WO2004060973A1 - 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 - Google Patents
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 Download PDFInfo
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- WO2004060973A1 WO2004060973A1 PCT/JP2003/016333 JP0316333W WO2004060973A1 WO 2004060973 A1 WO2004060973 A1 WO 2004060973A1 JP 0316333 W JP0316333 W JP 0316333W WO 2004060973 A1 WO2004060973 A1 WO 2004060973A1
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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
- C08G75/04—Polythioethers from mercapto compounds or metallic derivatives thereof
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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
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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
- C08G75/0209—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
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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
- C08G75/0254—Preparatory processes using metal sulfides
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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
- C08G75/14—Polysulfides
Definitions
- the present invention relates to a method for producing a polyarylene sulfide, and more particularly, to a method for recovering an organic solvent after washing a polyarylene sulfide obtained in a polymerization step in an organic amide solvent with an organic solvent.
- the present invention relates to a method for producing polyarylene sulfide, which includes a step of recycling an organic solvent purified by reducing the content of an alkaline compound such as methylamine contained in the organic solvent in a washing step.
- the present invention relates to a method for cleaning polyarylene sulfide obtained in a polymerization step. Further, the present invention relates to a method for purifying an organic solvent used for washing polyarylene sulfide.
- PAS Polyphenylene sulfide
- PPS polyphenylene sulfide
- PPS polyphenylene sulfide
- PAS has heat resistance, chemical resistance, flame retardancy, mechanical strength, It is an engineering plastic with excellent electrical properties and dimensional stability.
- PAS can be molded into various molded products, films, sheets, fibers, etc. by general melting methods such as extrusion molding, injection molding, and compression molding. It is widely used in the field.
- a method for producing PAS As a typical method for producing PAS, a method is known in which an alkali metal sulfide as a sulfur source is reacted with a haloaromatic compound in an organic amide solvent such as N-methyl-2-pyrrolidone. A combination of alkali metal hydrosulfide and alkali metal hydroxide is also used as a sulfur source.
- the post-treatment step involves washing the produced PAS with an organic solvent such as a ketone (eg, acetone) or an alcohol (eg, methanol), which is the same organic solvent as the polymerization solvent.
- an organic solvent such as a ketone (eg, acetone) or an alcohol (eg, methanol), which is the same organic solvent as the polymerization solvent.
- washing solvents acetone and methanol are widely used because of their low boiling point, easy recovery by distillation, and excellent washing power. ing.
- cleaning solvents are repeatedly used (recycled) in the cleaning process in the manufacture of PASS.
- a washing solvent is used repeatedly, after the washing step, the washing solvent is recovered by distilling a liquid component such as a filtrate containing many impurities and an organic amide solvent in addition to the washing solvent.
- washing solvent such as acetone
- the purification of the washing solvent by distillation and recovery alone will adversely affect the quality of the PAS produced. It was found that it was not possible to sufficiently remove trace amounts of impurities, which had an adverse effect on the properties of PAS after washing. Specifically, it was found that when the washing solvent was repeatedly collected and reused in the washing step, the washed PAS was colored or, in severe cases, the melt viscosity of the PAS was reduced. As a result, the washing solvent cannot be used any more repeatedly.
- Tm c also called “melt crystallization temperature”
- an aqueous solution of an acid or a salt of a weak alkali and a strong acid for example, ammonium chloride
- the washing solvent is repeatedly distilled and collected and recycled in the washing step, the effect of the acid or salt treatment is reduced and the crystallization temperature is hardly increased.
- the efficiency of the molding operation decreases, such as a longer injection molding cycle.
- N-methyl-2-pyrrolidone was recovered and purified from a PAS slurry obtained by reacting an alkali metal sulfide with a dihalo aromatic compound in an N-methyl-2-pyrrolidone solvent.
- a method has been proposed in which a small amount of an alkali metal hydroxide and / or an alkali metal carbonate is added to a liquid containing -methyl-2-pyrrolidone as a main component, followed by distillation (see, for example, Japanese Patent Application Laid-Open No. HEI 9-260572). 1 1—3 4 9 5 6 6).
- a method for recovering and purifying N-methyl-2-pyrrolidone from a PAS slurry obtained by reacting an alkali metal sulfide with a dihalo aromatic compound in an N-methyl-2-pyrrolidone solvent is described below.
- a method has been proposed in which a small amount of ammonia or an amine is added to a liquid containing -methyl-1-pyrrolidone as a main component, followed by distillation (for example, Japanese Patent Application Laid-Open No. 11-354,679). ).
- Such a method for recovering and purifying an organic amide solvent to which an alkaline compound is added is not suitable as a method for recovering and purifying a washing solvent such as acetone or methanol.
- a washing solvent such as acetone or methanol.
- An object of the present invention is to wash the polyarylene sulfide obtained in the polymerization step in an organic amide solvent with an organic solvent, recover the organic solvent, and adversely affect the quality of PAS produced in the recovered organic solvent. It is an object of the present invention to provide a method for producing polyarylene sulfide, which includes a step of recycling an organic solvent purified by reducing the content of impurities to be applied in a washing step.
- Another object of the present invention is to provide a new method for cleaning polyarylene sulfide in which an organic solvent used for cleaning is recycled in a cleaning step.
- the present inventors have conducted intensive studies to achieve the above object, and have found that In a PAS production method in which a dino-aromatic compound and a sulfur source such as metal sulfide are heated and polymerized in a medium, it is presumed that decomposition of the organic amide solvent is caused by the decomposition of organic amide solvent. We paid attention to the by-product of the compound. It has been found that, when mixed with a washing solvent, this alkaline compound is difficult to remove even by distillation, and accumulates in the washing solvent during repeated use and recovery of the washing solvent.
- an inorganic acid such as hydrochloric acid was added to the washing solvent recovered from the washing step to convert an alkaline compound such as methylamine into an inorganic acid salt. It has been found that distillation from, can effectively reduce the content of alkaline compounds that have a great adverse effect on the physical properties of PAS.
- treating the washing solvent recovered from the washing step with activated carbon can also significantly reduce the amount of alkaline compounds such as methylamine.
- At least one sulfur source selected from the group consisting of aluminum metal sulfide and aluminum metal sulfide and a dihachid aromatic compound are required.
- a polyarylene sulfide comprising a step of washing a polyarylene sulfide obtained in a polymerization step in an organic amide solvent (A) with an organic solvent (B).
- the organic solvent is washed with an organic solvent (B) in which the content of an alkaline compound has been reduced to 300 ppm or less on a weight basis, and the yellow index (YI) is 15.0 or less.
- a method for producing polyarylene sulfide which comprises obtaining polyarylene sulfide.
- the polycrystal having a crystallization temperature (Tmc) of 200 ° C. or more and a yellow index (YI) of 11.0 or less is used.
- Tmc crystallization temperature
- YI yellow index
- the organic solvent (B) used in the washing step is used. Collected and recycled for use in the washing process.At this time, the organic solvent (B) whose alkaline compound content in the collected organic solvent (B) has been reduced to 300 ppm or less by weight is washed.
- a method for cleaning polyarylene sulfide, which is characterized by being recycled in the process, is provided.
- the organic solvent (B) is recovered, and the recovered organic solvent is recovered.
- a method for purifying an organic solvent used for washing which comprises adding an inorganic acid to a solvent (B) and then distilling the solvent.
- the sulfur source at least one sulfur source selected from the group consisting of alkaline metal hydrosulfide and alkaline metal sulfide is used.
- alkali metal sulfide examples include lithium sulfide, sodium sulfide, potassium sulfide, rubidium sulfide, cesium sulfide, and a mixture of two or more of these.
- These alkali metal sulfides are usually marketed and used as hydrates.
- the hydrate for example, sodium sulfide nonahydrate (N a 2 S ⁇ 9 H 2 0), include sulfurized sodium pentahydrate (N a 2 S ⁇ 5 H 2 O) and the like.
- the alkali metal sulfate may be used as an aqueous mixture.
- alkali metal hydrosulfide is combined with alkali metal hydroxide as a sulfur source.
- the alkali metal bisulfide include lithium bisulfide, sodium bisulfide, potassium bisulfide, rubidium bisulfide, cesium bisulfide, 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. Among them, sodium hydrosulfide and lithium hydrosulfide are preferable in that they are industrially available at low cost.
- the alkali metal hydrosulfide is preferably used as an aqueous mixture such as an aqueous solution (that is, a mixture with fluid water) from the viewpoints of processing operation, measurement, and the like.
- 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 sulfide. In this case, the total molar amount of the alkali metal hydrosulfide and the alkali metal sulfide becomes the sulfur source charged 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 because they can be obtained industrially at low cost.
- the alkali metal hydroxide is preferably used as an aqueous mixture such as an aqueous solution.
- the water to be dehydrated in the dehydration step includes secondary water such as hydration water, an aqueous medium of an aqueous solution, and a reaction between alkali metal hydroxide and aluminum hydroxide.
- secondary water such as hydration water, an aqueous medium of an aqueous solution, and a reaction between alkali metal hydroxide and aluminum hydroxide.
- the dihalo aromatic compound used in the present invention is a dihalogenated aromatic compound having two halogen atoms directly bonded to an aromatic ring.
- aromatic compounds having dihachio include, for example, o-dihalobenzene, m_dihalobenzene, p-dihalobenzene, dihalotoluene, dihalonaphthalene, methoxydihalobenzene, dihalobiphenyl, dihalobenzoic acid, dihalodiphenyl ether And dihalodiphenenoresnorephon, dihalodiphenenoresnorephoxide, dihalodipheni / leketon, and the like.
- halogen atom refers to each atom of fluorine, chlorine, bromine, and iodine
- two halogen atoms may be the same or different.
- dihaloaromatic compounds can be used alone or in combination of two or more.
- the amount of the dihaloaromatic compound charged is usually from 0.90 to 1.5 mol per mol of the sulfur source (alkali metal sulfide and / or alkali metal hydrosulfide) remaining in the system after the dehydration step. , Preferably 0.95 to 1.20 mol, more preferably 1.00 to: 1.09.
- a monohalo compound (not necessarily an aromatic compound) can be used in combination to form a terminal having a specific structure in the produced PAS or to adjust the polymerization reaction or the molecular weight.
- Polyhalo compounds (not necessarily aromatic compounds) with three or more halogen atoms bonded to form a branched or crosslinked polymer, halogenated aromatic compounds containing active hydrogen, halogenated aromatic nitro compounds It is also possible to use objects and the like in combination.
- the polyhalo compound as the branching / crosslinking agent, trihalobenzene is preferable.
- an organic amide solvent that is an aprotic 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 to an alkali.
- organic amide solvent examples include amide compounds such as N, N-dimethylformamide and N, N-dimethylacetamide; ⁇ -alkyl-prolatatam compounds such as N-methyl- ⁇ -caprolactam ⁇ ⁇ ⁇ ⁇ -alkylpyrrolidone compounds such as ⁇ -methyl_2-pyrrolidone and ⁇ -cyclohexyl_2-pyrrolidone or ⁇ -cycloalkylpyrrolidone compounds; ⁇ such as 1,3-dialkyl-12-imidazolidinone , ⁇ -dialkylimidazolidinone compounds; tetraalkylurea compounds such as tetramethylurea; and hexaalkylphosphate triamide compounds such as hexamethylphosphoric triamide.
- These organic amide solvents may be used alone or in combination of two or more.
- ⁇ -alkylpyrrolidone compounds Preference is given to chloroalkylpyrrolidone compounds, N-alkylproprolatatam compounds and N, N-dialkylimidazolidinone compounds, in particular N-methyl-2-pyrrolidone, N-methyl- ⁇ -caprolactam, and 1,3- Dialkyl 1-2 imidazolidinones are preferably used.
- the amount of the organic amide solvent used in the polymerization reaction of the present invention is usually in the range of 0.1 to 0 kg / mol 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 salts of organic sulfonic acids, lithium halides, metal salts of organic carboxylic acids, and alkali metal salts of phosphoric acid, which are generally known as polymerization aids for PAS.
- organic carboxylate 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 as a step before the polymerization step in order to adjust the amount of water in the reaction system.
- the alkali metal sulfide and / or Z or alkali metal hydrosulfide are desirably heated in an organic amide solvent in an inert gas atmosphere, optionally in the presence of an alkali metal hydroxide.
- the reaction is carried out, and water is discharged out of the system by distillation.
- Alkali metal sulfides usually contain more water than is required for the polymerization reaction because they are used as hydrates or aqueous mixtures.
- an alkali metal hydrosulfide is used as a sulfur source, an equimolar amount of an alkali metal hydroxide is added and the reaction is performed in situ in an organic amide solvent.
- 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.
- dehydration is carried out until the amount of water coexisting in the polymerization reaction system is usually about 0.3 to 5 mol, preferably about 0.5 to 2 mol, per 1 mol of the sulfur source. If the amount of water becomes too low in the dehydration step, water may be added before the polymerization step to adjust to a desired amount of water.
- the introduction of these raw materials into the reaction tank is generally carried out 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 furthermore, each raw material 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 process, and N-methyl_2-pyrrolidone is particularly preferred.
- the amount of the organic amide solvent used is usually about 0.1 to about LO kg per mole of the sulfur source charged into the reactor.
- the mixture after charging the raw materials into the reaction tank is usually kept at a temperature of 300 ° C. or less, preferably in a temperature range of 100 ° C. to 250 ° C., usually for 15 minutes to 2 minutes.
- the heating is performed for 4 hours, preferably for 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 patch 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 discharged out of the reaction tank along with water. At that time, hydrogen sulfide is discharged out of the system as a gas.
- the polymerization step is performed by charging a dihalo aromatic compound to the mixture after the completion of the dehydration step, and heating the sulfur source and the dihalo aromatic 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 completion of the dehydration step with the dihaloaromatic compound is usually performed within a temperature range of 100 to 350 ° C, preferably 120 to 330 ° C.
- the charging order is not particularly limited, and both components are partially This is done by adding small amounts or at a time.
- the polymerization reaction is generally performed at 100 to 350 ° C, preferably 120 to 330 ° C. C, more preferably at 170-290 ° C.
- a heating method for the reaction 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 generally ranges from 10 minutes to 72 hours, preferably from 3.0 minutes to 48 hours.
- the amount of the organic amide solvent used in this step is usually 0.1 to 10 kg, preferably 0.15 to 1 kg, per 1 mol of the sulfur source charged during 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 usually preferably in the range of 0.3 to 5 mol per mol of the charged sulfur source.
- the coexisting water content may be outside this range.
- the coexisting water content can be in the range of 0.1 to 15 moles, preferably 0.5 to 10 moles, per mole of sulfur source such as alkali metal sulfide.
- the amount of coexisting water may be increased during the polymerization reaction, or may be reduced by distillation.
- the reaction is carried out at a temperature of 170 to 270 ° C, preferably 180 to 235 ° C, and the conversion of the dihaloaromatic compound is 50 to 98 mol. / 0, and then water is added so that more than 2.0 moles and not more than 10 moles, preferably 2.5 to 7.0 moles of water per mole of the charged sulfur source are present, There is a method of raising the temperature to 245 to 290 ° C. and continuing the reaction.
- the charged sulfur source means the amount of the sulfur source remaining in the reaction tank after the dehydration step when the dehydration step is provided.
- Particularly preferred polymerization methods include:
- a reaction mixture containing an organic amide solvent, a sulfur source (A) and a dihaloaromatic compound (B) is mixed with 0.5 to 2.0 moles of water per mole of the charged sulfur source (A).
- the polymerization reaction was carried out by heating to 170 to 270 ° C, and the conversion of the dihalo aromatic compound was 5 Step 1 for producing a prepolymer at 0-98%, and
- step 1 it is desirable to produce 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 1,216 sec ⁇ 1 .
- step 2 the polymerization reaction is continued until the melt viscosity of the prepolymer formed in step 1 increases.
- Water may be added at the end of the polymerization reaction or at the end of the polymerization reaction to increase the water content in order to reduce the content of by-product salt or impurities in the produced polymer or to recover the polymer in the form of particles.
- Many other known polymerization methods or modifications thereof can be applied to the polymerization step of the present invention, and it is not particularly limited to a specific polymerization method.
- the polymerization reaction system may be a patch system, a continuous system, or a combination of both systems.
- a method using two or more reaction tanks may be used for the purpose of shortening the polymerization cycle time.
- post-treatment after the polymerization reaction can be performed by a conventional method.
- the cooled product slurry can be collected as it is or by diluting with water or the like, followed by filtration, washing and filtration, and drying.
- the product slurry may be sieved from the polymer while still at an elevated temperature.
- the PAS is washed with the same organic amide solvent as the polymerization solvent ⁇ an organic solvent such as ketones (eg, acetone) and alcohols (eg, methanol). Further, the PAS may be washed with high-temperature water or the like. The resulting PAS can be treated with an acid or a salt such as ammonium chloride.
- an organic solvent such as ketones (eg, acetone) and alcohols (eg, methanol).
- the PAS may be washed with high-temperature water or the like.
- the resulting PAS can be treated with an acid or a salt such as ammonium chloride.
- the polymer is separated from the reaction solution containing the produced polymer.
- a washing step of washing the separated polymer with an organic solvent (B) is provided.
- the collected organic solvent (B) is purified to remove the contaminated alkaline compound.
- a purification step to reduce the content is arranged.
- the purified organic solvent (B) can be recycled in the PAS washing step. That is, the organic solvent (B) used in the PAS washing step can be purified and reused in another PAS washing step, and the number of reuses can be increased.
- the polymer is generally washed by contacting the polymer with an organic solvent (B). More specifically, the wet cake of the polymer separated in the separation step and the organic solvent (B) are mixed and stirred.
- the amount of the organic solvent (B) used for washing is usually about 1 to 10 times, preferably about 2 to 8 times the weight of the polymer.
- the polymer is separated from the liquid component (C) containing the organic solvent (B) used for washing.
- the purified PAS is generally recovered as a granular polymer and can be sieved using a screen. Therefore, also in the separation step, the polymer can be separated by sieving the reaction solution containing the generated polymer using a screen.
- the solid-liquid mixed component containing the organic amide solvent (A) that has passed through the screen is separated into a solid component and a liquid component (D1), and the separated solid component is added with the organic solvent (B) to form the organic amide.
- Separation into a liquid component (D2) containing the solvent (A) and the organic solvent (B) and a solid component is preferable for efficient recovery of the organic amide solvent (A). Since the solid component is fine particles such as by-product salts, it is desirable to use a centrifuge or a decanter to separate the liquid component (D1 and D2) from the solid component.
- the organic solvent (B) is generally recovered by distillation from the liquid component (C) or a mixture of the liquid component (C) and the liquid component (D1, Z or D2). Distillation can usually be simple distillation. However, the organic solvent (B) recovered by simple simple distillation contains an alkaline compound such as methinoleamine, and if washing and recovery are repeated, the alkaline compound (B) becomes an organic solvent (B). ) Accumulates inside.
- the content of the alkaline compound is reduced by adding an inorganic acid to the organic solvent (B) recovered by distillation and performing distillation again.
- Inorganic acids include hydrochloric acid, sulfuric acid, nitric acid, etc. Acids are preferred.
- an inorganic acid is added to the organic solvent (B) recovered by distillation, the inorganic acid reacts with an alkaline compound such as methylamine to form a salt (eg, hydrochloride), and the pH of the salt decreases. It is preferable to adjust the pH to less than 0.0 by adding an inorganic acid to the collected organic solvent (B) in order to efficiently remove an alkaline compound such as methylamine.
- the recovered organic solvent (B) is brought into contact with activated carbon to reduce the content of the alkaline compound.
- an inorganic acid such as hydrochloric acid from the viewpoint of controlling cost and pH.
- the organic solvent (B) used in the washing step ketones / alcohols are preferred, acetone and methanol are more preferred, and acetone is particularly preferred.
- the alkaline compound is typically methylamine.
- the content of the alkaline compound (for example, methylamine) in the organic solvent (B) recovered by distillation is adjusted to 3000 ppm or less by weight, preferably 2000 ⁇ pm or less. It is reduced to ⁇ or less, more preferably to 1000 ppm or less. Note that p pm is based on weight.
- the Tmc when a treatment for increasing the crystallization temperature (Tmc) is performed, the Tmc is 200 ° C or higher, preferably 210 ° C or higher, more preferably 220 ° C or higher, and the yellow index (YI)
- PAS 11.0 or less, preferably 10.0 or less, more preferably 7.0 or less
- a PAS having a yellow index (YI) of 15.0 or less, preferably 13.0 or less, more preferably 11.0 or less can be obtained.
- the melt viscosity (measured at a temperature of 310 ° C. and a shear rate of 1,216 sec- 1 ) of the PAS of the present invention is not particularly limited, but is preferably from 30 to 800 Pa ⁇ s, more preferably from 40 to 500 Pa ⁇ s. ⁇ Within s.
- PAS having a melt viscosity exceeding the melt viscosity of the prepolymer produced in the former step (step 1) is obtained.
- PAS obtained by the production method of the present invention can be used alone or after being oxidatively crosslinked, alone or, if desired, various inorganic fillers, fibrous fillers, and various synthetic fillers. It can be mixed with resin and molded into various injection molded products and extruded products such as sheets, films, fibers and pipes.
- the PAS obtained by the method of the present invention can stably perform these processes because the variation in melt viscosity between lots is small, and the molded product obtained is of high quality with little variation in various properties.
- PPS polyphenylene sulfide
- Vaporization chamber temperature 180 ° C
- F ID hydrogen flame ionization detector
- Carrier gas Nitrogen 30 m 1 Z min,
- the value was determined from a calibration curve using commercially available methylamine.
- the polymer was heated and melted by a hot press at 320 ° C and then rapidly cooled to form an amorphous sheet.
- DSC crystallization temperature
- the polymer was pressurized at room temperature with an electric press at 15 MPa for 1 minute to produce a tablet.
- the color tone was measured by a reflection light measurement method under the conditions of standard light C, a 2 ° field of view, and a colorimetric system, using TC-1800 manufactured by Tokyo Denshoku Technical Center. 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 tone of the sample was indicated by yellowness (yellow index: YI).
- the melt viscosity was measured by Toyo Seiki Capillograph 1-C.
- the capillaries used a flat die of ⁇ X 1 OmmL, and the set temperature was 310 ° C.
- the melt viscosity at a shear rate of 1,216 sec- 1 was measured.
- NMP N-methyl-2-pyrrolidone
- reaction solution is sieved through a 150 m (100 mesh) screen, Separation into a wet cake containing the granular polymer on the screen and components passed through the screen.
- the wet cake was contacted with high-purity acetone (containing no methylamine, 5 times the weight of the polymer) while stirring at room temperature for 10 minutes, and then a screen with an aperture of 150 ⁇ was used.
- the mixture was sieved and separated into a polymer component remaining on the screen and a component passing through the screen. The above operation was repeated once for the polymer component remaining on the screen.
- the liquid component (C) that passed through the screen was recovered in its entirety.
- the polymer component remaining on the screen is brought into contact with the polymer by 5 times the weight of ion-exchanged water while stirring at room temperature for 10 minutes, then separated with a screen having an aperture of 150 ⁇ , and screened again.
- the polymer component remaining on the top was recovered. This operation was repeated twice. Thereafter, the polymer component remaining on the recovered screen was brought into contact with a 0.6% by weight aqueous solution of acetic acid, which is 5 times the weight of the polymer, for 40 minutes, and then sieved with a screen having an aperture of 150 m.
- the polymer component remaining on the screen was recovered.
- the polymer component remaining on the screen was brought into contact with ion-exchanged water, which was 5 times the weight of the polymer, while stirring at room temperature for 10 minutes, and then sieved with a screen having an aperture of 150 ⁇ ⁇ , The polymer component remaining on the screen was recovered and dried at 105 ° C.
- the polymer recovered by the above operation was granular, had a melt viscosity of 144 Pas, a Tmc of 235 ° C, and a YI of 5.6.
- the components passing through the screen were NMP, a by-product salt, a low-molecular-weight PPS component, water, and organic compounds such as methylamine, which are polymerization solvents. Contains impurities.
- the components passing through the screen are separated into a liquid component (D1) and a solid component by centrifugation and decantation, and the solid component is 5 times higher in purity than the polymer by weight.
- Acetone is contacted and the mixture is liquid
- the liquid component (D2) was separated into the solid component and the solid component.
- the liquid components (C :), (Dl), and (D2) recovered in each of the above operations were mixed, and the mixture was subjected to simple distillation to recover acetone.
- the recovered acetone contained methylamine at a concentration of 200 ppm.
- washing solvent recovery step The steps (1) to (5) were performed in the same manner as described above, except that the acetone (methylamine amount 200 ppm) collected in step (5) was used in the polymer washing step and the polymerization solvent recovery step. went.
- acetone was recovered by simple distillation.
- the recovered acetone (second recovery acetone) had an increased methylamine content of 420 ppm.
- the acetone thus purified and recovered (the first acetone recovered by simplex distillation) had a reduced methylamine content of 20 ppm.
- the amount of methylamine in acetone recovered in the fifth time was 45 ppm, and the amount in the tenth time was 80 ppm. Table 2 shows the results.
- the acetone purified and recovered in this manner had a methylamine content reduced to 35 ppm.
- the amount of methylamine in the acetone recovered in the fifth time was 80 ppm and in the tenth was 170 ppm.
- Aqueous hydrochloric acid was added to the acetone (methylamine amount 4,710 ppm) collected in the 20th reference in Reference Example 1 to adjust the water content to about 30% by weight and the pH to 5.0, followed by simple distillation. When the acetone component was recovered, the amount of methylamine dropped to 190 ppm. Table 2 shows the results.
- Example 7 In the polymer washing step of Reference Example 1, the same procedure as in Reference Example 1 was carried out, except that acetone having a methylamine content of 80 ppm was used in the 10th recovery in Example 1 instead of high-purity acetone. As a result, the melt viscosity of the polymer was 140 Pa ⁇ s, Tmc ⁇ 232 ° C, and YI was 5.2. Table 3 shows the results. [Example 7]
- the crystallization temperature (Tmc) is determined by purifying the content of methylamine to 3000 ppm or less.
- a PPS with a force S of 200 ° C. or more and a yellow index (YI) of 11.0 or less can be obtained.
- the content of methylamine in acetone used for recycling is preferably 2000 ppm or less, more preferably lOppm or less, and particularly preferably 500 ppm or less.
- a method for producing a PAS which includes a step of recycling an organic solvent purified by reducing the content of impurities to be applied in a washing step.
- the quality of the PAS such as the crystallization temperature (Tmc) and the yellow index (YI) is not significantly reduced even if the organic solvent for washing is recovered and used repeatedly.
- a cleaning method which does not deteriorate the quality of PAS.
- a method for purifying an organic solvent for washing According to the present invention, the organic solvent for washing can be repeatedly recovered and purified and used, so that the cost can be reduced without lowering the quality of PAS.
- the method of the present invention is suitable for producing and washing large quantities of polyarylene sulfide in a large number of batches on an industrial scale.
Abstract
Description
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Priority Applications (7)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US10/540,834 US7632915B2 (en) | 2002-12-27 | 2003-12-19 | Production process and washing method of poly(arylene sulfide), and purification process of organic solvent used in washing |
KR1020057011985A KR101092194B1 (ko) | 2002-12-27 | 2003-12-19 | 폴리아릴렌술피드의 제조 방법 및 세정 방법, 및 세정에사용한 유기 용매의 정제 방법 |
EP03782837A EP1577337B1 (en) | 2002-12-27 | 2003-12-19 | Process for producing and method of cleaning polyarylene sulfide, and method of purifying organic solvent used for cleaning |
JP2004564499A JP4310279B2 (ja) | 2002-12-27 | 2003-12-19 | 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 |
DE60336503T DE60336503D1 (de) | 2002-12-27 | 2003-12-19 | Herstellungsverfahren und reinigungsverfahren für polyarylensulfid sowie reinigungsverfahren für die dabei verwendete organische lösung |
AU2003292586A AU2003292586A1 (en) | 2002-12-27 | 2003-12-19 | Process for producing and method of cleaning polyarylene sulfide, and method of purifying organic solvent used for cleaning |
AT03782837T ATE502972T1 (de) | 2002-12-27 | 2003-12-19 | Herstellungsverfahren und reinigungsverfahren für polyarylensulfid sowie reinigungsverfahren für die dabei verwendete organische lösung |
Applications Claiming Priority (2)
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JP2002-382176 | 2002-12-27 | ||
JP2002382176 | 2002-12-27 |
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WO2004060973A1 true WO2004060973A1 (ja) | 2004-07-22 |
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PCT/JP2003/016333 WO2004060973A1 (ja) | 2002-12-27 | 2003-12-19 | 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 |
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US (1) | US7632915B2 (ja) |
EP (1) | EP1577337B1 (ja) |
JP (1) | JP4310279B2 (ja) |
KR (1) | KR101092194B1 (ja) |
CN (1) | CN1326911C (ja) |
AT (1) | ATE502972T1 (ja) |
AU (1) | AU2003292586A1 (ja) |
DE (1) | DE60336503D1 (ja) |
WO (1) | WO2004060973A1 (ja) |
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- 2003-12-19 WO PCT/JP2003/016333 patent/WO2004060973A1/ja active Application Filing
- 2003-12-19 AT AT03782837T patent/ATE502972T1/de not_active IP Right Cessation
- 2003-12-19 JP JP2004564499A patent/JP4310279B2/ja not_active Expired - Fee Related
- 2003-12-19 CN CNB2003801076296A patent/CN1326911C/zh not_active Expired - Fee Related
- 2003-12-19 EP EP03782837A patent/EP1577337B1/en not_active Expired - Lifetime
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JP2013007050A (ja) * | 2007-01-05 | 2013-01-10 | Sk Chemicals Co Ltd | 明るさに優れるポリアリーレンスルフィド樹脂及び樹脂製品 |
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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 |
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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 |
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JP2014005317A (ja) * | 2012-06-21 | 2014-01-16 | Dic Corp | アルカリ金属含有無機塩を含む水溶液の製造方法およびカルボキシアルキルアミノ基含有化合物と非水溶性溶液を含む溶液の製造方法 |
CN110637046A (zh) * | 2017-10-20 | 2019-12-31 | 株式会社Lg化学 | 聚芳硫醚的制备方法 |
CN110637046B (zh) * | 2017-10-20 | 2022-01-18 | 株式会社Lg化学 | 聚芳硫醚的制备方法 |
Also Published As
Publication number | Publication date |
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EP1577337A4 (en) | 2007-06-20 |
DE60336503D1 (de) | 2011-05-05 |
US7632915B2 (en) | 2009-12-15 |
AU2003292586A1 (en) | 2004-07-29 |
JPWO2004060973A1 (ja) | 2006-05-11 |
US20060086374A1 (en) | 2006-04-27 |
CN1326911C (zh) | 2007-07-18 |
CN1732209A (zh) | 2006-02-08 |
JP4310279B2 (ja) | 2009-08-05 |
EP1577337A1 (en) | 2005-09-21 |
KR101092194B1 (ko) | 2011-12-13 |
EP1577337B1 (en) | 2011-03-23 |
KR20050087860A (ko) | 2005-08-31 |
ATE502972T1 (de) | 2011-04-15 |
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