WO2020256018A1 - Procédé de production de caoutchouc acrylique - Google Patents

Procédé de production de caoutchouc acrylique Download PDF

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Publication number
WO2020256018A1
WO2020256018A1 PCT/JP2020/023789 JP2020023789W WO2020256018A1 WO 2020256018 A1 WO2020256018 A1 WO 2020256018A1 JP 2020023789 W JP2020023789 W JP 2020023789W WO 2020256018 A1 WO2020256018 A1 WO 2020256018A1
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Prior art keywords
acrylic rubber
extruder
vent port
decompression
absolute pressure
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PCT/JP2020/023789
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English (en)
Japanese (ja)
Inventor
増田　浩文
和弘 江尻
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日本ゼオン株式会社
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Priority to CN202080042254.3A priority Critical patent/CN113993677A/zh
Publication of WO2020256018A1 publication Critical patent/WO2020256018A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B13/00—Conditioning or physical treatment of the material to be shaped
    • B29B13/06—Conditioning or physical treatment of the material to be shaped by drying
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B13/00—Conditioning or physical treatment of the material to be shaped
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B15/00—Pretreatment of the material to be shaped, not covered by groups B29B7/00 - B29B13/00
    • B29B15/02—Pretreatment of the material to be shaped, not covered by groups B29B7/00 - B29B13/00 of crude rubber, gutta-percha, or similar substances
    • B29B15/06—Washing devices
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F20/00—Homopolymers and copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and only one being terminated by only one carboxyl radical or a salt, anhydride, ester, amide, imide or nitrile thereof
    • C08F20/02—Monocarboxylic acids having less than ten carbon atoms, Derivatives thereof
    • C08F20/10—Esters
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F6/00—Post-polymerisation treatments

Definitions

  • the present invention relates to a method for producing acrylic rubber, and more particularly to a method for producing acrylic rubber that can appropriately reduce the water content of acrylic rubber while suppressing the occurrence of vent-up.
  • Acrylic rubber is widely used for functional parts mainly for automobile applications as a rubber material from which a crosslinked rubber product having excellent properties such as heat resistance and compression set resistance can be obtained. Further, in the process of producing acrylic rubber, a process of salting out the rubber polymer and then extruding and drying it with an extruder or the like is performed.
  • Patent Document 1 in a technique of extruding and drying a rubber polymer by an extruder or the like, a vent port that communicates with atmospheric pressure to depressurize and discharge the vaporized material to the atmosphere and a vent port that forcibly depressurizes and discharges the vaporized material
  • Patent Document 1 an extruder having a plurality of decompression vent ports is exemplified, but no mention is made as to what condition the absolute pressure of the plurality of decompression vent ports should be.
  • Patent Document 2 discloses a technique for extruding and drying a rubber polymer by an extruder or the like, in which the extruded rubber polymer is further dried by a sealed steam flow.
  • various conditions such as the amount of rubber polymer extruded from the tip of the extruder, the number of rotations of the screw of the extruder, the pressure of the polymer inside the tip of the extruder, and the specific energy of the extruder. The experimental results when the above is changed are disclosed.
  • Patent Documents 3 and 4 unlike the techniques of only dehydrating and drying the rubber polymer in the extruder as in Patent Document 1 and Patent Document 2, the salting of the rubber polymer and the salting of the rubber polymer in the extruder are provided. Following this, techniques for dehydration and drying are disclosed.
  • Patent Documents 3 and 4 an embodiment in which an extruder having a plurality of vent ports is used as an extruder is exemplified, but also in Patent Documents 3 and 4, the absolute pressure of the plurality of vent ports is set as any condition. No mention is made of this.
  • the acrylic rubber is dehydrated and dried in this order.
  • Drying following dehydration is usually performed by vacuum drying through a vacuum vent port.
  • molten acrylic rubber foams at the decompression vent port, causing vent-up in which the acrylic rubber flows into the decompression vent port, which reduces productivity. There was a problem that it would end up.
  • the present invention has been made in view of such an actual situation, and an object of the present invention is to provide a method for producing acrylic rubber, which can appropriately reduce the water content of acrylic rubber while suppressing the occurrence of vent-up. ..
  • the present inventors have used an extruder having a plurality of pressure reducing vent ports when drying acrylic rubber, and extruded the acrylic rubber.
  • the above object can be achieved by making the absolute pressure of the decompression vent port on the upstream side in the direction higher than the absolute pressure of the decompression vent port on the downstream side in the extrusion direction, and have completed the present invention.
  • it is a method for producing acrylic rubber, which comprises a drying step of drying acrylic rubber using an extruder in which screws are rotatably arranged inside a barrel.
  • an extruder one having a plurality of decompression vent ports was used.
  • a method for producing acrylic rubber in which the absolute pressure of the decompression vent port on the upstream side in the extrusion direction is made higher than the absolute pressure of the decompression vent port on the downstream side in the extrusion direction.
  • the difference between the absolute pressure of the decompression vent port on the upstream side in the extrusion direction and the absolute pressure of the decompression vent port on the downstream side in the extrusion direction is preferably in the range of 5.0 to 94.0 kPa.
  • the extruder having two or more decompression vent ports is used, and the absolute pressures of at least two decompression vent ports among the two or more decompression vent ports are extruded from the upstream side in the extrusion direction. It is preferable to set it so that it becomes lower in order toward the downstream side in the direction. In the present invention, it is preferable to use an extruder having a plurality of viewing windows at the plurality of pressure reducing vent ports.
  • the acrylic rubber is put into the extruder in a hydrous crumb state to dry the acrylic rubber.
  • the acrylic rubber is put into the extruder in a crumb state having a water content of 60 to 70% by weight to dry the acrylic rubber.
  • the extruder provided with a first discharge slit and a second discharge slit in order from the upstream side in the extrusion direction on the upstream side in the extrusion direction from the plurality of pressure reducing vent ports.
  • the processing amount of acrylic rubber dried by the extruder per unit time is Q [kg / h] and the rotation speed of the screw is N [rpm]
  • the following formula (1) is satisfied. Is preferable. 3 ⁇ Q / N ⁇ 8 (1)
  • a cleaning step of cleaning the acrylic rubber is further provided in the cleaning tank, and the cleaning step and the drying step are continuous steps in this order.
  • a method for producing an acrylic rubber which can appropriately reduce the water content of the acrylic rubber while suppressing the occurrence of vent-up.
  • FIG. 1 is a schematic view showing a cleaning tank and an extruder used in the method for producing acrylic rubber according to the embodiment of the present invention.
  • FIG. 2 is a schematic view showing a screw arranged inside the extruder.
  • FIG. 3 is a cross-sectional view taken along the line III-III of FIG. 1 and the line III-III of FIG.
  • the method for producing acrylic rubber of the present invention is a method for producing acrylic rubber, which comprises a drying step of drying the acrylic rubber using an extruder in which screws are rotatably arranged inside a barrel.
  • an extruder one having a plurality of decompression vent ports was used.
  • the absolute pressure of the decompression vent port on the upstream side in the extrusion direction is set higher than the absolute pressure of the decompression vent port on the downstream side in the extrusion direction.
  • the acrylic rubber used in the production method of the present invention has a (meth) acrylic acid ester monomer as a main component (preferably having 30% by weight or more in the total rubber monomer unit) in the molecule.
  • Acrylic acid ester monomer and / or methacrylic acid ester monomer are a rubber-like polymer containing a unit.
  • the (meth) acrylic acid ester monomer forming the (meth) acrylic acid ester monomer unit which is the main component of the acrylic rubber used in the production method of the present invention is not particularly limited, but for example, (meth) acrylic.
  • examples thereof include an acid alkyl ester monomer and a (meth) acrylic acid alkoxyalkyl ester monomer.
  • the (meth) acrylic acid alkyl ester monomer is not particularly limited, but an ester of alkanol having 1 to 8 carbon atoms and (meth) acrylic acid is preferable, and specifically, methyl (meth) acrylic acid, ( Ethyl acrylate, n-propyl (meth) acrylate, isopropyl (meth) acrylate, n-butyl (meth) acrylate, isobutyl (meth) acrylate, n-hexyl (meth) acrylate, (meth) Examples thereof include 2-ethylhexyl acrylate and cyclohexyl (meth) acrylate.
  • (meth) acrylic acid alkyl ester monomer having an alkyl group having 2 or more carbon atoms is preferable
  • ethyl (meth) acrylate and n-butyl (meth) acrylic acid are more preferable
  • acrylic acid is particularly preferred. These can be used alone or in combination of two or more.
  • the (meth) acrylic acid alkoxyalkyl ester monomer is not particularly limited, but an ester of an alkoxyalkyl alcohol having 2 to 8 carbon atoms and (meth) acrylic acid is preferable, and specifically, (meth) acrylic acid.
  • 2-ethoxyethyl (meth) acrylate and 2-methoxyethyl (meth) acrylate are preferable, and 2-ethoxyethyl acrylate and 2-methoxyethyl acrylate are particularly preferable. These can be used alone or in combination of two or more.
  • the (meth) acrylic acid ester monomer unit includes 30 to 100% by weight of the (meth) acrylic acid alkyl ester monomer unit, and the (meth) acrylic acid alkoxyalkyl ester. It is preferable to use a monomer unit consisting of 70 to 0% by weight.
  • the content of the (meth) acrylic acid ester monomer unit in the acrylic rubber used in the production method of the present invention is preferably 30% by weight or more, more preferably 50 to 99.9% by weight, still more preferably. It is 80 to 99.5% by weight, particularly preferably 95 to 99.5% by weight. If the content of the (meth) acrylic acid ester monomer unit is too small, the weather resistance, heat resistance, and oil resistance of the obtained rubber crosslinked product may decrease, while if it is too large, the obtained rubber crosslinked product may be deteriorated. The mechanical strength of the object may decrease.
  • the acrylic rubber used in the production method of the present invention may contain a crosslinkable monomer unit in addition to the (meth) acrylic acid alkyl ester monomer unit, if necessary.
  • the crosslinkable monomer forming the crosslinkable monomer unit is not particularly limited, and is, for example, an ⁇ , ⁇ -ethylene unsaturated carboxylic acid monomer; a monomer having an epoxy group; having a halogen atom. Monomer; diene monomer; and the like.
  • the ⁇ , ⁇ -ethylenically unsaturated carboxylic acid monomer forming the ⁇ , ⁇ -ethylenically unsaturated carboxylic acid monomer unit is not particularly limited, and is, for example, ⁇ , ⁇ - having 3 to 12 carbon atoms.
  • the acrylic rubber can be made into a carboxyl group-containing acrylic rubber having a carboxyl group as a cross-linking point, whereby a rubber cross-linked product can be obtained. , The compression resistance and permanent strain resistance can be further improved.
  • ⁇ , ⁇ -ethylenically unsaturated monocarboxylic acid having 3 to 12 carbon atoms include acrylic acid, methacrylic acid, ⁇ -ethylacrylic acid, crotonic acid, and cinnamic acid.
  • Specific examples of the ⁇ , ⁇ -ethylenically unsaturated dicarboxylic acid having 4 to 12 carbon atoms include butendioic acids such as fumaric acid and maleic acid; itaconic acid; citraconic acid; chloromaleic acid; and the like.
  • monoester of ⁇ , ⁇ -ethylenic unsaturated dicarboxylic acid having 4 to 12 carbon atoms and alkanol having 1 to 8 carbon atoms include monomethyl fumarate, monoethyl fumarate, mono n-butyl fumarate, and malein.
  • Itaconic acid monochain alkyl esters such as monomethyl acid, monoethyl maleate, monon-butyl maleate; monocyclopentyl fumarate, monocyclohexyl fumarate, monocyclohexenyl fumarate, monocyclopentyl maleate, monocyclohexyl maleate, maleine
  • examples thereof include butenedioic acid monoesters having an alicyclic structure such as monocyclohexenyl acid acid; itaconic acid monoesters such as monomethyl itaconic acid, monoethyl itaconic acid, monon-butyl itaconic acid, and monocyclohexyl itaconic acid.
  • a monoester of ⁇ , ⁇ -ethylenically unsaturated dicarboxylic acid having 4 to 12 carbon atoms and an alkanol having 1 to 8 carbon atoms is preferable, and a monoester of butendioic acid or butendion having an alicyclic structure Acid monoesters are more preferred, mono-n-butyl fumarate, mono n-butyl maleate, monocyclohexyl fumarate, and monocyclohexyl maleate are even more preferred, and mono n-butyl fumarate is particularly preferred.
  • These ⁇ , ⁇ -ethylenically unsaturated carboxylic acid monomers can be used alone or in combination of two or more.
  • the dicarboxylic acid also includes those existing as anhydrides.
  • the monomer having an epoxy group is not particularly limited, and for example, an epoxy group-containing (meth) acrylic acid ester such as glycidyl (meth) acrylate; an epoxy group-containing ether such as allyl glycidyl ether and vinyl glycidyl ether; Can be mentioned.
  • the monomer having a halogen atom is not particularly limited, and for example, an unsaturated alcohol ester of a halogen-containing saturated carboxylic acid, a (meth) acrylic acid haloalkyl ester, a (meth) acrylic acid haloacyloxyalkyl ester, or (meth) acrylic.
  • an unsaturated alcohol ester of a halogen-containing saturated carboxylic acid a (meth) acrylic acid haloalkyl ester, a (meth) acrylic acid haloacyloxyalkyl ester, or (meth) acrylic.
  • acrylic include acid (haloacetylcarbamoyloxy) alkyl esters, halogen-containing unsaturated ethers, halogen-containing unsaturated ketones, halomethyl group-containing aromatic vinyl compounds, halogen-containing unsaturated amides, and haloacetyl group-containing unsaturated monomers.
  • unsaturated alcohol esters of halogen-containing saturated carboxylic acids include vinyl chloroacetate, vinyl 2-chloropropionate, and allyl chloroacetate.
  • Specific examples of the (meth) acrylic acid haloalkyl ester include chloromethyl (meth) acrylic acid, 1-chloroethyl (meth) acrylic acid, 2-chloroethyl (meth) acrylic acid, and 1,2-dichloroethyl (meth) acrylic acid. , 2-Chloropropyl (meth) acrylic acid, 3-chloropropyl (meth) acrylic acid, and 2,3-dichloropropyl (meth) acrylic acid.
  • (meth) acrylic acid haloacyloxyalkyl ester examples include (meth) acrylic acid 2- (chloroacetoxy) ethyl, (meth) acrylic acid 2- (chloroacetoxy) propyl, and (meth) acrylic acid 3- (chloro). Examples thereof include acetoxy) propyl and 3- (hydroxychloroacetoxy) propyl (meth) acrylate.
  • (meth) acrylic acid (haloacetylcarbamoyloxy) alkyl ester examples include 2- (chloroacetylcarbamoyloxy) ethyl (meth) acrylic acid and 3- (chloroacetylcarbamoyloxy) propyl (meth) acrylic acid. Can be mentioned.
  • halogen-containing unsaturated ether examples include chloromethyl vinyl ether, 2-chloroethyl vinyl ether, 3-chloropropyl vinyl ether, 2-chloroethyl allyl ether, 3-chloropropyl allyl ether and the like.
  • halogen-containing unsaturated ketone examples include 2-chloroethyl vinyl ketone, 3-chloropropyl vinyl ketone, 2-chloroethyl allyl ketone and the like.
  • halomethyl group-containing aromatic vinyl compound examples include p-chloromethylstyrene, m-chloromethylstyrene, o-chloromethylstyrene, and p-chloromethyl- ⁇ -methylstyrene.
  • halogen-containing unsaturated amide examples include N-chloromethyl (meth) acrylamide.
  • haloacetyl group-containing unsaturated monomer examples include 3- (hydroxychloroacetoxy) propylallyl ether and p-vinylbenzylchloroacetic acid ester.
  • Examples of the diene monomer include a conjugated diene monomer and a non-conjugated diene monomer.
  • Specific examples of the conjugated diene monomer include 1,3-butadiene, isoprene, and piperylene.
  • Specific examples of the non-conjugated diene monomer include ethylidene norbornene, dicyclopentadiene, dicyclopentadienyl (meth) acrylate, and 2-dicyclopentadienyl ethyl (meth) acrylate. ..
  • the acrylic rubber when an ⁇ , ⁇ -ethylenically unsaturated carboxylic acid monomer is used, the acrylic rubber can be a carboxyl group-containing acrylic rubber.
  • a carboxyl group-containing acrylic rubber as the acrylic rubber, it is possible to improve the compression resistance and permanent strain resistance while improving the oil resistance and heat resistance.
  • the content of the crosslinkable monomer unit in the acrylic rubber used in the production method of the present invention is preferably 0.01% by weight or more, more preferably 0.1 to 50% by weight, still more preferably 0. It is 5 to 20% by weight, particularly preferably 0.5 to 5% by weight.
  • the acrylic rubber used in the production method of the present invention is, in addition to the (meth) acrylic acid ester monomer unit and the crosslinkable monomer unit used as needed, other monomers copolymerizable with these. It may have a unit of.
  • Other such copolymerizable monomers include aromatic vinyl monomers, ⁇ , ⁇ -ethylenic unsaturated nitrile monomers, acrylamide-based monomers, and ⁇ , ⁇ -ethylenic unsaturated dicarboxylics. Examples thereof include acid diester monomers and other olefin-based monomers.
  • aromatic vinyl monomer examples include styrene, ⁇ -methylstyrene, and divinylbenzene.
  • Examples of the ⁇ , ⁇ -ethylenically unsaturated nitrile monomer include acrylonitrile and methacrylonitrile.
  • Examples of the acrylamide-based monomer include acrylamide and methacrylamide.
  • the ⁇ , ⁇ -ethylenic unsaturated dicarboxylic acid diester monomer is a maleic acid dialkyl ester such as dimethyl maleate or din-butyl maleate having an alkyl group having 1 to 18 carbon atoms; fumaric acid.
  • a fumaric acid dialkyl ester such as dimethyl or din-butyl fumarate having an alkyl group having 1 to 18 carbon atoms; a dicyclopentyl maleate such as dicyclopentyl maleate or dicyclohexyl maleate and a cycloalkyl ester.
  • a group having 4 to 16 carbon atoms a dicycloalkyl ester of fumaric acid such as dicyclopentyl fumarate and dicyclohexyl fumarate having a cycloalkyl group having 4 to 16 carbon atoms; dimethyl itaconate, di-itaconate Itaconic acid dialkyl ester such as n-butyl having an alkyl group having 1 to 18 carbon atoms: an itaconic acid dicycloalkyl ester such as dicyclohexyl itaconate having a cycloalkyl group having 4 to 16 carbon atoms. ; And so on.
  • olefin-based monomers include ethylene, propylene, vinyl chloride, vinylidene chloride, vinyl acetate, ethyl vinyl ether, and butyl vinyl ether.
  • styrene, acrylonitrile, methacrylonitrile, ethylene and vinyl acetate are preferable, and acrylonitrile, methacrylonitrile, and ethylene are more preferable.
  • copolymerizable monomers can be used alone or in combination of two or more.
  • the content of the unit of these other copolymerizable monomers in the acrylic rubber of the present invention is usually 49.9% by weight or less, preferably 19.5% by weight or less, and more preferably 10% by weight or less. , More preferably 4.5% by weight or less.
  • the content may be in the above range.
  • the content of ethylene units is preferably 10% by weight or less, and more preferably 4.5% by weight or less.
  • the acrylic rubber used in the production method of the present invention has an acrylonitrile unit or a methacrylonitrile unit, the total content of the acrylonitrile unit and the methacrylonitrile unit shall be 10% by weight or less. It is preferable to use 4.5% by weight or less.
  • the acrylic rubber used in the production method of the present invention is preferably obtained by polymerizing each of the above monomers.
  • any of an emulsion polymerization method, a suspension polymerization method, a massive polymerization method, and a solution polymerization method can be used, but from the viewpoint of ease of control of the polymerization reaction, known acrylic rubber It is preferable to use an emulsion polymerization method or a solution polymerization method under normal pressure, which is generally used as a production method.
  • acrylic rubber is obtained in the form of latex (latex of acrylic rubber).
  • acrylic rubber can be obtained in the form of a polymer solution (polymer solution of acrylic rubber).
  • the polymerization may be a batch type, a semi-batch type, or a continuous type.
  • the polymerization is usually carried out in a temperature range of 0 to 70 ° C, preferably 5 to 50 ° C.
  • Acrylic rubber hydrous crumb specifically, a mixture of acrylic rubber crumb and serum water (hereinafter referred to as "clam slurry") can be obtained.
  • the serum water means water that may contain a coagulant, a polymerization auxiliary material residue, or the like (a coagulant, a polymerization auxiliary material residue, or the like may be dissolved or dispersed).
  • serum water either the water associated with the acrylic rubber crumb or the water accompanying the acrylic rubber crumb and later separated is defined as serum water.
  • the serum water is used including the case where the type and amount of the dissolved or dispersed components are changed due to washing or drying.
  • the coagulant include calcium chloride, magnesium chloride, sodium chloride, magnesium sulfate, barium chloride and the like.
  • FIG. 1 is a schematic view showing a cleaning tank and an extruder used in the method for producing acrylic rubber according to the embodiment of the present invention.
  • the washing tank and the extruder according to the embodiment shown in FIG. 1 are used as the manufacturing apparatus used in the method for manufacturing the acrylic rubber of the present invention
  • emulsion polymerization or solution polymerization will be carried out as described above.
  • the crumb slurry (more specifically, the water-containing crumb contained in the crumb slurry) obtained by solidification is washed and then dried to obtain a solid acrylic rubber. The method will be described.
  • the manufacturing apparatus includes an extruder 1 and a cleaning tank 7.
  • the crumb slurry obtained according to the above method is continuously supplied to the washing tank 7, and the water-containing crumb contained in the crumb slurry is washed in the washing tank 7.
  • the washed clam slurry (more specifically, the clam slurry containing the washed hydrous crumb) is continuously discharged from the washing tank 7, and the continuously discharged clam slurry (more specifically).
  • the clam slurry containing the washed hydrous crumb is continuously supplied to the feed port 310 of the extruder 1 from the discharge port provided in the washing tank 7.
  • the washed crumb slurry is continuously discharged from the discharge port provided in the washing tank 7 and passes through the water removal facility 8 (for example, draining by a screen) shown in FIG.
  • the water removal facility 8 for example, draining by a screen
  • the feed port 310 of the extruder 1 After some water has been removed, it is continuously supplied to the feed port 310 of the extruder 1 in the state of a hydrous crumb (that is, the state of a crumb containing water) or the state of a crumb slurry. It has become. If it is in the state of a hydrous crumb, it may be accompanied by water.
  • the hydrous crumb or the crumb slurry supplied to the feed port 310 of the extruder 1 is dried in the extruder 1 as described later.
  • cleaning by the cleaning tank 7 and drying by the extruder 1 are performed in a continuous process, so that space saving and improvement of production efficiency are possible. Furthermore, it is possible to improve the production stability by performing it in a continuous process
  • the method for cleaning the clam slurry (more specifically, the water-containing crumb contained in the clam slurry) by the cleaning tank 7 is not particularly limited, but the cleaning tank 7 is supplied with cleaning water together with the clam slurry for cleaning.
  • a method of stirring by a stirring blade provided in the tank 7 can be mentioned.
  • the amount of washing water supplied with respect to 100 parts by weight of the crumb is preferably 900 to 9900 parts by weight, more preferably 1570 to 4900 parts by weight, from the viewpoint of effectively performing washing.
  • the embodiment in which one cleaning tank 7 is provided is illustrated in FIG. 1, the embodiment in which two or more cleaning tanks are provided in multiple stages may be configured to perform cleaning a plurality of times.
  • the extruder 1 has a drive unit 2 and a single barrel 3 composed of 11 divided barrel blocks 31 to 41. Inside the barrel 3, a supply zone 100, a dehydration zone 102, and a drying zone 104 are sequentially formed from the upstream side to the downstream side of the barrel 3.
  • the supply zone 100 is a region for supplying the hydrous crumb or the crumb slurry continuously supplied from the cleaning tank 7 to the inside of the barrel 3.
  • the dehydration zone 102 is a region for separating and discharging a liquid (serum water) containing a coagulant or the like from the hydrous crumb or crumb slurry.
  • the drying zone 104 is a region for drying the dehydrated crumbs.
  • the inside of the barrel block 31 corresponds to the supply zone 100
  • the inside of the barrel blocks 32 to 34 corresponds to the dehydration zone 102
  • the inside of the barrel blocks 35 to 41 corresponds to the drying zone 104.
  • the number of barrel blocks installed can be optimized according to the composition of the acrylic rubber to be handled, and is not limited to the mode shown in FIG.
  • a feed port 310 for receiving a water-containing crumb or a crumb slurry was formed in the barrel block 31 constituting the supply zone 100, and a part of water was removed from the washing tank 7 through the screen 8 in the feed port 310. , Hydrous crumbs or crumb slurries are continuously fed. Further, the barrel blocks 32 and 34 forming the dehydration zone 102 are formed with a first discharge slit 320 and a second discharge slit 340 for draining the water contained in the water-containing crumb, respectively. Further, in the barrel blocks 36, 38, 39, 40 which form a part of the drying zone 104, the first decompression vent port 360 for removing volatile substances such as water contained in the crumb after dehydration by degassing. , The second decompression vent port 380, the third decompression vent port 390, and the fourth decompression vent port 400 are formed, respectively.
  • FIG. 2 is a schematic view showing a screw arranged inside the extruder 1.
  • a screw 6 as shown in FIG. 2 is arranged inside the barrel 3.
  • a drive means such as a motor housed in a drive unit 2 (see FIG. 1) is connected to the base end of the screw 6 in order to drive the screw 6, whereby the screw 6 is rotatably held. ..
  • the shape of the screw 6 is not particularly limited, but it is preferable to appropriately combine a screw block having various screw configurations and a kneading disc.
  • the screw 6 can be configured to have different screw configurations in the regions corresponding to the zones 100, 102, and 104 described above formed inside the barrel 3.
  • the L / Da is preferably 20 to 60. Is.
  • the outer diameter Da of the screw 6 is defined by the diameter of the peak portion 60A (see FIG. 3) of the screw block 60 constituting the screw when viewed from the axial direction.
  • FIG. 3 is a cross-sectional view taken along the lines III-III of FIG. 1 and the line III-III of FIG. 2, and the cross-sectional view shown in FIG. 3 is a cross-sectional view of the screw block 60 portion of the extruder 1. It is sectional drawing which crosses the valley part 60B. That is, as shown in FIG. 3, the two screws 6 and 6 mesh the peak portion 60A of the screw block 60 of one screw 6 with the valley portion 60B of the screw block 60 of the other screw 6 and one of them.
  • the mixing property in each zone 100, 102, 104 can be improved.
  • the rotation directions of the two screws 6 may be the same direction or different directions, but from the viewpoint of self-cleaning performance, a type that rotates in the same direction is preferable.
  • Da / Di is preferable. Is in the range of 1.2 to 2.5.
  • the relationship between L1 and the entire length of the screw 6 described above is L (mm) L1.
  • / L is preferably 0.2 to 0.9.
  • a die 5 for extruding the acrylic rubber dehydrated and dried in the barrel 3 into a predetermined shape and commercializing it is connected to the downstream side of the barrel block 41 described above, for example, drying.
  • the acrylic rubber can be extruded into a sheet.
  • the crumb slurry washed by the washing tank 7 is passed through a water removing facility 8 (for example, draining with a screen) to remove a part of water, and the acrylic rubber crumb is used. Is continuously supplied to the feed port 310 provided in the barrel block 31 in the state of a water-containing crumb or a crumb slurry in which a part of water has been removed.
  • the clam slurry washed by the washing tank 7 is continuously supplied from the washing tank 7 directly (or via a predetermined clam slurry flow path) to the feed port 310 provided in the barrel block 31. May be good.
  • the amount of the coagulant contained in the finally obtained dried acrylic rubber can be suppressed to a low level, and From the viewpoint of reducing the slipping out of the crumb from the first discharge slit 320, which will be described later, it is preferable that the water content is relatively high.
  • the water content of the crumb supplied to the feed port 310 is , It is preferably 50 to 70% by weight, more preferably 58 to 70% by weight, and even more preferably 60 to 70% by weight.
  • the water content of the clam supplied to the feed port 310 includes, for example, the water content of the clam slurry before cleaning supplied to the cleaning tank 7, the amount of cleaning water supplied to the cleaning tank 7, and water such as a slit screen. It can be controlled by adjusting through the removal equipment 8.
  • the average crumb diameter of the crumb-shaped acrylic rubber contained in the hydrous crumb or the crumb slurry supplied to the feed port 310 is not particularly limited, but is preferably 0.1 to 10 mm from the viewpoint of improving the drying efficiency. , More preferably 1.0 to 5.0 mm.
  • the average crumb diameter of the crumb-shaped acrylic rubber can be controlled by adjusting the solidification conditions at the time of solidification.
  • the temperature of the hydrous crumb or the crumb slurry supplied to the feed port 310 is preferably 30 to 90 ° C., more preferably 40 to 90 ° C., still more preferably 50 to 85, from the viewpoint of ensuring sufficient drying efficiency. °C.
  • the temperature of the hydrous crumb or crumb slurry supplied to the feed port 310 is the polymerization temperature of acrylic rubber, the temperature of the coagulant used for coagulation (for example, the temperature of the coagulant aqueous solution), and the temperature of the washing water when washing by the washing tank 7. It can be controlled by adjusting such as.
  • the barrel temperature in the barrel block 31 constituting the supply zone 100 is not particularly limited, but is preferably 30 to 150 ° C., more preferably 40 to 140 ° C. from the viewpoint of improving the drying efficiency while suppressing the deterioration of the acrylic rubber. Is.
  • the hydrous crumb or crumb slurry supplied to the feed port 310 is sent from the supply zone 100 to the dehydration zone 102 by the rotation of the screw 6.
  • the water-containing crumb or serum water contained in the crumb slurry (more specifically, more specifically, (Serum water separated from the crumbs) is discharged to obtain a hydrous crumb in a state of preferably containing 10 to 50% by weight of water, more preferably 10 to 40% by weight of water. Can be done.
  • the barrel temperature in the barrel blocks 32 to 34 constituting the dehydration zone 102 is not particularly limited, but is preferably 30 to 170 ° C., more preferably 40 to 170 ° C. from the viewpoint of increasing the dehydration efficiency while suppressing the deterioration of the acrylic rubber. It is 160 ° C.
  • the water-containing crumb obtained in the dehydration zone 102 is sent to the drying zone 104 by the rotation of the screw 6.
  • the crumb sent to the drying zone 104 is plasticized and kneaded by the rotation of the screw 6 to form a melt, which generates heat and is carried to the downstream side while raising the temperature.
  • the melt reaches the decompression vent ports 360, 380, 390, 400 provided in the barrel blocks 36, 38, 39, 40, the pressure is released, so that the moisture contained in the melt is released. Volatile matter is separated and vaporized.
  • the decompression vent ports 360, 380, 390, and 400 are connected to a decompression pump via a decompression pipe connected to the side surface of each decompression vent port so that the pressure is reduced. It is configured in. Further, the decompression vent ports 360, 380, 390, and 400 are provided with a valve (not shown) for adjusting the absolute pressure and a pressure gauge (not shown) for measuring the absolute pressure. The absolute pressure can be adjusted. In addition, in FIG. 1, the decompression vent ports 360, 380, 390, and 400 are illustrated as being connected to the same decompression pump through a decompression pipe, but the present invention is not particularly limited to such an embodiment and is separate. May be connected to a decompression pump.
  • the absolute of the fourth vacuum vent 400 positioned absolute pressure P 1 of the first vacuum vent port 360 which is located on the most upstream side of the vacuum vent port 360,380,390,400, on the most downstream side It shall be higher than the pressure P 4 (P 1 > P 4 ).
  • the absolute pressure P 1 of the first decompression vent port 360 may be higher than the absolute pressure P 4 of the fourth decompression vent port 400 (P 1 > P 4 ) (that is, the most upstream).
  • the absolute pressure of the decompression vent port on the side may be higher than the absolute pressure of the decompression bend port on the most downstream side), and the difference between these pressures shall be in the range of 5.0 to 94.0 kPa.
  • the range is preferably 9.0 to 92.0 kPa, more preferably 18.0 to 88.0 kPa.
  • the absolute pressure P 1 of the first decompression vent port 360 represents the absolute pressure of the most upstream decompression vent port
  • the absolute pressure P 4 of the fourth decompression vent port 400 is the most downstream decompression vent port. Represents the absolute pressure of.
  • the absolute pressure P 1 of the first decompression vent port 360 may be higher than the absolute pressure P 4 of the fourth decompression vent port 400 (P 1 > P 4 ).
  • the absolute pressure of the decompression vent port is not particularly limited, but the absolute pressure of the first decompression vent port 360 is preferably 7.3 to 96.3 kPa, more preferably 11.3 to 94.3 kPa. It is more preferably 21.3 to 91.3 kPa.
  • an absolute pressure P 1 of the first vacuum vent port 360 as long as greater than the absolute pressure P 4 of the fourth vacuum vent 400, the absolute of the second vacuum vent port 380
  • the absolute pressure of each decompression vent port may be appropriately set so as to have the above relationship, and is not particularly limited, but the absolute pressure of the second decompression vent port 370 is preferably 2.3 to 91.3 kPa. It is more preferably 6.3 to 81.3 kPa, and even more preferably 11.3 to 71.3 kPa.
  • the absolute pressure of the third decompression vent port 380 is preferably 2.3 to 61.3 kPa, more preferably 3.3 to 51.3 kPa, and 3.3 to 46.3 kPa.
  • the absolute pressure of the fourth decompression vent port 400 is preferably 2.3 to 51.3 kPa, more preferably 3.3 to 41.3 kPa, and 3.3 to 36.3 kPa. It is more preferable to do so.
  • the absolute pressure of the fourth decompression vent port 400 when relatively low, preferably 2.3 to 21.3 kPa, more preferably 2.3 to 11.3 kPa, the first decompression vent the absolute pressure P 1 of the mouth 360, the difference in pressure between the absolute pressure P 4 of the fourth vacuum vent 400, preferably in the range of 60 ⁇ 94.0kPa, more preferably 70 ⁇ 94.0kPa, further It is preferably 80 to 88.0 kPa.
  • the absolute pressure of the fourth decompression vent port 400 is relatively high, preferably 22.3 to 51.3 kPa, more preferably 26.3 to 41.3 kPa, and even more preferably 28.3 to 36.3 kPa.
  • the absolute pressure P 1 of the first vacuum vent port 360 that the difference in pressure between the absolute pressure P 4 of the fourth vacuum vent port 400, in the range of 5.0 ⁇ 25 kPa preferably , More preferably 5.0 to 20 kPa, still more preferably 7.0 to 15 kPa.
  • glass viewing windows 361, 381, 391, 401 are formed on the upper surfaces of the decompression vent ports 360, 380, 390, and 400 so that the inside of the decompression vent can be confirmed. This makes it easy to confirm the presence or absence of vent-up, and even if vent-up occurs at a stage where the operating conditions are not stable, such as at the beginning of operation, such vent-up will occur in a timely manner. Can be found.
  • the barrel temperature in the barrel blocks 35 to 41 constituting the drying zone 104 is not particularly limited, but volatile components such as water contained in the acrylic rubber melt while appropriately suppressing the vent-up of the acrylic rubber melt. From the viewpoint that the removal efficiency of the rubber can be further improved, the temperature is preferably 100.0 to 220.0 ° C, more preferably 105.0 to 210.0 ° C.
  • the crumb from which the water has passed through the drying zone 104 is sent out to the outlet side by the screw 6, and is in a state of substantially containing almost no water, specifically, the water content is preferably 1.0. It is introduced into the die 5 in a state of being reduced to less than% by weight, more preferably 0.1 to 0.8% by weight, where it is discharged, for example, in the form of a sheet, cooled if necessary, and then a sheet cutter ( It is introduced into (not shown) and cut to an appropriate length.
  • the processing amount Q of the acrylic rubber to be dried per unit time is the processing amount [kg / kg / kg / kg / of acrylic rubber to be dried in one hour when the extrusion drying process is performed once in the extruder 1. h].
  • the rotation speed N of the screw 6 is the rotation speed [rpm] when the screw 6 rotates inside the barrel 3 in 1 minute in the extruder 1.
  • Q / N is preferably 3 ⁇ Q / N ⁇ 8, more preferably 3.5 ⁇ Q / N ⁇ 7, still more preferably 4 ⁇ Q / N ⁇ 6, and particularly preferably 4.5 ⁇ .
  • Q / N ⁇ 5.5 is preferably 3 ⁇ Q / N ⁇ 8, more preferably 3.5 ⁇ Q / N ⁇ 7, still more preferably 4 ⁇ Q / N ⁇ 6, and particularly preferably 4.5 ⁇ .
  • the absolute pressure P 1 of the first vacuum vent port 360 because it is an higher than the absolute pressure P 4 of the fourth vacuum vent 400, a "Q / N" above range Even in the case of, the vent-up can be appropriately suppressed, and thus the effect of setting "Q / N" in the above range, specifically, the acrylic rubber in which the water content is appropriately reduced can be obtained. It is possible to effectively enhance the effect of being able to produce with high productivity.
  • the Mooney viscosity (ML1 + 4, 100 ° C.) (polymer Mooney) of the acrylic rubber produced by the production method of the present embodiment is not particularly limited, but is preferably 10 to 80, more preferably 20 to 70, and even more preferably. It is 25 to 60.
  • a method for producing acrylic rubber which comprises a drying step of drying acrylic rubber using an extruder in which a screw is rotatably arranged inside a barrel.
  • the extruder one having a plurality of decompression vent ports was used. It is possible to provide a method for producing acrylic rubber in which the absolute pressure of the decompression vent port on the upstream side in the extrusion direction is made higher than the absolute pressure of the decompression vent port on the downstream side in the extrusion direction.
  • the water content of the acrylic rubber can be appropriately reduced while suppressing the occurrence of vent-up.
  • any embodiment may include an aspect in which the absolute pressure is lower than that of the pressure reducing vent port on the side, and the specific embodiment thereof is not particularly limited.
  • a method for producing acrylic rubber which comprises a drying step of drying acrylic rubber using an extruder in which a screw is rotatably arranged inside a barrel.
  • a method for producing acrylic rubber can be provided, in which the extruder is provided with a pressure reducing vent port having a viewing window. According to the invention according to the second aspect of the present invention, it is possible to easily confirm the presence or absence of the occurrence of vent-up.
  • a method for producing acrylic rubber which comprises a drying step of drying acrylic rubber using an extruder in which a screw is rotatably arranged inside a barrel.
  • a method for producing acrylic rubber in which acrylic rubber is put into the extruder in a crumb state having a water content of 60 to 70% by weight to dry the acrylic rubber.
  • the amount of the coagulant contained in the finally obtained dried acrylic rubber can be suppressed to a low level, and the clam slit is removed from the drainage slit. Can be reduced.
  • a method for producing acrylic rubber which comprises a drying step of drying acrylic rubber using an extruder in which a screw is rotatably arranged inside a barrel.
  • the method is provided. 3 ⁇ Q / N ⁇ 8 (1) According to the invention according to the fourth aspect of the present invention, it is possible to effectively enhance the effect that acrylic rubber having an appropriately reduced water content can be produced with high productivity.
  • a cleaning process that cleans acrylic rubber in the cleaning tank A method for producing acrylic rubber, which comprises a drying step of drying acrylic rubber using an extruder in which a screw is rotatably arranged inside a barrel, and the washing step and the drying step are continuous steps. Provided. According to the invention according to the fifth aspect of the present invention, it is possible to save space and improve production efficiency, and further, it is possible to improve production stability.
  • ⁇ Synthesis example 1 200 parts of water, 3 parts of sodium lauryl sulfate and 15 parts of ethyl acrylate, 55 parts of n-butyl acrylate, 28 parts of methoxyethyl acrylate in a polymerization reactor equipped with a thermometer, agitator, nitrogen introduction tube and decompression device. And 2 parts of mono-n-butyl fumarate were charged. After that, oxygen was sufficiently removed by repeating degassing and nitrogen substitution under reduced pressure, and then 0.002 parts of sodium formaldehyde sulfoxylate and 0.005 parts of cumene hydroperoxide were added to carry out an emulsion polymerization reaction at normal pressure and normal temperature.
  • Acrylic rubber latex was obtained by starting and continuing the reaction until the polymerization conversion rate reached 95%. Next, the obtained latex of acrylic rubber was coagulated with an aqueous calcium chloride solution to obtain a slurry of acrylic rubber (solid content concentration: 32% by weight).
  • Example 1 The acrylic rubber slurry obtained in Synthesis Example 1 was washed and dried using the washing tank 7 and the extruder 1 shown in FIG. 1 to obtain a solid acrylic rubber.
  • the supply rate of acrylic rubber to the cleaning tank 7 when cleaning in the cleaning tank 7 is 500 kg / h (supply rate in terms of solid rubber content), and the cleaning water is supplied to the cleaning tank 7. Washing was performed at a rate of 12000 kg / h.
  • the acrylic rubber slurry after cleaning is passed through the water removal facility 8 (slit screen) from the cleaning tank 7 as a water content crumb (moisture content: 60% by weight) of the acrylic rubber (a mode in which water is accompanied by the water content crumb).
  • the supply rate of 1250 kg / h to the extruder 1 (supply rate in terms of acrylic rubber (that is, the amount of acrylic rubber to be dried Q). ) was supplied at 500 kg / h) and dried by the extruder 1. Further, the temperature of the water-containing crumb of acrylic rubber at the time of charging into the extruder 1 was set to 40 ° C.
  • the conditions for drying by the extruder 1 are the barrel temperature of the supply zone 100: 80 ° C., the barrel temperature of the dehydration zone 102: 130 ° C., and the barrel temperature of the drying zone 104: 160 ° C., and the absolute pressure reducing vent port 360 of the first decompression vent port 360.
  • absolute pressure of the third decompression vent port 390 4 kPa
  • absolute pressure of the fourth decompression vent port 400 4 kPa (first decompression vent).
  • the water content of the water-containing crumb after passing through the dehydration zone 102 was 40% by weight.
  • the washing tank 7 and the extruder 1 are used to wash the acrylic rubber slurry and dry the water-containing crumb of the acrylic rubber to continuously obtain a solid acrylic rubber for 2 hours continuously.
  • vent-up of each decompression vent port did not occur, and the obtained solid acrylic rubber also had a water content reduced to 0.7% by weight.
  • the Mooney viscosity (ML1 + 4, 100 ° C.) (measured according to JIS K6300-1; the same applies hereinafter) of the obtained solid acrylic rubber was 32.
  • Example 2 The absolute pressure of each decompression vent port when drying by the extruder 1 is as follows: absolute pressure of the first decompression vent port 360: 41.3 kPa, absolute pressure of the second decompression vent port 380: 41.3 kPa, third decompression vent.
  • the absolute pressure of the port 390 was 36.3 kPa
  • the absolute pressure of the fourth decompression vent port 400 was 31.3 kPa (the difference between the absolute pressure of the first decompression vent port 360 and the absolute pressure of the fourth decompression vent port 400).
  • the operation of washing the acrylic rubber slurry and drying the acrylic rubber-containing crumb to continuously obtain solid acrylic rubber was continuously performed for 2 hours in the same manner as in Example 1. I went.
  • Example 2 the water content of the water-containing crumb after passing through the dehydration zone 102 was 40% by weight. As a result, also in Example 2, vent-up of each decompression vent port did not occur, and the obtained solid acrylic rubber also had a water content reduced to 0.2% by weight.
  • the Mooney viscosity (ML1 + 4, 100 ° C.) of the obtained solid acrylic rubber was 34.
  • Example 3 The acrylic rubber slurry obtained in Synthesis Example 1 was washed and dried using the washing tank 7 and the extruder 1 shown in FIG. 1 to obtain a solid acrylic rubber.
  • the supply rate of acrylic rubber to the cleaning tank 7 is 400 kg / h (supply rate in terms of solid rubber content), and the cleaning water is supplied to the cleaning tank 7. Washing was performed at a rate of 9600 kg / h.
  • the acrylic rubber slurry after cleaning is passed through the water removal facility 8 (slit screen) from the cleaning tank 7 as a water content crumb (moisture content: 60% by weight) of the acrylic rubber (a mode in which water is accompanied by the water content crumb).
  • the extruder 1 In the state where the water content is 60% by weight, the extruder 1 is supplied with a supply rate of 1000 kg / h (supply rate in terms of acrylic rubber (that is, the amount of acrylic rubber to be dried Q). ) was supplied at 400 kg / h) and dried by the extruder 1. Further, the temperature of the water-containing crumb of acrylic rubber at the time of charging into the extruder 1 was set to 40 ° C.
  • the conditions for drying by the extruder 1 are the barrel temperature of the supply zone 100: 80 ° C., the barrel temperature of the dehydration zone 102: 130 ° C., and the barrel temperature of the drying zone 104: 160 ° C., and the absolute decompression vent port 360 Pressure: 41 kPa, absolute pressure of the second decompression vent port 380: 41 kPa, absolute pressure of the third decompression vent port 390: 30 kPa, and absolute pressure of the fourth decompression vent port 400: 25 kPa (absolute of the first decompression vent port 360).
  • the water content of the water-containing crumb after passing through the dehydration zone 102 was 20% by weight.
  • the washing tank 7 and the extruder 1 wash the acrylic rubber slurry and dry the water-containing crumb of the acrylic rubber to continuously obtain solid acrylic rubber for two hours continuously.
  • venting up of each decompression vent port did not occur, and the obtained solid acrylic rubber also had a water content reduced to 0.4% by weight.
  • the Mooney viscosity (ML1 + 4, 100 ° C.) of the obtained solid acrylic rubber was 32.
  • Example 4 The acrylic rubber slurry obtained in Synthesis Example 1 was washed and dried using the washing tank 7 and the extruder 1 shown in FIG. 1 to obtain a solid acrylic rubber.
  • the supply rate of acrylic rubber to the cleaning tank 7 when cleaning is performed in the cleaning tank 7 is 500 kg / h (supply rate in terms of solid rubber content), and the cleaning water is supplied to the cleaning tank 7. Washing was performed at a rate of 12000 kg / h.
  • the acrylic rubber slurry after cleaning is passed through the water removal facility 8 (slit screen) from the cleaning tank 7 as a water content crumb (moisture content: 60% by weight) of the acrylic rubber (a mode in which water is accompanied by the water content crumb).
  • the supply rate of 1250 kg / h to the extruder 1 (supply rate in terms of acrylic rubber (that is, the amount of acrylic rubber to be dried Q). ) was supplied at 500 kg / h) and dried by the extruder 1. Further, the temperature of the water-containing crumb of acrylic rubber at the time of charging into the extruder 1 was set to 65 ° C. The temperature of the water-containing crumb of acrylic rubber when it was put into the extruder 1 was adjusted by adjusting the temperature of the washing water when washing in the washing tank 7.
  • the conditions for drying by the extruder 1 are the barrel temperature of the supply zone 100: 90 ° C., the barrel temperature of the dehydration zone 102: 140 ° C., and the barrel temperature of the drying zone 104: 170 ° C., and the absolute decompression vent port 360 Pressure: 65 kPa, absolute pressure of the second decompression vent port 380: 55 kPa, absolute pressure of the third decompression vent port 390: 40 kPa, and absolute pressure of the fourth decompression vent port 400: 35 kPa (absolute of the first decompression vent port 360).
  • the water content of the water-containing crumb after passing through the dehydration zone 102 was 40% by weight.
  • the washing tank 7 and the extruder 1 wash the acrylic rubber slurry and dry the water-containing crumb of the acrylic rubber to continuously obtain a solid acrylic rubber for 2 hours continuously.
  • venting up of each decompression vent port did not occur, and the obtained solid acrylic rubber also had a water content reduced to 0.4% by weight.
  • the Mooney viscosity (ML1 + 4, 100 ° C.) of the obtained solid acrylic rubber was 32.
  • each decompression vent port 360 when drying is performed by the extruder 1 The pressure of each decompression vent port 360 when drying is performed by the extruder 1, the absolute pressure of the first decompression vent port 360: 4 kPa, the absolute pressure of the second decompression vent port 380: 4 kPa, the absolute pressure of the third decompression vent port 390.

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Abstract

L'invention concerne un procédé de production d'un caoutchouc acrylique, le procédé comprenant une étape de séchage pour sécher le caoutchouc acrylique à l'aide d'une extrudeuse ayant une vis disposée à l'intérieur d'un cylindre d'une manière pouvant être entraînée en rotation. Une extrudeuse ayant une pluralité d'orifices d'évacuation à pression réduite est utilisée en tant qu'extrudeuse, et la pression absolue d'un orifice d'évacuation à pression réduite au niveau d'un côté amont dans la direction d'extrusion est réglée pour être supérieure à la pression absolue d'un orifice d'évacuation à pression réduite au niveau d'un côté aval dans la direction d'extrusion.
PCT/JP2020/023789 2019-06-18 2020-06-17 Procédé de production de caoutchouc acrylique WO2020256018A1 (fr)

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