℃、保圧無しとした。
成型後の、キャビティー(C1)と同じランナーにある一次スプルーから最も遠いキャビティー(C10)の充填度を比較した。充填度(質量%)は、キャビティー(C1)の成形品に対する、キャビティー(C10)の成形品の質量比から求めた。キャビティー(C10)の充填度が高いほど、キャビティーバランスが優れていると言える。充填度に基づいて、各組成物のキャビティーバランスを以下の基準で判定した。
AA:100質量%以下から、90質量%以上の範囲
A:90質量%未満から、80質量%以上の範囲
B:80質量%未満から、70質量%以上の範囲
C:70質量%未満から、60質量%以上の範囲
D:60質量%未満以下の範囲
圧力計、温度計、コンデンサー、デカンター、精留塔を付けた撹拌翼付き150Lオートクレーブにp-ジクロロベンゼン(以下、DCBと略す)33.222kg(226mol)、NMP2.280kg(23mol)、47.23質量%水硫化ソーダ27.300kg(230mol)、及び49.21質量%苛性ソーダ18.533kg(228mol)を仕込み、撹拌しながら窒素雰囲気下で173℃まで5時間掛けて昇温して、水27.3kgを留出させた後、釜を密閉した。脱水時に共沸により留出したDCBはデカンターで分離して随時釜内に戻し、脱水終了後の釜内は無水硫化ナトリウム組成物がDCB中に分散した状態であった。更に、内温を160℃に冷却し、NMP47.492kg(479mol)を仕込み、185℃まで昇温した。圧力が0.00MPaに到達した時点で、精留塔を連結したバルブを開放し、内温200℃まで1時間掛けて昇温した。この際、精留塔出口温度が110℃以下になる様に冷却とバルブ開度で制御した。留出したDCBと水の混合蒸気はコンデンサーで凝縮し、デカンターで分離して、DCBは釜へ戻した。留出水量は179gであった。次に、内温200℃から230℃まで3時間かけて昇温し、1時間撹拌した後、250℃まで昇温し1時間撹拌して反応終了後、オートクレーブの内温を250℃から235℃に冷却し、到達後にオートクレープの底弁を開いて減圧状態のまま撹拌翼付き150リットル真空撹拌乾燥機(脱溶媒機ジャケット温度120度)にフラッシュさせてN-メチル-2-ピロリドンを抜き取り、室温まで冷却し、サンプリングした結果、N.V.55%の粗PPS混合物を得た。
合成例1で得た粗PPS混合物400gとメタノール水溶液(富士フイルム和光純薬株式会社製「試薬特級」)422gをフラスコに入れ、40℃で30分間撹拌混合し、そのスラリーを桐山ロートで減圧濾過し、上から押し固め、さらに上から80wt%メタノール水溶液(富士フイルム和光純薬株式会社製「試薬特級」80質量部に水20質量部を加えたもの)422gを数回に分けて注ぎろ過した。更に、そのろ過して作製したケーキをビーカーに移して薬さじで粉末状に砕き、そこに20℃の水を422g注ぎ、30分間攪拌混合した。そのスラリーを桐山ロートで減圧ろ過し、上から押し固め、更に上から20℃の水422gを数回に分けて注ぎろ過した。
上記ケーキをビーカーに移して、そこに634gの炭酸水を注ぎ、1時間攪拌混合した。そのスラリーを桐山ロートで減圧ろ過し、上から押し固め、更に上から炭酸水442gを数回に分けて注ぎろ過した。
そのろ過して作製したケーキをバットに移して薬さじで粉末状に砕き、120℃×4時間で乾燥し、精製PPSを得た。得られた精製PPSについて測定を行った。その結果を表1に示す。
合成例1で得た粗PPS混合物400gとメタノール水溶液(富士フイルム和光純薬株式会社製「試薬特級」)422gをフラスコに入れ、40℃で30分間撹拌混合し、そのスラリーを桐山ロートで減圧濾過し、上から押し固め、さらに上から50wt%メタノール水溶液(富士フイルム和光純薬株式会社製「試薬特級」50質量部に水50質量部を加えたもの)422gを数回に分けて注ぎろ過した。更に、そのろ過して作製したケーキをビーカーに移して薬さじで粉末状に砕き、そこに20℃の水を442g注ぎ、30分間攪拌混合した。そのスラリーを桐山ロートで減圧ろ過し、上から押し固め、更に上から20℃の水422gを数回に分けて注ぎろ過した。
上記ケーキをビーカーに移して、そこに634gの炭酸水を注ぎ、1時間攪拌混合した。そのスラリーを桐山ロートで減圧ろ過し、上から押し固め、更に上から炭酸水442gを数回に分けて注ぎろ過した。
そのろ過して作製したケーキをバットに移して薬さじで粉末状に砕き、120℃×4時間で乾燥し、精製PPSを得た。得られた精製PPSについて測定を行った。その結果を表1に示す。
合成例1で得た粗PPS混合物400gとメタノール水溶液(富士フイルム和光純薬株式会社製「試薬特級」)422gをフラスコに入れ、40℃で30分間撹拌混合し、そのスラリーを桐山ロートで減圧濾過し、上から押し固め、さらに上から30wt%メタノール水溶液(富士フイルム和光純薬株式会社製「試薬特級」30質量部に水70質量部を加えたもの)422gを数回に分けて注ぎろ過した。更に、そのろ過して作製したケーキをビーカーに移して薬さじで粉末状に砕き、そこに20℃の水を442g注ぎ、30分間攪拌混合した。そのスラリーを桐山ロートで減圧ろ過し、上から押し固め、更に上から20℃の水422gを数回に分けて注ぎろ過した。
上記ケーキをビーカーに移して、そこに643gの炭酸水を注ぎ、1時間攪拌混合した。そのスラリーを桐山ロートで減圧ろ過し、上から押し固め、更に上から炭酸水442gを数回に分けて注ぎろ過した。
そのろ過して作製したケーキをバットに移して薬さじで粉末状に砕き、120℃×4時間で乾燥し精製PPSを得た。得られた精製PPSについて測定を行った。その結果を表1に示す。
合成例1で得た粗PPS混合物400gとNMP422gをフラスコに入れ、40℃で30分間撹拌混合し、そのスラリーを桐山ロートで減圧濾過し、上から押し固め、さらに上からNMP422gを数回に分けて注ぎろ過した。更に、そのろ過して作製したケーキをビーカーに移して薬さじで粉末状に砕き、そこに70℃の水を442g注ぎ、30分間攪拌混合した。そのスラリーをそのスラリーを桐山ロートで減圧ろ過し、上から押し固め、更に上から70℃の水442gを数回に分けて注ぎろ過した。そのろ過して作製したケーキと炭酸水634gをオートクレーブに仕込み、160℃で1時間攪拌混合した。そのスラリーを桐山ロートで減圧ろ過し、上から押し固め、更に上から25℃の炭酸水422gを数回に分けて注ぎろ過した。そのろ過して作製したケーキをバットに移して薬さじで粉末状に砕き、120℃×4時間で乾燥し、精製PPSを得た。得られた精製PPSについて測定を行った。その結果を表1に示す。
合成例1で得た粗PPS混合物400gとNMP422gをフラスコに入れ、40℃で30分間撹拌混合し、そのスラリーを桐山ロートで減圧濾過し、上から押し固め、さらに上からNMP422gを数回に分けて注ぎろ過した。更に、そのろ過して作製したケーキをビーカーに移して薬さじで粉末状に砕き、そこに70℃の水を442g注ぎ、30分間攪拌混合した。そのスラリーをそのスラリーを桐山ロートで減圧ろ過し、上から押し固め、更に上から70℃の水442gを数回に分けて注ぎろ過した。そのろ過して作製したケーキと炭酸水634gをフラスコに入れ、25℃で1時間攪拌混合した。そのスラリーを桐山ロートで減圧ろ過し、上から押し固め、更に上から25℃の炭酸水422gを数回に分けて注ぎろ過した。そのろ過して作製したケーキをバットに移して薬さじで粉末状に砕き、120℃×4時間で乾燥し、精製PPSを得た。得られた精製PPSについて測定を行った。その結果を表1に示す。
Claims (11)
- 有機極性溶媒中、ポリハロ芳香族化合物とスルフィド化剤とを反応させて得られるポリアリーレンスルフィドを含有する粗反応生成物を脱溶媒させることにより、粗ポリアリーレンスルフィドを含む混合物を得る工程(1)と、粗ポリアリーレンスルフィドを含む混合物を精製して、前記粗ポリアリーレンスルフィドを比表面積30〔m2/g〕以上の範囲の多孔質粒子とする工程(2)と、得られた多孔質粒子と炭酸水とを接触させる工程(3)とを有し、
前記工程(2)が、炭素原子数1~3の酸素原子含有溶媒と接触させる工程(2Ss)と、水と接触させる工程(2Sw)とをそれぞれ少なくとも1回ずつ行う工程を有し、
工程(3)後の多孔質粒子中に含まれる下記構造式(1)で表される化合物(1)の割合が、1000〔ppm〕超から、3000〔ppm〕以下の範囲であることを特徴とするポリアリーレンスルフィドの精製方法。
- 前記工程(2)において、前記炭素原子数1~3の酸素原子含有溶媒が水溶液である、請求項1記載の精製方法。
- 前記水溶液中の炭素原子数1~3の酸素原子含有溶媒の濃度が水溶液100質量部に対して、90質量部以下の範囲である、請求項2記載の精製方法。
- 前記工程(3)において、ポリアリーレンスルフィドの多孔質粒子と炭酸水とを0.1MPaより小さい圧力下で接触させる、請求項1~3のいずれか一項記載の精製方法。
- 前記工程(3)において、ポリアリーレンスルフィドの多孔質粒子と炭酸水とを60℃以下の温度で接触させる、請求項1~4のいずれか一項記載の精製方法。
- 請求項1~5の何れか一項に記載の精製方法によりポリアリーレンスルフィドを精製する工程を有することを特徴とするポリアリーレンスルフィドの製造方法。
- 精製されたポリアリーレンスルフィドは、比表面積10〔m2/g〕以上の範囲の多孔質粒子である、請求項6記載のポリアリーレンスルフィドの製造方法。
- 精製されたポリアリーレンスルフィドは、等温結晶加速度が4分以上から、9分以下の範囲(ただし、示差走査熱量測定装置を用いて、350℃/3分溶融させた後、350℃から240℃に急冷却(210℃/分)し、冷却した温度(240℃)で15分間保持した際の測定値である)である請求項6記載のポリアリーレンスルフィドの製造方法。
- 等温結晶加速度が4分以上から、9分以下の範囲(ただし、示差走査熱量測定装置を用いて、350℃/3分溶融させた後、350℃から240℃に急冷却(210℃/分)し、冷却した温度(240℃)で15分間保持した際の測定値である)である請求項10記載のポリアリーレンスルフィド。
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WO2023218735A1 (ja) * | 2022-05-10 | 2023-11-16 | Dic株式会社 | ポリアリーレンスルフィドの精製方法及び製造方法 |
JP7419831B2 (ja) | 2020-01-20 | 2024-01-23 | 東ソー株式会社 | ポリアリーレンスルフィドの製造方法 |
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