WO2005078006A1 - ポリアリーレンスルフィド及びその製造方法 - Google Patents
ポリアリーレンスルフィド及びその製造方法 Download PDFInfo
- Publication number
- WO2005078006A1 WO2005078006A1 PCT/JP2005/002370 JP2005002370W WO2005078006A1 WO 2005078006 A1 WO2005078006 A1 WO 2005078006A1 JP 2005002370 W JP2005002370 W JP 2005002370W WO 2005078006 A1 WO2005078006 A1 WO 2005078006A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- washing
- water
- mol
- alkali metal
- polymer
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- 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
-
- 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
-
- 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
-
- 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
- C08G75/0209—Polyarylenethioethers derived from monomers containing one aromatic ring
- C08G75/0213—Polyarylenethioethers derived from monomers containing one aromatic ring containing elements other than carbon, hydrogen or sulfur
-
- 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
- C08G75/0254—Preparatory processes using metal sulfides
-
- 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 polyarylene sulfide and a method for producing the same. More specifically, the present invention relates to a polyarylene sulfide having excellent melt stability, a low crystallization temperature and excellent whiteness, and a method for producing the same.
- the polyarylene sulfide of the present invention is suitable for use in materials such as fibers. Background art
- PAS Polyarylsene sulfide
- PPS polyphenylene sulfide
- PAS polyphenylene sulfide
- PPS polyphenylene sulfide
- PAS can be formed into various molded products, films, sheets, fibers, etc. by general melt processing methods including extrusion molding, injection molding, and compression molding. Is widely used in
- a typical method for producing PAS is to react a sulfur source with a dihalo aromatic compound in an organic amide solvent such as N-methyl-1-pyrrolidone (hereinafter abbreviated as “NMP”). ing.
- NMP N-methyl-1-pyrrolidone
- an alkali metal sulfate is mainly used. It is also known to use an alkali metal sulfide obtained by reacting an alkali metal hydrosulfide and an alkali metal hydroxide in situ as a sulfur source.
- the polymerization reaction between the sulfur source and the dihalo aromatic compound is a desalination polycondensation reaction, and after the reaction, a large amount of a salt such as NaCl (ie, an alkali metal halide) is generated. Therefore, conventionally, PAS obtained by polymerization is washed with a washing liquid such as water, an organic solvent, a mixture of water and an organic solvent, or water containing a surfactant, and a salt such as NaCl is used. There has been proposed a method for removing such a problem (for example, Japanese Patent Publication No. Hei 6-86582, Japanese Patent Publication No. Hei 6-57747, Japanese Patent Laid-Open No. 4-1393925, Fairness four one five five four No. 45, and JP-A No. 10-265575).
- PAS is a crystalline polymer that generally has poor melt stability and a high crystallization rate from the molten state, so that yarn breakage is likely to occur during melt spinning, and the physical properties of the molded product after melt molding are poor. It has problems such as inconsistency. PAS also has a problem that it is easily colored under melt processing conditions.
- an alkali metal sulfide is reacted with a para- and meta-dihalo aromatic compound in an organic amide solvent.
- an acid or a hydrogen salt is added to the slurry containing PAS after the reaction to adjust the pH of the slurry to 7.0 to 11.0.
- a method for producing PAS has been proposed in which the slurry is filtered, and the obtained cake is heated in a non-oxidizing gas atmosphere to remove the solvent (for example, see Japanese Patent Application Laid-Open No. 201275 publication).
- an object of the present invention is a polyarylene sulfide obtained by polymerizing a sulfur source and a dihalo-aromatic compound in an organic amide solvent in the presence of an alkali metal hydroxide.
- An object of the present invention is to provide a polyarylene sulfide having a low activation temperature, high whiteness, and excellent melt stability, and a method for producing the same.
- the present inventors have conducted intensive studies to achieve the above object, and have found that PAS is produced by polymerizing a sulfur source and a dihaloaromatic compound in the presence of an alkali metal hydroxide in an organic amide solvent.
- the charged amounts of the respective components are adjusted so that 1.00 to 1.09 mol of an alkali metal hydroxide is present per 1 mol of the sulfur source, and secondly, after the polymerization,
- the washing step the polymer produced in the polymerization step is repeatedly washed twice or more with a washing liquid composed of water, a hydrophilic organic solvent or a mixture thereof.
- the crystallization temperature is low and whiteness is controlled by controlling the cleaning conditions so that the pH of the cleaning solution after cleaning is within the range of 8.0 to 1100. PAS with excellent melt stability and remarkably improved melt stability I found that.
- the polyarylene sulfide of the present invention has the following properties (e) and / or (f):
- a method for producing a polyarylene sulfide which comprises polymerizing a sulfur source and a dihalo aromatic compound in an organic amide solvent,
- the charging amount of each component is adjusted so that 1.00 to 1.09 moles of alkali metal hydroxide is present per mole of sulfur source,
- the polymer formed in the polymerization step is washed twice or more repeatedly with a washing solution composed of water, a hydrophilic organic solvent or a mixture thereof, with water or a mixed solution in the final washing step.
- the cleaning conditions are controlled so that the pH of the cleaning solution after the cleaning is within the range of 8.0 to 11.0, and
- a method for producing polyarylene sulfide is provided.
- the method for producing a polyarylene sulfide of the present invention comprises the following steps 1 to 5: (1) 0.95 to 1 mol / mol of an organic amide solvent, an alkali metal hydrosulfide, and an aluminum metal hydrosulfide. 1. Add a mixture containing 05 moles of alkali metal hydroxide. A dehydration step of heating and reacting, and discharging at least a part of a distillate containing water from inside the system containing the mixture to the outside of the system;
- the mixture remaining in the system contains 1.00 to 1.09 moles of alkali metal water per mole of a sulfur source containing alkali metal hydrosulfide (hereinafter referred to as “charged sulfur source”).
- a charging step 2 in which an alkali metal hydroxide and water are added as necessary so that the oxide and 0.5 to 2.0 moles of water are present;
- the dihalo-aromatic compound is added to the mixture, and the sulfur source and the dihalo-aromatic compound are polymerized at a temperature of 170 to 270 ° C in an organic amide solvent to obtain a dihalo-aromatic compound.
- Pre-polymerization step 3-1 to produce a pre-polymer with a product transfer rate of 50 to 98%, and after the pre-polymerization step, 2.0 to 10 moles of water per mole of sulfur source charged.
- the polymer produced in the polymerization step is washed twice or more with a washing solution composed of water, a hydrophilic organic solvent or a mixture thereof, and at that time, water or water is washed in the final washing step.
- an alkali metal hydrosulfide is generally used as a sulfur source.
- the alkali metal hydrogen sulfide include lithium hydrogen sulfide, sodium hydrogen sulfide, lithium hydrogen sulfide, hydrogen sulfide / revidium, cesium hydrosulfide, and a mixture of two or more of these.
- the alkali metal hydrosulfide any of an anhydride, a hydrate, and an aqueous solution may be used.
- sodium hydrogen sulfide and lithium hydrogen sulfide are preferable in that they can be obtained industrially at low cost.
- it can be used as an aqueous mixture such as an aqueous solution (that is, a mixture with fluid water) in view of processing operations and measurement. Preferred from the point.
- alkali metal hydrosulfide In the production process of alkali metal hydrosulfide, a small amount of alkali metal sulfide is generally produced as a by-product.
- the alkali metal hydrosulfide used in the present invention may contain a small amount of alkali metal sulfate. In this case, the total molar amount of the alkali metal hydrosulfide and the alkali metal sulfide becomes the charged sulfur source after the dehydration step.
- alkali metal hydroxide examples include lithium hydroxide, sodium hydroxide, potassium hydroxide, rubidium hydroxide, cesium hydroxide, and a mixture of two or more of these. Of these, sodium hydroxide and lithium hydroxide are preferred.
- the metal hydroxide is preferably used as an aqueous mixture such as an aqueous solution.
- the water to be dehydrated in the dehydration step includes hydration water, an aqueous medium of an aqueous solution, and a reaction between the alkali metal hydrosulfide and the alkali metal hydroxide. And water by-produced.
- the dihaloaromatic compound used in the present invention is a dihalogenated aromatic compound having two halogen atoms directly bonded to an aromatic ring.
- aromatic compound having a dihalide include, for example, o-dihachibenzene, m-dihalobenzene, ⁇ -dihachibenzene, dihalotonorene, dihalonaphthalene, methoxydihalobenzene, dihalobiphenyl, dihalobenzoic acid, dihalobenzoic acid, and dihalobenzoic acid.
- Examples include halodiphenyl ether, dihalodiphenyl snolephone, dihau diphenylenorelesolefoxide, dihau diphenyl-/ leketone, and the like.
- halogen atom refers to each atom of fluorine, chlorine, bromine, and iodine.
- two halogen atoms may be the same or different.
- These dihaloaromatic compounds can be used alone or in combination of two or more.
- the amount of the dihaloaromatic compound charged is usually 0.90 to 1.50 mol per mol of sulfur source (alkali metal sulfide and Z or alkali metal hydrosulfide) remaining in the system after the dehydration step.
- Mol preferably 0.95 to: L.20 mol, more preferably 1.0. 0 to 1.09 monole.
- a monohalo compound (not necessarily an aromatic compound) can be used in combination to form a terminal of a specific structure in the produced PAS or to regulate the polymerization reaction or molecular weight.
- a polyhalo compound to which three or more halogen atoms are bonded (not necessarily an aromatic conjugate), an active hydrogen-containing halogenated aromatic compound, It is also possible to use an aromatic compound in combination.
- the polyhalo conjugate as a branching / crosslinking agent, preferably, trihalobenzene is used.
- an organic amide solvent which is a non-protonic polar organic solvent is used as a solvent for the dehydration reaction and the polymerization reaction.
- the organic amide solvent is preferably stable at a high temperature with respect to alkali.
- organic amide solvent examples include amide compounds such as N, N-dimethylformamide and N, N-dimethylacetamide; ⁇ -alkyl-prolatatam compounds such as N-methyl- ⁇ -proprotamata; ⁇ -alkylpyrrolidone compounds such as pyrrolidone, ⁇ -cyclohexyl-2-pyrrolidone or ⁇ -cyclohexanolylpyrrolidone compounds; 1,3-diakynoley 2-imidazolidinone, etc.
- amide compounds such as N, N-dimethylformamide and N, N-dimethylacetamide
- ⁇ -alkyl-prolatatam compounds such as N-methyl- ⁇ -proprotamata
- ⁇ -alkylpyrrolidone compounds such as pyrrolidone, ⁇ -cyclohexyl-2-pyrrolidone or ⁇ -cyclohexanolylpyrrolidone compounds
- ⁇ -dialkylimidazoli Dinon compounds tetraalkyl urea compounds such as tetramethyl urea
- hexaalkyl phosphate triamide compounds such as hexamethyl phosphate triamide.
- organic amide solvents may be used alone or in combination of two or more.
- organic amide solvents ⁇ -alkylpyrrolidone compounds, ⁇ -cycloalkylpyrrolidone compounds, ⁇ ⁇ ⁇ ⁇ -alkylprolactam compounds, and ⁇ , ⁇ -dialkylimidazolidinone compounds are preferred.
- —Methyl-2-pyrrolidone, ⁇ -methyl- ⁇ -caprolactam, and 1,3-dialkyl-12-imidazolidinone are preferably used.
- Organic amide used in the polymerization reaction of the present invention The amount of solvent used is usually in the range of 0.1 to 10 kg per mole of sulfur source.
- various polymerization auxiliaries can be used as needed in order to accelerate the polymerization reaction and to obtain PAS having a high degree of polymerization in a short time.
- the polymerization aid include metal sulfonic acid salts, lithium halides, metal organic carboxylate salts, and alkali metal phosphate salts which are generally known as polymerization aids for PAS.
- organic carboxylic acid metal salts are particularly preferable because they are inexpensive.
- the amount of the polymerization aid used varies depending on the type of the compound used, but is generally in the range of 0.01 to 10 mol per 1 mol of the charged sulfur source.
- a dehydration step is arranged to adjust the amount of water in the reaction system.
- the dehydration step is preferably carried out by heating a mixture containing an organic amide solvent, an alkali metal hydrosulfide and an alkali metal hydroxide under an inert gas atmosphere, and discharging water out of the system by distillation.
- a mixture containing 0.95 to 1.05 mol of alkali metal hydroxide per 1 mol of organic amide solvent, alkali metal hydrosulfide, and alkali metal hydrosulfide is heated to react at least a part of the alkali metal hydrosulfide with the alkali metal hydroxide to convert it to the alkali metal sulfide, and to remove the distillate containing water from the system containing the mixture. It is preferable to discharge at least a part out of the system.
- the molar ratio of alkali metal hydroxide to aluminum hydroxide in this step is too small, the amount of sulfur component (hydrogen sulfide) volatilized in the dehydration step will increase. A decrease in the amount of the sulfur source causes a decrease in productivity, and an abnormal reaction due to an increase in the polysulfide component in the charged sulfur source remaining after dehydration and a decrease in the quality of the produced PAS are likely to occur. If the molar ratio of alkali metal hydroxide per mole of alkali metal hydroxide charged is too large, the quality of the organic amide solvent will increase and it will be difficult to carry out the polymerization reaction stably. Or decrease the quality of the produced PAS Sometimes.
- the preferred molar ratio of alkali metal hydroxide per mole of alkali metal hydrosulfide charged in this step is 0.96 to 1.04.
- Alkali metal hydrosulfides often contain small amounts of alkali metal sulfides, and the amount of sulfur source is the sum of the alkali metal hydrosulfide and the aluminum metal sulfide .
- Alkali metal hydrosulfide does not pose a problem as a raw material for PAS even if it contains alkali metal sulfide. Even if a small amount of alkali metal sulfate is mixed, the molar ratio with the alkali metal hydroxide is calculated based on the content (analytical value) of the alkali metal hydrosulfide, and the molar ratio is calculated. Can be adjusted.
- the water consisting of water of hydration (water of crystallization), aqueous medium, and by-product water is dehydrated until it falls within the required range.
- the dehydration is preferably performed until the amount of coexisting water in the polymerization reaction system becomes 0.5 to 2.0 mol with respect to 1 mol of the sulfur source. If the water content becomes too low in the dewatering step, water may be added before the polymerization step to adjust the water content to a desired value.
- these raw materials are charged into the reaction tank within a temperature range from room temperature to 300 ° C., preferably from room temperature to 200 ° C.
- the order of charging the raw materials may be in any order, and additional raw materials may be added during the dehydration operation.
- An organic amide solvent is used as a solvent used in the dehydration step. This solvent is preferably the same as the organic amide solvent used in the polymerization step, and N-methyl-1-pyrrolidone is particularly preferred.
- the amount of the organic amide solvent used is usually about 0.1 to 10 kg per mole of the sulfur source charged into the reaction vessel.
- the mixture after charging the raw materials into the reaction tank is usually kept at a temperature of 300 ° C. or less, preferably 100 to 250 ° C., usually for 15 minutes to 24 hours.
- the heating is performed for a time, preferably 30 minutes to 10 hours.
- the heating method includes a method of maintaining a constant temperature, a method of stepwise or continuous heating, or a method of combining both.
- the dehydration step is performed by a batch system, a continuous system, or a combination of both systems.
- the apparatus for performing the dehydration step may be the same as or different from the reactor (reactor) used in the subsequent polymerization step.
- the material of the device is preferably a corrosion-resistant material such as titanium.
- a part of the organic amide solvent is usually It is discharged out of the reaction tank along with it. At that time, hydrogen sulfide is discharged out of the system as a gas.
- the alkali metal hydroxide and the organic amide solvent react by heat treatment to produce an alkyl metal alkylaminoalkyl carboxylate, and the alkali metal hydroxide becomes an alkali metal hydroxide. It is presumed that it forms a complex with the metal alkylaminoalkylcarboxylate and exists in the system.
- a part of the alkali metal hydroxide reacts with water to generate hydrogen sulfide and an alkali metal hydroxide, and the generated hydrogen sulfide is discharged out of the system. Emissions of hydrogen sulfide outside the system are directly linked to the reduction of sulfur sources in the system.
- the mixture remaining in the system after the dehydration step contains 1.0 to 1.0 per mole of a sulfur source (alkali sulfur source) containing an alkali metal hydrosulfide and an alkali metal sulfide. It is preferred to add the alkali metal hydroxide and water as needed so that 9 moles of alkali metal hydroxide and 0.5-2.0 moles of water are present.
- the amount of charged sulfur source is sometimes referred to as the “effective S” amount.
- the molar ratio of the alkali metal hydroxide per mole of sulfur source is from 1.0 to 1.09, preferably from 1.01 to 1.08, and more preferably from 1.015 to 1.0. 0 75, particularly preferred is 1.02 to 1.06. It is preferable to carry out the polymerization reaction in a state where the alkali metal hydroxide is in a small excess, in order to stably carry out the polymerization reaction and obtain high-quality PAS. 8. Polymerization process
- the polymerization step is performed by charging a dihaloaromatic compound to the mixture after the completion of the dehydration step and heating the sulfur source and the dihaloaromatic compound in an organic amide solvent.
- a polymerization tank different from the reaction tank used in the dehydration step is used, the mixture after the dehydration step and the dihaloaromatic compound are charged into the polymerization tank.
- the amount of the organic amide solvent and the amount of coexisting water may be adjusted as necessary.
- a polymerization aid or other additives may be mixed.
- Mixing of the mixture obtained after the dehydration step with the dihaloaromatic compound is usually performed in a temperature range of 100 to 350 ° C, preferably 120 to 330 ° C.
- the order of charging is not particularly limited, and usually, both components are partially charged little by little or at a time.
- the polymerization reaction is generally preferably performed in a two-step process at a temperature in the range of 170 to 290 ° C.
- a heating method a method of maintaining a constant temperature, a method of stepwise or continuous heating, or a combination of both methods is used.
- the polymerization reaction time is generally in the range of 10 minutes to 72 hours, preferably in the range of 30 minutes to 48 hours.
- the amount of the organic amide solvent used in the polymerization step is usually 0.1 to 10 kg, preferably 0.15 to 1 kg, per 1 mol of the charged sulfur source present in the polymerization step. Within this range, the amount may be changed during the polymerization reaction.
- the amount of coexisting water at the start of the polymerization reaction is preferably in the range of 0.5 to 2.0 mol per 1 mol of the charged sulfur source. It is preferable to increase the amount of coexisting water during the polymerization reaction.
- A a reaction mixture containing an organic amide solvent, a sulfur source, a dihaloaromatic compound, and a predetermined molar ratio of an alkali metal hydroxide, in an amount of 0.5 to 2.0 mol per mol of the charged sulfur source.
- the polymerization reaction was carried out by heating to 170 to The first step of forming a prepolymer at a conversion of aromatic compounds of 50 to 98%; and (B) the reaction system such that 2.0 to 10 mol of water is present per 1 mol of charged sulfur source.
- a second-stage polymerization step of adjusting the amount of water in the mixture and heating the mixture to 245 to 290 ° C. to continue the polymerization reaction;
- the polymerization reaction is carried out by at least two stages of polymerization steps including In the pre-polymerization step, it is desirable to form a prepolymer having a melt viscosity of 0.5 to 30 Pa ⁇ s measured at a temperature of 310 ° C. and a shear rate of 12 16 sec 1 .
- Water may be added at the end of or at the end of the polymerization reaction to increase the water content in order to reduce the content of by-product salt and impurities in the produced polymer, and to recover the polymer in particulate form.
- the polymerization reaction system may be a batch system, a continuous system, or a combination of both systems. In batch polymerization, to shorten the polymerization cycle time,
- a system using two or more reaction vessels may be used. 9. Post-treatment process
- a post-treatment step after the polymerization step there is generally a step of separating PAS from a reaction mixture (slurry) containing PAS generated by the polymerization reaction, washing and drying. After drying, the product PAS is recovered.
- the PAS can be recovered by drying the cooled slurry as it is or by diluting it with water or the like, repeating filtration and washing and drying. it can.
- the granular polymer can be separated from the slurry by a method of sieving using a screen. It is preferable because it can be easily separated from the base.
- the polymer may be sieved in a high temperature state.
- PAS after such a separation treatment has an organic amide solvent, an alkali metal halide, an oligomer, a decomposition product, and the like attached thereto. Therefore, in order to obtain PAS having excellent physical properties, it is necessary to sufficiently wash and purify the generated PAS.
- the polymer produced in the polymerization step is Wash twice or more with a washing solution consisting of an organic solvent or a mixture of these solvents.
- the number of washings is preferably at least three times, more preferably at least four times, particularly preferably at least five times.
- the upper limit of the number of washings is often about 10 to 15 times.
- the hydrophilic organic solvent may be an aprotic organic solvent or a protic organic solvent.
- Aprotic organic solvents include ketone solvents such as acetone; nitrile solvents such as acetonidol; amide solvents such as N-methyl-2-pyrrolidone and N, N-dimethylformamide.
- Protic organic solvents include alcoholic solvents such as methyl alcohol, ethynoleanol, propynoleanol, and ethylene glycol. These hydrophilic organic solvents can be used alone or in combination of two or more.
- acetone is preferable because of its excellent effect of removing impurities (low molecular weight components) such as oligomers and decomposition products. Acetone is preferred from the viewpoint of economy and safety.
- the hydrophilic organic solvent has an excellent effect of removing low molecular weight organic impurities such as oligomers and decomposition products.
- a mixed solution of water and a hydrophilic organic solvent has an excellent effect of removing by-product alkali metal halides such as NaC1 in addition to low molecular weight organic impurities.
- Water is excellent in removing alkali metal halides, organic amide solvents, and hydrophilic organic solvents used for washing.
- the washing step it is preferable to carry out both washing with a hydrophilic organic solvent or a mixed solution (a mixed solution of water and a hydrophilic organic solvent) and washing with water.
- a hydrophilic organic solvent or a mixed solution a mixed solution of water and a hydrophilic organic solvent
- the mixing ratio of water and the hydrophilic organic solvent in the mixed liquid is arbitrary, and can be appropriately selected from arbitrary mixing ratios, for example, within a weight ratio of 1:99 to 99: 1.
- the mixed solution preferably has a water content of 1 to 60% by weight, more preferably 1-3 0% by weight, particularly preferred properly is preferable for enhancing the removal efficiency of the organic impurities, such as 1-2 0 weight 0/0 mixture that forces oligomers and decomposition products using the.
- Washing with a washing solution is generally performed by mixing PAS and the washing solution and stirring the mixture.
- the amount of the washing solution used in each washing cycle is usually 1 to 15 times the volume of the polymer, preferably 2 to 0 times the volume of L, more preferably 3 to 8 times the volume.
- the washing time is generally 1 to 120 minutes, preferably 3 to 100 minutes, more preferably 5 to 60 minutes.
- washing liquid is separated using a screen or a centrifuge. Doing filtered using a screen, liquid content is usually 3 0-7 0 weight 0/0, often 4 0-6 0 weight. /. A small amount of wet cake is obtained. Using a centrifugal separator, it is possible to use a low liquid content.
- the next washing cycle is performed.
- Cleaning is generally performed at room temperature (15-30 ° C), but can be performed at lower or higher temperatures as long as the cleaning liquid is in a liquid state.
- the produced PAS can be treated with an acid (acid washing) or treated with a salt such as ammonium chloride.
- PAS is mixed with water or a mixed solution (ie, a mixed solution of water and a hydrophilic organic solvent) in the final washing step by such repeated washing (that is, the final washing). Washing is performed using a flat washing solution, and washing conditions are controlled so that the pH of the washing solution after washing falls within the range of 8.0 to 11.0.
- this final washing step it is preferable to use water or a mixed solution having a high water content (for example, a mixed solution having a water content of 60 to 99% by weight), and more preferably water. No.
- the final washing step means the final washing in the repeated washing, and after the washing in the washing cycle, the PAS is dried and recovered as a product.
- the pH of the washing solution after washing refers to the pH measured for the washing solution after mixing PAS and the washing solution, stirring and washing.
- PAS obtained by polymerizing a sulfur source and a dihalo-aromatic compound in an organic amide solvent in the presence of an alkali metal hydroxide is an alkaline conjugate such as a residual alkali metal hydroxide. Since the substance is eluted in the washing solution, the pH of the washing solution after washing may show a strong force even if water is used as the washing solution.
- the final washing step as a method for controlling the washing conditions so that the pH of the washing solution after washing is in the range of 8.0 to: L1.0, for example, (i) adding an acid or a basic compound
- a method using a washing solution (ii) a method for adjusting the number of washings, (iii) a method for adjusting the amount of the washing solution relative to the polymer, and (iv) a method combining these methods.
- the pH of the washing solution after washing in the final washing step is usually 8.0 to 11.0, preferably 8.5 to 10.7.
- the content of low molecular weight components extracted by Soxhlet extraction using a black hole form is preferably 5.0% by weight or less, more preferably 4.0% by weight or less, and particularly preferably 3.0% by weight or less. It is desirable to repeat the washing until the weight becomes less than or equal to% by weight. Insufficient cleaning may increase the content of low molecular weight components, deteriorating the physical properties of PAS and limiting its use.
- PAS is separated from the washing solution by filtration using a screen.
- the wet PAS (wet cake) separated from the washing solution is dried by heating under normal pressure or reduced pressure to remove the washing solution. Thus, the dried PAS is recovered.
- the PAS of the present invention is an arylene sulfite represented by the structural formula [—Ar—S—]. It is an aromatic polymer having a repeating unit as a main component.
- Ar is an arylene group. Repeating units [- Ar- S-] and one mole (basal mole)
- the repeating units generally 50 mol% or more, preferably rather 70 mole 0/0 or more, more preferably is a polymer containing 90 mole 0/0 above.
- arylene group (Ar) a p-phenylene group, an m-phenylene group and the like are preferable.
- a PAS having the following properties can be obtained when measured by the measurement method (described in the Examples) defined in the present specification.
- the PAS of the present invention has a melt viscosity of 1 to 3000 Pa ⁇ s, preferably 3 to 2000 Pa ⁇ s, more preferably 10 to 1500 Pa ⁇ s measured at a temperature of 310 ° C. and a shear rate of 1216 sec ⁇ 1. Particularly preferred is 15 to: L 200 Pa's.
- the melt viscosity of PAS can be used as an index of molecular weight. If the melt viscosity of PAS is too low, the mechanical properties will be insufficient, and if it is too high, the melt fluidity will decrease and the moldability will decrease.
- the PAS of the present invention has a pH (resin pH) of 7.0 to 12.0, preferably 7.0 to: L 1.5, measured in a mixed solvent of water Zaceton (2: 1 by volume). More preferably, it is 7.5 to 11.5.
- whiteness, crystallization temperature, and melt stability can be adjusted to preferable ranges by controlling production conditions including washing conditions so that the resin pH falls within this range.
- the PAS of the present invention has a crystallization temperature (also referred to as “melt crystallization temperature”) of 220 ° C. or lower, which is measured in a process of decreasing the temperature at a rate of 10 ° C.Z from a molten state at a temperature of 340 ° C., preferably It is below 210 ° C.
- the crystallization temperature can often be below 205 ° C, and even below 200 ° C.
- the lower limit of the crystallization temperature is preferably about 165 ° C. Since the PAS of the present invention has a low crystallization temperature, the crystallization speed from the molten state is low. By slowing the crystallization speed of PAS, melt moldability such as extrudability can be improved.
- the PAS of the present invention has a melt molded product having a whiteness of 70 or more.
- the upper limit of whiteness is usually around 85 or 80. If the whiteness of PAS is high, it is possible to obtain molded products with excellent color tone, and tones the PAS molded product to any color It becomes easier. If the whiteness of PAS is too low, the color tone of the molded product becomes brown or color unevenness occurs. Further, if the whiteness of the PAS is too low, it becomes difficult to obtain a desired color even if a colorant is used.
- PAS of the present invention after holding for 5 minutes at a temperature 310 ° C, for melt viscosity value MVi measured at a shear rate of 1216 sec one 1, was held for 30 minutes at 310 ° C, at a pruning cross rate 1216 sec-1 the ratio mvz / MVi of the measured melt viscosity value MV 2 is the preferred properly 0.80 or more, more preferably 0.85 or more. In many cases, this ratio MVsZMVi can be greater than 0.90, and even greater than 0.95. The upper limit of this ratio MVs / MV is preferably 1.0.
- the PAS of the present invention has a low molecular weight component content of preferably 5.0% by weight or less, more preferably 4.0% by weight or less, and particularly preferably 3.% by weight or less, extracted by Soxhlet extraction using black form. 0% by weight or less.
- the content of the low molecular weight component contained in PAS is preferably as small as possible, but the lower limit is usually about 1.0% by weight or about 1.5% by weight. If the content of the low molecular weight component is too large, the melt stability of the PAS will decrease, and the physical properties of the molded product will decrease.
- the PAS of the present invention is excellent in melt stability, low in crystallization temperature, and excellent in whiteness, so that it is suitable for use in materials such as fibers.
- the PAS of the present invention can be formed into various molded products by extrusion molding, injection molding, compression molding and the like. As PAS, PPS is particularly preferred. The invention's effect
- the PAS of the present invention has a low crystallization rate from the molten state, Since it has excellent melt moldability and excellent melt stability, for example, yarn breakage during melt spinning does not easily occur, and the physical properties of molded articles after melt molding hardly change. Furthermore, since the PAS of the present invention has little thermal discoloration during melt processing, a molded article having high whiteness can be obtained.
- the polymer yield is calculated based on the polymer weight (theoretical amount) assuming that all of the available sulfur components present in the reactor after the dehydration step have been converted into polymers.
- the ratio (% by weight) of the recovered polymer weight was calculated.
- the melt viscosity was measured by Capillograph 1-C manufactured by Toyo Seiki. At this time, the drill used a flat die of 1 ⁇ X 1 OmmL, and the set temperature was 310 ° C. Introducing the polymer sample to the device, after holding for 5 minutes, the melt viscosity was measured at a shear rate of 1216 sec one 1.
- the melt viscosity of the polymer was measured according to the melt viscosity measurement method described above, The ratio was calculated. That is, after holding for 5 minutes a polymer sample at a temperature 3 10 ° C, the melt viscosity was measured (MV X) at a shear rate of 1216 sec-1. For the same polymer sample, after holding for 30 minutes at 310 ° C, the melt viscosity was measured (MV 2) at a shear speed 1216 sec one 1. The ratio (MVs / MV ⁇ ) was then calculated based on these measurements. This ratio, also called the retention of melt viscosity, indicates that the higher the ratio, the higher the melt stability of the polymer.
- the polymer was heated and melted by a hot press at 320 ° CZ for 10 minutes, and then solidified by a room temperature press to produce a sheet.
- the obtained sheet was aged at 150 ° C for 30 minutes to produce a crystallized sheet.
- the color tone was measured by a standard light C and reflected light measurement method using a “color difference meter CR-200” manufactured by MINOLTA. Prior to measurement, calibration was performed using a standard white plate. Each sample was measured at three points and the average was calculated. The color was expressed in whiteness (WH).
- the polymer was heated and melted by a hot press at 320 ° C for 10 minutes, and then rapidly cooled to produce an amorphous sheet.
- Approximately 10 mg of the amorphous sheet was taken as a measurement sample, and the crystallization temperature (Tmc) under a temperature-lowering condition was measured using a “differential scanning calorimeter DSC7” manufactured by Perkin-Elmer. More specifically, the temperature of the sample is raised to 340 ° C in a nitrogen gas atmosphere (20 m1Z), held at that temperature for 1 minute, and then lowered at a rate of 10 ° C / min. The crystallization temperature was measured at.
- pDCB p-dichlorobenzene
- the reaction mixture cooled to around room temperature was sampled by sampling 214.3 g and sieved using a 100-mesh screen to obtain a wet state (water content 60%).
- a wet state water content 60%.
- 1528 g of acetone and 80 g of ion-exchanged water were added to the wet granular polymer, and the mixture was washed with stirring for 30 minutes.
- the amount of the washing solution is 5 times the theoretical polymer recovery amount, and the water content of the washing solution is 5% by weight.
- washing was performed with the washing solution at room temperature.
- the stirring power was set to the floating limit or higher.
- the polymer content after washing was sieved by filtration using a 100-mesh screen.
- the liquid content of the wet cake after filtration was 40 to 60% by weight.
- Example 2 The thus obtained washed polymer was dried at 105 ° C for 13 hours by a dryer. The yield of the granular polymer thus obtained was 92%, and the melt viscosity thereof was 160 Pa ⁇ s. Table 1 shows data on color tone, melt stability, crystallization temperature, and content of low molecular weight components.
- Example 2
- Example 3 After the completion of the reaction, the polymer was washed in the same manner as in Example 1 to obtain a purified polymer. After the final deionized water washing was completed, a pH meter was put into the washing solution before filtration, and the pH after 5 minutes was measured. The yield of the granular polymer thus obtained was 93%, and the melt viscosity was 141 Pa ⁇ s. Table 1 shows data on color tone, melt stability, crystallization temperature, and content of low molecular weight components.
- Example 3 shows data on color tone, melt stability, crystallization temperature, and content of low molecular weight components.
- the dehydration step to the polymerization step were performed in exactly the same manner as in Example 1.
- the post-treatment step was performed by the following method.
- Example 5 After the completion of the reaction, the polymer was washed in the same manner as in Example 1 to obtain a purified polymer. After the final ion-exchanged water washing was completed, a pH meter was added to the washing solution before filtration, and the pH after 5 minutes was measured. The yield of the granular polymer thus obtained was 92%, and the melt viscosity was 230 Pa ⁇ s. Table 1 shows data on color tone, melt stability, crystallization temperature, and content of low molecular weight components.
- Example 5 Example 5
- Example 6 After the completion of the reaction, the polymer was washed in the same manner as in Example 1 to obtain a purified polymer. After the final washing with ion-exchanged water was completed, a pH meter was added to the washing solution before filtration, and the pH after 5 minutes was measured. The yield of the granular polymer thus obtained was 85%, and the melt viscosity was 450 Pa ⁇ s. Table 1 shows data on color tone, melt stability, crystallization temperature, and content of low molecular weight components.
- Example 6 Example 6
- the dehydration step to the polymerization step were performed in exactly the same manner as in Example 2.
- the post-processing step was performed by the following method.
- Example 1 After completion of the reaction, the polymer was washed in the same manner as in Example 1 except that the number of times of washing with ion-exchanged water was changed to 8, to obtain a purified polymer. After the last ion-exchange water washing is completed, put a pH meter into the washing solution before filtration and adjust the pH after 5 minutes. It was 8.9 when measured. The yield of the granular polymer thus obtained was 92%, and the melt viscosity thereof was 123 Pa ⁇ s. Table 1 shows data on color tone, melt stability, crystallization temperature, and content of low molecular weight components. Comparative Example 1
- the dehydration step to the polymerization step were performed in exactly the same manner as in Example 1.
- the post-processing step was performed by the following method.
- Example 1 The polymer was washed in the same manner as in Example 1 except that approximately 3 g of NaOH (purity 9.7%) was added to the washing solution during the final washing with ion-exchanged water. Got. After the final ion-exchanged water washing was completed, a pH meter was added to the washing solution before filtration, and the pH after 5 minutes was measured. The result was 12.5. The yield of the granular polymer thus obtained was 92%, and its melt viscosity was 155 Pa ⁇ S. Table 1 shows data on color tone, melt stability, crystallization temperature, and content of low molecular weight components. Comparative Example 2
- the dehydration step to the polymerization step were performed in exactly the same manner as in Example 1.
- the post-processing step was performed by the following method.
- acetic acid water prepared by adding 1.88 g of acetic acid to 470 g of ion-exchanged water, and further washed with 470 g of ion-exchanged water. Washing was performed four times for 20 minutes to obtain a washed polymer. After the final washing with ion-exchanged water was completed, a pH meter was put into the washing solution before filtration, and the pH after 5 minutes was measured.
- washing was performed with the washing solution at room temperature.
- the stirring power was set to the floating limit or higher.
- the polymer content after washing was sieved by filtration using a 100-mesh screen.
- the liquid content of the wet cake after filtration was 40 to 60% by weight.
- Example 2 After the completion of the reaction, the polymer was washed in the same manner as in Example 1 to obtain a purified polymer. After the final deionized water washing was completed, a ⁇ meter was put into the washing solution before filtration, and ⁇ after 5 minutes was measured. The yield of the granular polymer thus obtained was 85%, and the melt viscosity was 171 Pa ⁇ s. Table 1 shows data on color tone, melt stability, crystallization temperature, and content of low molecular weight components. Comparative Example 4
- Example 1 After the completion of the reaction, the polymer was washed in the same manner as in Example 1 to obtain a purified polymer. After the final washing with ion-exchanged water was completed, a pH meter was added to the washing solution before filtration, and the pH after 5 minutes was measured. The yield of the granular polymer thus obtained was 80%, and the melt viscosity was 470 Pa ⁇ s. Table 1 shows data on color tone, melt stability, crystallization temperature, and content of low molecular weight components. table 1
- the PAS of the present invention (Examples 1 to 5) had a resin pH in the range of 7.0 to 12.0, a high whiteness, and excellent melt stability, It can be seen that the crystallization temperature is low.
- the polyarylene sulfide of the present invention can be used as it is or after being oxidatively crosslinked, alone or, if desired, by blending various inorganic fillers, fibrous fillers, and various synthetic resins to obtain various injection molded articles or the like. It can be formed into extruded products such as sheets, films, fibers and pipes. Since the polyarylene sulfide of the present invention has a low crystallization rate and excellent melt stability, it is particularly suitable for producing extruded products such as fibers.
Landscapes
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Polymers With Sulfur, Phosphorus Or Metals In The Main Chain (AREA)
- Processes Of Treating Macromolecular Substances (AREA)
Abstract
Description
Claims
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
KR1020067018512A KR101118399B1 (ko) | 2004-02-12 | 2005-02-09 | 폴리아릴렌 술피드 및 그의 제조 방법 |
DE602005027178T DE602005027178D1 (de) | 2004-02-12 | 2005-02-09 | Polyarylensulfid und herstellungsverfahren dafür |
EP05710270A EP1714994B1 (en) | 2004-02-12 | 2005-02-09 | Polyarylene sulfide and process for producing the same |
US10/589,006 US7655748B2 (en) | 2004-02-12 | 2005-02-09 | Poly(arylene sulfide) and production process thereof |
AT05710270T ATE503790T1 (de) | 2004-02-12 | 2005-02-09 | Polyarylensulfid und herstellungsverfahren dafür |
US12/653,623 US8076447B2 (en) | 2004-02-12 | 2009-12-16 | Poly (arylene sulfide) and production process thereof |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2004-034397 | 2004-02-12 | ||
JP2004034397A JP4782383B2 (ja) | 2004-02-12 | 2004-02-12 | ポリアリーレンスルフィド及びその製造方法 |
Related Child Applications (2)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US10/589,006 A-371-Of-International US7655748B2 (en) | 2004-02-12 | 2005-02-09 | Poly(arylene sulfide) and production process thereof |
US12/653,623 Division US8076447B2 (en) | 2004-02-12 | 2009-12-16 | Poly (arylene sulfide) and production process thereof |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2005078006A1 true WO2005078006A1 (ja) | 2005-08-25 |
Family
ID=34857656
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2005/002370 WO2005078006A1 (ja) | 2004-02-12 | 2005-02-09 | ポリアリーレンスルフィド及びその製造方法 |
Country Status (9)
Country | Link |
---|---|
US (2) | US7655748B2 (ja) |
EP (1) | EP1714994B1 (ja) |
JP (1) | JP4782383B2 (ja) |
KR (1) | KR101118399B1 (ja) |
CN (1) | CN100547013C (ja) |
AT (1) | ATE503790T1 (ja) |
DE (1) | DE602005027178D1 (ja) |
TW (1) | TW200530295A (ja) |
WO (1) | WO2005078006A1 (ja) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2011142557A3 (ko) * | 2010-05-12 | 2012-04-19 | 에스케이케미칼주식회사 | 가공성이 우수한 폴리아릴렌 설파이드 및 이의 제조 방법 |
Families Citing this family (24)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2005298669A (ja) * | 2004-04-12 | 2005-10-27 | Polyplastics Co | ポリアリーレンサルファイド樹脂組成物及びその成形品 |
US7312300B2 (en) * | 2005-02-22 | 2007-12-25 | Chevron Phillips Chemical Company Lp | Inferred water analysis in polyphenylene sulfide production |
JP4813196B2 (ja) * | 2006-02-02 | 2011-11-09 | ポリプラスチックス株式会社 | 円筒形状部位保有成形品用ポリアリーレンサルファイド樹脂組成物及び円筒形状部位保有成形品 |
US8263734B2 (en) * | 2009-02-13 | 2012-09-11 | Chevron Phillips Chemical Company Lp | System and method for reducing off-gassing of polyphenylene sulfide |
CN102822239B (zh) * | 2010-03-31 | 2015-05-13 | 株式会社吴羽 | 支化状聚亚芳基硫醚树脂及其制造方法 |
WO2011145428A1 (ja) | 2010-05-19 | 2011-11-24 | 株式会社クレハ | ポリアリーレンスルフィドの製造方法、及びポリアリーレンスルフィド |
WO2012070335A1 (ja) * | 2010-11-26 | 2012-05-31 | 株式会社クレハ | ポリアリーレンスルフィドの製造方法、及びポリアリーレンスルフィド |
JP2012187727A (ja) * | 2011-03-08 | 2012-10-04 | Polyplastics Co | 射出成形品の製造方法 |
WO2015047719A1 (en) | 2013-09-25 | 2015-04-02 | Ticona Llc | Method of polyarylene sulfide crystallization |
WO2015047721A1 (en) | 2013-09-25 | 2015-04-02 | Ticona Llc | Scrubbing process for polyarylene sulfide formation |
JP6684206B2 (ja) | 2013-09-25 | 2020-04-22 | ティコナ・エルエルシー | ポリアリーレンスルフィドの形成中における塩副生成物の分離 |
US9562139B2 (en) | 2013-09-25 | 2017-02-07 | Ticona Llc | Process for forming low halogen content polyarylene sulfides |
US9587074B2 (en) | 2013-09-25 | 2017-03-07 | Ticona Llc | Multi-stage process for forming polyarylene sulfides |
JP6517789B2 (ja) | 2013-09-25 | 2019-05-22 | ティコナ・エルエルシー | 複数の化合物からポリマーを分離するための方法及びシステム |
US9771465B2 (en) | 2013-12-25 | 2017-09-26 | Toray Industries, Inc. | Polyarylene sulfide resin composition and molded article comprising same |
JP6803844B2 (ja) | 2015-02-19 | 2020-12-23 | ティコナ・エルエルシー | 低粘度のポリアリーレンスルフィドを形成する方法 |
WO2016133740A1 (en) | 2015-02-19 | 2016-08-25 | Ticona Llc | Method of polyarylene sulfide precipitation |
WO2016133739A1 (en) | 2015-02-19 | 2016-08-25 | Ticona Llc | Method for forming a high molecular weight polyarylene sulfide |
WO2016153610A1 (en) | 2015-03-25 | 2016-09-29 | Ticona Llc | Technique for forming a high melt viscosity polyarylene sulfide |
WO2017022524A1 (ja) * | 2015-07-31 | 2017-02-09 | 東レ株式会社 | ポリフェニレンスルフィド樹脂組成物およびその製造方法 |
KR101928254B1 (ko) | 2015-09-30 | 2018-12-11 | 가부시끼가이샤 구레하 | 폴리아릴렌 설파이드의 제조 방법 |
KR101968882B1 (ko) | 2015-09-30 | 2019-04-12 | 가부시끼가이샤 구레하 | 폴리아릴렌 설파이드의 제조 방법 |
US11407861B2 (en) | 2019-06-28 | 2022-08-09 | Ticona Llc | Method for forming a polyarylene sulfide |
WO2021126543A1 (en) * | 2019-12-20 | 2021-06-24 | Ticona Llc | Method for forming a polyarylene sulfide |
Citations (24)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH02160834A (ja) | 1988-12-14 | 1990-06-20 | Toray Philips Petorooriamu Kk | ポリアリーレンスルフィドの製造方法 |
JPH02302436A (ja) | 1989-05-18 | 1990-12-14 | Dainippon Ink & Chem Inc | ポリアリーレンスルフィドの製造方法 |
JPH0455445A (ja) | 1990-06-25 | 1992-02-24 | Nippon Supeshiyaritei Prod Kk | 抗菌性成形品 |
JPH04139215A (ja) | 1990-09-28 | 1992-05-13 | Idemitsu Petrochem Co Ltd | ポリアリーレンスルフィドの洗浄方法 |
EP0547718A2 (en) | 1991-12-17 | 1993-06-23 | Tonen Chemical Corporation | Process for the preparation of polyarylene sulfide and an apparatus for the preparation thereof |
US5235034A (en) | 1989-11-06 | 1993-08-10 | Phillips Petroleum Company | Treatment of polyarylene sulfide/sulfone polymers with zinc compound and acidic solution |
JPH05271414A (ja) | 1992-03-25 | 1993-10-19 | Dainippon Ink & Chem Inc | 高分子量ポリアリーレンスルフィドの製造方法 |
JPH0651792A (ja) | 1992-07-31 | 1994-02-25 | Sanyo Electric Co Ltd | 音声認識装置 |
JPH0651793A (ja) | 1992-08-04 | 1994-02-25 | Sharp Corp | 音声認識装置 |
JPH0657747A (ja) | 1992-08-10 | 1994-03-01 | Futaba Kogyo Kk | パイル打設機 |
JPH0686528A (ja) | 1992-07-16 | 1994-03-25 | Teac Corp | クローポールpm形ステッピングモータ |
JPH07286042A (ja) | 1994-04-20 | 1995-10-31 | Idemitsu Petrochem Co Ltd | ポリアリーレンスルフィドの製造方法 |
JPH08183858A (ja) | 1994-12-28 | 1996-07-16 | Kureha Chem Ind Co Ltd | ポリフェニレンスルフィドの製造方法 |
JPH08198965A (ja) | 1995-01-26 | 1996-08-06 | Dainippon Ink & Chem Inc | ポリアリーレンスルフィドの製造法 |
JPH1045912A (ja) | 1996-07-31 | 1998-02-17 | Dainippon Ink & Chem Inc | ポリアリーレンスルフィドの精製方法 |
JPH1045911A (ja) | 1996-07-31 | 1998-02-17 | Dainippon Ink & Chem Inc | ポリアリーレンスルフィドの精製方法 |
JPH10130388A (ja) | 1996-10-31 | 1998-05-19 | Tonen Chem Corp | ポリアリーレンスルフィドの製造法 |
JPH10265575A (ja) | 1997-03-25 | 1998-10-06 | Idemitsu Petrochem Co Ltd | ポリアリーレンスルフィドの精製方法 |
JPH11209617A (ja) | 1998-01-27 | 1999-08-03 | Kureha Chem Ind Co Ltd | ポリアリーレンスルフィド樹脂成形品の製造方法 |
JP2001040090A (ja) | 1999-05-21 | 2001-02-13 | Dainippon Ink & Chem Inc | ポリアリーレンスルフィド、その製造方法、及びポリアリーレンスルフィド組成物 |
JP2001181394A (ja) | 1999-12-24 | 2001-07-03 | Dainippon Ink & Chem Inc | ポリアリーレンスルフィドの製造方法 |
EP1219665A2 (en) | 2000-12-19 | 2002-07-03 | Kwangju Institute of Science and Technology | Poly (arylene ether sulfide) and poly (arylene ether sulfone) for optical device and method for preparing the same |
JP2002201275A (ja) | 2000-12-28 | 2002-07-19 | Dic Ep Inc | ポリアリーレンスルフィドの製造法 |
JP2004244619A (ja) | 2003-01-21 | 2004-09-02 | Kureha Chem Ind Co Ltd | ポリアリーレンスルフィド及びその製造方法 |
Family Cites Families (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS61228023A (ja) | 1985-04-01 | 1986-10-11 | Kureha Chem Ind Co Ltd | ポリアリ−レンスルフィドの精製法 |
JPS61255933A (ja) * | 1985-05-08 | 1986-11-13 | Kureha Chem Ind Co Ltd | 重合体スラリ−の処理法 |
JPH0686528B2 (ja) | 1986-02-12 | 1994-11-02 | 大日本インキ化学工業株式会社 | ポリフエニレンスルフイドからのナトリウム塩の除去方法 |
JPH0657747B2 (ja) | 1986-03-24 | 1994-08-03 | 大日本インキ化学工業株式会社 | ポリフエニレンスルフイドの精製方法 |
US4786711A (en) | 1987-01-23 | 1988-11-22 | Phillips Petroleum Company | P-phenylene sulfide polymer preparation with dehydrated mixture of alkali metal hydroxide and excess alkali metal bisulfide |
US4767841A (en) | 1987-02-24 | 1988-08-30 | Phillips Petroleum Company | Arylene sulfide polymer preparation from dehydrated admixture comprising sulfur source, cyclic amide solvent and water |
US6600009B2 (en) | 1996-10-31 | 2003-07-29 | Dainippon Ink And Chemicals, Incorporated | Process for the preparation of polyarylene sulfide |
-
2004
- 2004-02-12 JP JP2004034397A patent/JP4782383B2/ja not_active Expired - Fee Related
-
2005
- 2005-02-03 TW TW094103427A patent/TW200530295A/zh unknown
- 2005-02-09 EP EP05710270A patent/EP1714994B1/en not_active Not-in-force
- 2005-02-09 US US10/589,006 patent/US7655748B2/en not_active Expired - Fee Related
- 2005-02-09 DE DE602005027178T patent/DE602005027178D1/de active Active
- 2005-02-09 CN CNB2005800046786A patent/CN100547013C/zh not_active Expired - Fee Related
- 2005-02-09 KR KR1020067018512A patent/KR101118399B1/ko active IP Right Grant
- 2005-02-09 AT AT05710270T patent/ATE503790T1/de not_active IP Right Cessation
- 2005-02-09 WO PCT/JP2005/002370 patent/WO2005078006A1/ja active Application Filing
-
2009
- 2009-12-16 US US12/653,623 patent/US8076447B2/en not_active Expired - Fee Related
Patent Citations (24)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH02160834A (ja) | 1988-12-14 | 1990-06-20 | Toray Philips Petorooriamu Kk | ポリアリーレンスルフィドの製造方法 |
JPH02302436A (ja) | 1989-05-18 | 1990-12-14 | Dainippon Ink & Chem Inc | ポリアリーレンスルフィドの製造方法 |
US5235034A (en) | 1989-11-06 | 1993-08-10 | Phillips Petroleum Company | Treatment of polyarylene sulfide/sulfone polymers with zinc compound and acidic solution |
JPH0455445A (ja) | 1990-06-25 | 1992-02-24 | Nippon Supeshiyaritei Prod Kk | 抗菌性成形品 |
JPH04139215A (ja) | 1990-09-28 | 1992-05-13 | Idemitsu Petrochem Co Ltd | ポリアリーレンスルフィドの洗浄方法 |
EP0547718A2 (en) | 1991-12-17 | 1993-06-23 | Tonen Chemical Corporation | Process for the preparation of polyarylene sulfide and an apparatus for the preparation thereof |
JPH05271414A (ja) | 1992-03-25 | 1993-10-19 | Dainippon Ink & Chem Inc | 高分子量ポリアリーレンスルフィドの製造方法 |
JPH0686528A (ja) | 1992-07-16 | 1994-03-25 | Teac Corp | クローポールpm形ステッピングモータ |
JPH0651792A (ja) | 1992-07-31 | 1994-02-25 | Sanyo Electric Co Ltd | 音声認識装置 |
JPH0651793A (ja) | 1992-08-04 | 1994-02-25 | Sharp Corp | 音声認識装置 |
JPH0657747A (ja) | 1992-08-10 | 1994-03-01 | Futaba Kogyo Kk | パイル打設機 |
JPH07286042A (ja) | 1994-04-20 | 1995-10-31 | Idemitsu Petrochem Co Ltd | ポリアリーレンスルフィドの製造方法 |
JPH08183858A (ja) | 1994-12-28 | 1996-07-16 | Kureha Chem Ind Co Ltd | ポリフェニレンスルフィドの製造方法 |
JPH08198965A (ja) | 1995-01-26 | 1996-08-06 | Dainippon Ink & Chem Inc | ポリアリーレンスルフィドの製造法 |
JPH1045912A (ja) | 1996-07-31 | 1998-02-17 | Dainippon Ink & Chem Inc | ポリアリーレンスルフィドの精製方法 |
JPH1045911A (ja) | 1996-07-31 | 1998-02-17 | Dainippon Ink & Chem Inc | ポリアリーレンスルフィドの精製方法 |
JPH10130388A (ja) | 1996-10-31 | 1998-05-19 | Tonen Chem Corp | ポリアリーレンスルフィドの製造法 |
JPH10265575A (ja) | 1997-03-25 | 1998-10-06 | Idemitsu Petrochem Co Ltd | ポリアリーレンスルフィドの精製方法 |
JPH11209617A (ja) | 1998-01-27 | 1999-08-03 | Kureha Chem Ind Co Ltd | ポリアリーレンスルフィド樹脂成形品の製造方法 |
JP2001040090A (ja) | 1999-05-21 | 2001-02-13 | Dainippon Ink & Chem Inc | ポリアリーレンスルフィド、その製造方法、及びポリアリーレンスルフィド組成物 |
JP2001181394A (ja) | 1999-12-24 | 2001-07-03 | Dainippon Ink & Chem Inc | ポリアリーレンスルフィドの製造方法 |
EP1219665A2 (en) | 2000-12-19 | 2002-07-03 | Kwangju Institute of Science and Technology | Poly (arylene ether sulfide) and poly (arylene ether sulfone) for optical device and method for preparing the same |
JP2002201275A (ja) | 2000-12-28 | 2002-07-19 | Dic Ep Inc | ポリアリーレンスルフィドの製造法 |
JP2004244619A (ja) | 2003-01-21 | 2004-09-02 | Kureha Chem Ind Co Ltd | ポリアリーレンスルフィド及びその製造方法 |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2011142557A3 (ko) * | 2010-05-12 | 2012-04-19 | 에스케이케미칼주식회사 | 가공성이 우수한 폴리아릴렌 설파이드 및 이의 제조 방법 |
US9546248B2 (en) | 2010-05-12 | 2017-01-17 | Sk Chemicals Co., Ltd. | Polyarylene sulfide having excellent processability and preparation method thereof |
Also Published As
Publication number | Publication date |
---|---|
JP2005225931A (ja) | 2005-08-25 |
JP4782383B2 (ja) | 2011-09-28 |
KR20070020221A (ko) | 2007-02-20 |
EP1714994A4 (en) | 2007-02-21 |
EP1714994A1 (en) | 2006-10-25 |
EP1714994B1 (en) | 2011-03-30 |
CN1918214A (zh) | 2007-02-21 |
CN100547013C (zh) | 2009-10-07 |
US20100113739A1 (en) | 2010-05-06 |
TW200530295A (en) | 2005-09-16 |
ATE503790T1 (de) | 2011-04-15 |
US20070093642A1 (en) | 2007-04-26 |
US7655748B2 (en) | 2010-02-02 |
KR101118399B1 (ko) | 2012-03-09 |
DE602005027178D1 (de) | 2011-05-12 |
US8076447B2 (en) | 2011-12-13 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
WO2005078006A1 (ja) | ポリアリーレンスルフィド及びその製造方法 | |
JP5221877B2 (ja) | ポリアリーレンスルフィドの製造方法 | |
JP4777610B2 (ja) | ポリアリーレンスルフィド及びその製造方法 | |
JP5623277B2 (ja) | 粒状ポリアリーレンスルフィドの製造方法 | |
JP5731196B2 (ja) | 末端ハロゲン基含量が低減されたポリアリーレンスルフィドの製造方法 | |
US10072123B2 (en) | Polyarylene sulfide production method and polyarylene sulfide | |
JP3989785B2 (ja) | ポリアリーレンスルフィドの製造方法 | |
JP6517337B2 (ja) | 粒状ポリアリーレンスルフィドを製造する方法、及び粒状ポリアリーレンスルフィド | |
JP4310279B2 (ja) | ポリアリーレンスルフィドの製造方法及び洗浄方法、並びに洗浄に使用した有機溶媒の精製方法 | |
WO2004065457A1 (ja) | ポリアリーレンスルフィド及びその製造方法 | |
JP2000191785A (ja) | ポリアリーレンスルフィドの製造方法 | |
KR20170103875A (ko) | 미분 폴리아릴렌 설파이드를 제조하는 방법 및 미분 폴리아릴렌 설파이드 | |
US11427683B2 (en) | Preparation method of polyarylene sulfide | |
JP7191344B2 (ja) | ポリアリーレンスルフィドの製造方法 | |
US11192981B2 (en) | Preparation method of polyarylene sulfide | |
JP6889271B2 (ja) | ポリアリーレンスルフィドの製造方法 | |
JPH07228698A (ja) | ポリアリーレンスルフィドの製造方法 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AK | Designated states |
Kind code of ref document: A1 Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BW BY BZ CA CH CN CO CR CU CZ DE DK DM DZ EC EE EG ES FI GB GD GE GH GM HR HU ID IL IN IS KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NA NI NO NZ OM PG PH PL PT RO RU SC SD SE SG SK SL SY TJ TM TN TR TT TZ UA UG US UZ VC VN YU ZA ZM ZW |
|
AL | Designated countries for regional patents |
Kind code of ref document: A1 Designated state(s): GM KE LS MW MZ NA SD SL SZ TZ UG ZM ZW AM AZ BY KG KZ MD RU TJ TM AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LT LU MC NL PL PT RO SE SI SK TR BF BJ CF CG CI CM GA GN GQ GW ML MR NE SN TD TG |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application | ||
WWE | Wipo information: entry into national phase |
Ref document number: 2007093642 Country of ref document: US Ref document number: 10589006 Country of ref document: US |
|
WWE | Wipo information: entry into national phase |
Ref document number: 200580004678.6 Country of ref document: CN |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
WWW | Wipo information: withdrawn in national office |
Country of ref document: DE |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2005710270 Country of ref document: EP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 1020067018512 Country of ref document: KR |
|
WWP | Wipo information: published in national office |
Ref document number: 2005710270 Country of ref document: EP |
|
WWP | Wipo information: published in national office |
Ref document number: 1020067018512 Country of ref document: KR |
|
WWP | Wipo information: published in national office |
Ref document number: 10589006 Country of ref document: US |