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WO2006001113A1 - Appareil de polymérisation et procédé servant à produire un polymère - Google Patents

Appareil de polymérisation et procédé servant à produire un polymère Download PDF

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Publication number
WO2006001113A1
WO2006001113A1 PCT/JP2005/007588 JP2005007588W WO2006001113A1 WO 2006001113 A1 WO2006001113 A1 WO 2006001113A1 JP 2005007588 W JP2005007588 W JP 2005007588W WO 2006001113 A1 WO2006001113 A1 WO 2006001113A1
Authority
WO
WIPO (PCT)
Prior art keywords
polymerization
temperature
supply pipe
solution
kettle
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/JP2005/007588
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English (en)
Japanese (ja)
Inventor
Takuya Furukawa
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Mitsubishi Chemical Corp
Original Assignee
Mitsubishi Rayon Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Mitsubishi Rayon Co Ltd filed Critical Mitsubishi Rayon Co Ltd
Priority to JP2006528375A priority Critical patent/JP5249514B2/ja
Publication of WO2006001113A1 publication Critical patent/WO2006001113A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • 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
    • C08F2/00—Processes of polymerisation
    • C08F2/01—Processes of polymerisation characterised by special features of the polymerisation apparatus used
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0053—Details of the reactor
    • B01J19/0066—Stirrers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • B01J19/1806—Stationary reactors having moving elements inside resulting in a turbulent flow of the reactants, such as in centrifugal-type reactors, or having a high Reynolds-number
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00002—Chemical plants
    • B01J2219/00027—Process aspects
    • B01J2219/0004—Processes in series
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
    • B01J2219/00094—Jackets

Definitions

  • the present invention relates to a polymerization apparatus and a method for producing a polymer using the same.
  • a solution polymerization method is known as a method for obtaining a vinyl polymer by polymerizing a vinyl monomer.
  • a vinyl tank is prepared by heating a mixing tank that mixes a bull monomer, a solvent and a polymerization initiator, and a mixed liquid supplied from the mixing tank through a supply pipe. What comprises the superposition
  • the solution polymerization method includes a batch polymerization method in which a solvent, a vinyl monomer, and a polymerization initiator are mixed, heated, and superposed in a polymerization vessel, and a solvent is added to the polymerization vessel in advance, at a predetermined temperature.
  • a dropping type polymerization method in which a mixture of a vinyl monomer and a polymerization initiator is dropped from a mixing tank to a polymerization kettle and polymerization is performed.
  • the former is useful as a method for obtaining a relatively high polymer.
  • the latter can obtain a relatively low molecular weight copolymer, and the composition of the copolymer can be further improved by using a bull copolymer composed of a plurality of types of beer monomer units. It is useful as a uniform method.
  • solution polymerization is performed by the dropping polymerization method using the polymerization apparatus described above, the following problems may occur.
  • the vicinity of the outlet of the supply pipe is located inside the upper portion of the polymerization kettle, and is thus heated by the heat inside the polymerization kettle.
  • the vinyl monomer is supplied to the polymerization vessel in a state of being mixed with the polymerization initiator. For this reason, a part of the vinyl monomer is heated in a pipe near the outlet of the supply pipe to start polymerization, and a vinyl polymer is formed in the supply pipe to form a cullet, or a plurality of bulls.
  • a copolymer having a heterogeneous composition was often generated.
  • the vinyl polymer is an acrylic resin resin
  • a relatively low molecular weight polymer is required to reduce the amount of solvent, and for this reason, it is necessary to increase the concentration of the polymerization initiator! / For these reasons, the above two problems were likely to appear.
  • the bulle monomer and the polymerization initiator are supplied to the polymerization vessel through separate supply pipes, they are immediately diluted by the solvent that has been added to the polymerization vessel. It takes time for the monomer and the polymerization initiator to come into contact with each other in the polymerization kettle, and by that time, a part of the polymerization initiator is decomposed and disappears, and the polymerization initiator becomes useless. was there.
  • Patent Document 1 Japanese Patent Laid-Open No. 63-30334
  • Patent Document 2 JP 2002-167411 A
  • an object of the present invention is to provide a polymerization apparatus and an insoluble material in which a polymer is not generated and a polymerization initiator is not precipitated in a supply pipe provided between a mixing tank and a polymerization kettle. It is an object of the present invention to provide a method for producing a polymer that can stably produce a polymer solution free from contamination.
  • the polymerization apparatus of the present invention prepares a mixed liquid by mixing a monomer and a polymerization initiator.
  • a mixing tank that heats the mixed liquid to polymerize the monomer
  • a supply pipe that supplies the mixed liquid from the mixing tank to the polymerization tank
  • a temperature control that adjusts the temperature of the mixed liquid in the supply pipe It comprises the means.
  • the method for producing a polymer of the present invention includes supplying a mixed solution prepared by mixing a monomer and a polymerization initiator in a mixing tank to a polymerization vessel through a supply pipe.
  • the temperature of the mixed solution in the supply pipe is maintained in the range of 15 to 30 ° C.
  • the polymerization apparatus of the present invention it is possible to suppress the formation of a polymer or the precipitation of a polymerization initiator in a supply pipe provided between a mixing tank and a polymerization kettle.
  • a polymer solution can be stably produced without mixing insoluble matter.
  • the present invention can be suitably used particularly for the production of a resin for acrylic paints.
  • FIG. 1 is a schematic configuration diagram showing an example of a polymerization apparatus of the present invention.
  • FIG. 1 is a schematic configuration diagram showing an example of the polymerization apparatus of the present invention.
  • the polymerization apparatus 10 includes a mixing tank 12 that mixes and temporarily stores a monomer, a solvent, and a polymerization initiator, and a polymerization vessel 14 that performs polymerization of the monomer by heating the liquid mixture supplied from the mixing tank 12.
  • the polymerization initiator supply pipe 36 for supplying the polymerization initiator solution in the supply tank 16 to the polymerization tank 14, and the mixed solution supply pipe 32 are coaxially surrounded.
  • a water pipe 40 (temperature control means) provided in the water pipe 40, a water supply pipe 42 for supplying water to the water pipe 40, and a drain pipe 44 for discharging water from the water pipe 40 are schematically configured. .
  • the mixing tank 12 includes a tank body 60, a stirring blade 62 that stirs the liquid in the tank, a motor 64 that rotates the liquid, a manhole 65 that supplies a polymerization initiator, and a temperature inside the tank body 60. Temperature adjusting means 66 for adjusting.
  • the mixing tank 12 those used in a conventional solution polymerization apparatus can be used.
  • the superposition kettle 14 is composed of a kettle main body 70, a stirring blade 72 for stirring the liquid in the kettle, a motor 74 for rotating the kettle, a temperature adjusting means 76 for adjusting the temperature inside the kettle main body 70, and a superposition. And a filter 78 for filtering the polymer solution taken out from the kettle 14.
  • a polymerization vessel 14 those used in conventional solution polymerization apparatuses can be used.
  • the mixed liquid supply pipe 32 and the flowing water pipe 40 are double pipes, the inner pipe is the mixed liquid supply pipe 32, and the outer pipe is the flowing water pipe 40. Has been. By flowing water whose temperature is adjusted through the flowing water pipe 40, the temperature of the mixed liquid flowing through the mixed liquid supply pipe 32 can be adjusted to a predetermined temperature.
  • the flowing water pipe 40 surrounds the mixed liquid supply pipe 32 up to the outlet of the mixed liquid supply pipe 32 located inside the polymerization kettle 14, and the mixed liquid supply pipe 32 At the outlet, the end face of the water pipe 40 is sealed.
  • the end face of the double pipe formed of the mixed liquid supply pipe 32 and the flowing water pipe 40 is inclined with respect to the pipe axis as shown in FIG.
  • the inclination angle OC is preferably 30 to 60 °.
  • the position of the mixed solution supply pipe 32 in the polymerization vessel 14 is determined so that the properly mixed liquid is exposed above the liquid level 20 in the polymerization vessel 14 and the top of the polymerization vessel 14 and the stirring blade 72 are stirred.
  • a solvent is charged into the polymerization kettle 14, and the temperature inside the polymerization kettle 14 is heated to a predetermined temperature by the temperature control means 76.
  • the monomer and solvent are supplied to the mixing tank 12 from the raw material supply pipe 30 and the polymerization initiator is charged from the manhole 65.
  • the mixing tank 12 the monomer, solvent and polymerization initiator are sufficiently stirred and mixed, and the resulting liquid mixture is temporarily stored.
  • the mixed solution in the mixing tank 12 is dropped into the polymerization vessel 14 through the mixed solution supply pipe 32 at a predetermined dropping rate to perform solution polymerization.
  • a polymerization initiator is added from the supply tank 16 through the polymerization initiator supply pipe 36 as necessary.
  • the polymer solution is taken out from the bottom of the polymerization vessel 14 through the polymer solution take-out pipe 34 through the filtration process by the filter 78.
  • the amount and temperature of water supplied to the flowing water pipe 40 are the temperature of the liquid mixture in the liquid mixture supply pipe 32. Is controlled in the range of 15-30 ° C. Specifically, the amount of water supplied to the supply pipe is preferably 25 to 50 LZmin, and more preferably 30 to 40 LZmin. Further, the temperature of the supplied water is preferably 15 to 30 ° C, more preferably 18 to 25 ° C.
  • the mixed liquid flowing in the mixed liquid supply pipe 32 reaches the polymerization tank 14. There is a risk that the polymerization initiator will precipitate.
  • the temperature of the mixed solution in the mixed solution supply pipe 32 exceeds 30 ° C, monomer polymerization occurs, and cullet may be generated or a copolymer with a heterogeneous composition may be generated. is there.
  • the monomer in the case of producing a bull polymer, various bull monomers can be used.
  • acrylic resin various metatalates and / or acrylates and, if necessary, other vinyl polymers can be used in combination.
  • butyl monomer examples include methyl methacrylate, ethyl methacrylate, n-butyl methacrylate, i butyl methacrylate, t butyl methacrylate, amyl methacrylate, cyclohexyl methacrylate.
  • Methacrylic acid esters such as acrylate, 2-ethylhexyl methacrylate, stearyl methacrylate, dodecyl methacrylate, 2-hydroxyethyl methacrylate, glycidyl methacrylate; methyl acrylate, ethyl acrylate, n —Acrylic acid esters such as butyl phthalate, i-butyl acrylate, 2-ethyl hexyl acrylate, 2-hydroxyethyl acrylate, and 4-hydroxy acrylate; Burcyan compounds such as acrylonitrile and meta-talyl-tolyl; styrene, etc. An aromatic bur compound of Tali Le acid, and unsaturated carboxylic acids such as methacrylic acid.
  • Examples of the polymerization initiator for the bulle monomer include, for example, diisopropyl peroxy dicarbonate, di-t-hexyl silver oxide, t-butyl neodecanoate, t-butyl peroxypivalate, t-butyl peroxy.
  • 2-Ethylhexanoate pivare trauroyl peroxide, benzoyl peroxide, t-butylperoxypropyl carbonate, t-butylperoxybenzoate, dicumyl peroxide, di-t-butyl peroxide, 1, 1, t Organic peroxides such as butylperoxy 3, 3, 5 trimethylcyclohexane; 2, 2, azobis (2, 4 dimethylvale-tri ), 2, 2, -azobisisobutyronitrile, 2, 2, -azobis 2-methylbutyronitrile, l-azobis (1-cyclohexanecarbo-tolyl), 2, 2'-azobis (2 , 4, 4 trimethylpentane) and the like.
  • Examples of the solvent include aromatic hydrocarbons such as toluene and xylene; alcohol compounds such as isopropyl alcohol, 1-butanol and isobutanol; ester compounds such as ethyl acetate, n-butyl acetate and isobutyl acetate; ethylene glycol Examples include monoethyl ether, propylene glycol monomethyl ether; ketone compounds such as methyl ethyl ketone, methyl isobutyl ketone, and cyclohexanone; and aliphatic hydrocarbons such as n-xane and n-heptane.
  • aromatic hydrocarbons such as toluene and xylene
  • alcohol compounds such as isopropyl alcohol, 1-butanol and isobutanol
  • ester compounds such as ethyl acetate, n-butyl acetate and isobutyl acetate
  • ethylene glycol Examples include monoethy
  • the flowing water pipe 40 temperature control means
  • the temperature of the mixed liquid flowing through the mixed liquid supply pipe 32 is controlled. Further, the temperature can be adjusted to a temperature at which polymerization of the monomer occurs and precipitation of the polymerization initiator does not occur, and generation of the polymer in the tube and precipitation of the polymerization initiator can be suppressed.
  • the temperature of the mixed liquid in the mixed liquid supply pipe 32 is kept at 30 ° C or lower, so that the polymer in the pipe is Formation of the polymer solution with no insoluble matter mixed can be obtained.
  • the temperature of the mixed liquid in the mixed liquid supply pipe 32 is maintained at 15 ° C. or higher, precipitation of the polymerization initiator in the pipe is suppressed, and the polymer solution that does not interrupt the production can be stabilized. Can be manufactured.
  • the polymerization apparatus of the present invention is not limited to the illustrated example, and a temperature control means for adjusting the temperature of the mixed liquid in the supply pipe to the supply pipe for supplying the mixed liquid in the mixing tank to the polymerization kettle. Any form can be used as long as it is provided.
  • the resin for acrylic paints was produced under a temperature of 30 ° C.
  • the mixing tank 12 has a tank body 60 with a capacity of 4.5 m3, a stirring blade 62, a motor 6 The one with 4 was used.
  • the jacket temperature of the mixing tank was 25 ° C.
  • a kettle main body 70 having a capacity of 6 m3 and equipped with a stirring blade 72, a motor 74, a jacket (temperature control means 76), and a filter 78 was used as the polymerization kettle 14.
  • a supply tank 16 with a capacity of 0.5 m3 was used.
  • 230 kg of propylene glycol monomethyl ether, 230 kg of xylene, 345 kg of zinc methacrylate, 345 kg of zinc oleate, 207 kg of methyl methacrylate, 207 kg of methyl methacrylate, 1403 kg of ethyl acetate, t-butyl pertoate 92k g was charged, stirred and mixed to obtain a mixture.
  • the temperature of the mixture was 20 ° C.
  • the mixed liquid in the mixing tank 12 is fed into the polymerization kettle 14 in the amount of 11.9 kgZ.
  • the solution was dropped and solution polymerization was performed.
  • the temperature of the mixed liquid at the upstream side of 3 Ocm from the supply pipe outlet was 20 ° C, and the temperature of the mixed liquid at the supply pipe outlet was also 20 ° C. .
  • Example 2 Using the same polymerization apparatus 10 as in Example 1, the temperature of the resin for acrylic paints was 30 ° C. Manufactured.
  • the liquid mixture in the mixing tank 12 is fed into the polymerization kettle 14 by 11.6 kgZ.
  • the solution was dropped to perform solution polymerization. While dropping the mixed solution into the polymerization kettle, the temperature of the mixed solution at 30 cm upstream from the supply pipe outlet was 20 ° C, and the temperature of the mixed solution at the supply pipe outlet was also 20 ° C. It was.
  • Example 1 A polymerization apparatus similar to Example 1 was used under the same conditions as in Example 1 except that the flowing water pipe 40 was not provided as a polymerization apparatus. Was manufactured.
  • the temperature of the mixed solution in the mixing tank was 20 ° C. Also heavy While the mixed solution was dripping into the keg kettle, the temperature of the mixed solution at 30 cm upstream from the supply tube outlet was 20 ° C, but the temperature of the mixed solution at the supply tube outlet increased to 80 ° C. Was.
  • the mixed solution supply pipe 32 After observing the polymerization vessel 14 and the mixed solution supply pipe 32 after draining the resin solution, the mixed solution supply pipe 32 was not cooled, so that adhesion of the polymer was confirmed near the outlet of the mixed solution supply pipe 32. .
  • Example 2 As a polymerization apparatus, the same polymerization apparatus as in Example 1 was used except that the flowing water pipe 40 was not provided. Under the same conditions as in Example 2, the resin for acrylic paints was the same as in Example 2. Was manufactured. The temperature of the mixed solution in the mixing tank was 20 ° C. While the mixed solution was dripped into the superposition kettle, the temperature of the mixed solution 30 cm upstream from the supply tube outlet was 20 ° C, but the temperature of the mixed solution at the supply tube outlet was 60 °. It had risen to C.
  • the obtained rosin solution was slightly cloudy.
  • the liquid mixture in the mixing tank 12 is fed into the polymerization kettle 14 in an amount of 10. lkgZ. drop Solution polymerization was carried out. While the mixed liquid was dripped into the polymerization kettle, the temperature of the mixed liquid at the upstream side of 3 Ocm from the supply pipe outlet was 20 ° C, and the temperature of the mixed liquid at the supply pipe outlet was also 20 ° C. .
  • the mixed solution supply pipe 32 was warmed with 20 ° C water. The precipitation of '-azobis isopuchi-tolyl was not confirmed.
  • Example 3 As a polymerization apparatus, a polymerization apparatus similar to that in Example 3 was used except that the flowing water pipe 40 was not provided, and a resin for acrylic paint was used in the same manner as in Example 3 under the condition of a temperature of 5 ° C. Was manufactured.
  • the temperature of the mixed solution in the mixing tank was 20 ° C.
  • the temperature of the liquid mixture at the upstream of 30 cm from the outlet of the supply pipe was 20 ° C while the liquid mixture was being dropped into the polymerization kettle.
  • the temperature of the liquid mixture at the outlet of the supply pipe was 5 ° C. Met.
  • the liquid mixture supply pipe 32 since the liquid mixture supply pipe 32 was warmed with water at 20 ° C, the liquid mixture supply pipe 32 was clogged with precipitation of 2,2'-azobisisobuty-trill and polymerization was performed. I could't complete it.
  • the polymerization apparatus and the polymer production method of the present invention can suppress the insoluble matter from being mixed into the resulting polymer solution, the turbidity of the paint using the polymer solution as a raw material is eliminated, and the paint is obtained. When coating is applied, the occurrence of spot-like coating defects is suppressed.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Polymerisation Methods In General (AREA)
  • Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)

Abstract

Appareil de polymérisation, caractérisé en ce qu'il comprend une cuve de mélange dans laquelle on prépare un mélange liquide en mélangeant un monomère et un initiateur de polymérisation, un réacteur de polymérisation dans lequel on polymérise le monomère en chauffant le mélange liquide, un tuyau d'alimentation servant à introduire le mélange liquide provenant de la cuve de mélange dans le réacteur de polymérisation et des moyens de réguler la température servant à réguler la température du mélange liquide dans le tuyau d'alimentation. Un procédé servant à produire un polymère dans lequel on introduit un mélange liquide préparé en mélangeant un monomère et un initiateur de polymérisation dans une cuve de mélange dans un réacteur de polymérisation en passant par un tuyau d'alimentation et on polymérise le monomère en chauffant le mélange liquide dans le réacteur de polymérisation est caractérisé en ce qu'on maintient la température du mélange liquide dans le tuyau d'alimentation dans une plage de 15-30°C.
PCT/JP2005/007588 2004-06-25 2005-04-21 Appareil de polymérisation et procédé servant à produire un polymère Ceased WO2006001113A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP2006528375A JP5249514B2 (ja) 2004-06-25 2005-04-21 重合装置および重合体の製造方法

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2004188108 2004-06-25
JP2004-188108 2004-06-25

Publications (1)

Publication Number Publication Date
WO2006001113A1 true WO2006001113A1 (fr) 2006-01-05

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JP (2) JP5249514B2 (fr)
CN (2) CN100532397C (fr)
WO (1) WO2006001113A1 (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2008050461A (ja) * 2006-08-24 2008-03-06 Mitsubishi Rayon Co Ltd 重合体の製造方法、重合体およびレジスト組成物
JP2012246496A (ja) * 2012-08-24 2012-12-13 Mitsubishi Rayon Co Ltd 重合体の製造方法、およびレジスト組成物の製造方法
EP2772305A1 (fr) * 2013-02-27 2014-09-03 Uhde Inventa-Fischer GmbH Dispositif de polymérisation et procédé de fabrication de polymères thermoplastiques
JP2014196512A (ja) * 2014-07-14 2014-10-16 三菱レイヨン株式会社 重合体の製造方法、およびレジスト組成物の製造方法
JP2017155126A (ja) * 2016-03-01 2017-09-07 三菱ケミカル株式会社 水性分散体及びその製造方法
US10442824B2 (en) 2013-02-06 2019-10-15 Uhde Inventa-Fischer Gmbh Method for the production of a titanium containing catalyst, titanium containing catalyst, method for the production of polyester and polyester

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JP6443971B2 (ja) * 2014-09-30 2018-12-26 株式会社日本触媒 熱可塑性樹脂の製造方法
CN116289267A (zh) * 2022-09-08 2023-06-23 张彩玉 一种蛋白基纺织涂料印花粘合剂的制备方法

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JPH10306107A (ja) * 1997-03-04 1998-11-17 Mitsubishi Gas Chem Co Inc 重合体の製造方法
JP2000159816A (ja) * 1998-11-27 2000-06-13 Mitsubishi Rayon Co Ltd メタクリル系重合体の製造方法
JP2004018560A (ja) * 2002-06-12 2004-01-22 Nippon Shokubai Co Ltd （メタ）アクリル酸系重合体の製造方法および装置

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JPH10306107A (ja) * 1997-03-04 1998-11-17 Mitsubishi Gas Chem Co Inc 重合体の製造方法
JP2000159816A (ja) * 1998-11-27 2000-06-13 Mitsubishi Rayon Co Ltd メタクリル系重合体の製造方法
JP2004018560A (ja) * 2002-06-12 2004-01-22 Nippon Shokubai Co Ltd （メタ）アクリル酸系重合体の製造方法および装置

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2008050461A (ja) * 2006-08-24 2008-03-06 Mitsubishi Rayon Co Ltd 重合体の製造方法、重合体およびレジスト組成物
JP2012246496A (ja) * 2012-08-24 2012-12-13 Mitsubishi Rayon Co Ltd 重合体の製造方法、およびレジスト組成物の製造方法
US10442824B2 (en) 2013-02-06 2019-10-15 Uhde Inventa-Fischer Gmbh Method for the production of a titanium containing catalyst, titanium containing catalyst, method for the production of polyester and polyester
EP2772305A1 (fr) * 2013-02-27 2014-09-03 Uhde Inventa-Fischer GmbH Dispositif de polymérisation et procédé de fabrication de polymères thermoplastiques
WO2014131736A1 (fr) * 2013-02-27 2014-09-04 Uhde Inventa-Fischer Gmbh Dispositif de polymérisation et procédé de production de polymères thermoplastiques
US9943824B2 (en) 2013-02-27 2018-04-17 Uhde Inventa-Fisher GmbH Polymerisation device and method for the production of thermoplastic polymers
JP2014196512A (ja) * 2014-07-14 2014-10-16 三菱レイヨン株式会社 重合体の製造方法、およびレジスト組成物の製造方法
JP2017155126A (ja) * 2016-03-01 2017-09-07 三菱ケミカル株式会社 水性分散体及びその製造方法

Also Published As

Publication number Publication date
JPWO2006001113A1 (ja) 2008-04-17
CN101481430A (zh) 2009-07-15
CN100532397C (zh) 2009-08-26
CN101006102A (zh) 2007-07-25
JP2013100560A (ja) 2013-05-23
JP5249514B2 (ja) 2013-07-31
CN101481430B (zh) 2011-05-04
JP5590425B2 (ja) 2014-09-17

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