WO2011016364A1 - カルボキシル基含有水溶性重合体の製造方法 - Google Patents
カルボキシル基含有水溶性重合体の製造方法 Download PDFInfo
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- WO2011016364A1 WO2011016364A1 PCT/JP2010/062579 JP2010062579W WO2011016364A1 WO 2011016364 A1 WO2011016364 A1 WO 2011016364A1 JP 2010062579 W JP2010062579 W JP 2010062579W WO 2011016364 A1 WO2011016364 A1 WO 2011016364A1
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- 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
- C08F20/04—Acids, Metal salts or ammonium salts thereof
- C08F20/06—Acrylic acid; Methacrylic acid; Metal salts or ammonium salts thereof
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- 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
- C08F120/00—Homopolymers 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
- C08F120/02—Monocarboxylic acids having less than ten carbon atoms; Derivatives thereof
- C08F120/04—Acids; Metal salts or ammonium salts thereof
- C08F120/06—Acrylic acid; Methacrylic acid; Metal salts or ammonium salts thereof
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- 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
- C08F2/04—Polymerisation in solution
- C08F2/06—Organic solvent
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- 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
- C08F20/62—Monocarboxylic acids having ten or more carbon atoms; Derivatives thereof
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- 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
- C08F6/06—Treatment of polymer solutions
- C08F6/10—Removal of volatile materials, e.g. solvents
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- 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
- C08F220/00—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
- C08F220/02—Monocarboxylic acids having less than ten carbon atoms; Derivatives thereof
- C08F220/04—Acids; Metal salts or ammonium salts thereof
- C08F220/06—Acrylic acid; Methacrylic acid; Metal salts or ammonium salts thereof
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- 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
- C08F2400/00—Characteristics for processes of polymerization
Definitions
- the present invention relates to a method for producing a carboxyl group-containing water-soluble polymer, and in particular, to produce a carboxyl group-containing water-soluble polymer by reacting a monomer component containing an ⁇ , ⁇ -unsaturated carboxylic acid in an inert solvent. On how to do.
- the carboxyl group-containing water-soluble polymer usually dissolves a monomer component containing an ⁇ , ⁇ -unsaturated carboxylic acid and a polymerizable compound having two or more ethylenically unsaturated groups used as necessary. It is produced by precipitation polymerization in an inert solvent that does not dissolve the carboxyl group-containing water-soluble polymer produced by polymerization of the monomer component.
- Precipitation polymerization refers to a polymerization method in which a polymer produced by a polymerization reaction is precipitated in a solvent by using an inert solvent as described above. In this polymerization method, a powdery carboxyl group-containing water-soluble polymer is used. A polymer can be obtained.
- Patent Documents 6 and 7 add a monomer component to a reaction solution in which a specific amount of the monomer component remains unreacted. The method of adding to and reacting is described. Further, Patent Document 8 (particularly, claims and paragraph 0032) describes a method of adding a monomer component in about 2 to 8 times with respect to an inert solvent and a continuous addition of the monomer component. Describes a method of adding in small portions.
- the method of adding monomer components additionally or in divided additions is practical because the effect of suppressing the increase in the viscosity of the reaction solution slurry is insufficient despite the complicated management and operation.
- the resulting carboxyl group-containing water-soluble polymer tends to be light and have a low bulk specific gravity.
- the method of continuously adding the monomer component lacks practicality because, as described in Patent Document 8, the optimization range of the reaction conditions such as the polymerization temperature is narrow and difficult to manage.
- An object of the present invention is to improve the practical efficiency and improve the production efficiency in the production of a carboxyl group-containing water-soluble polymer by precipitation polymerization.
- the inventor of the present invention focused on a method of carrying out a polymerization reaction while continuously adding an inert solvent solution of a monomer component to an inert solvent in the production of a carboxyl group-containing water-soluble polymer by precipitation polymerization.
- the monomer component concentration in the inert solvent solution, the monomer component concentration relative to the total amount of the inert solvent used, and the monomer component in the polymerization reaction system after the addition of the total amount of the inert solvent solution is completed. It was found that when the polymerization rate was controlled, an increase in viscosity of the reaction slurry could be easily suppressed, and the production efficiency of the carboxyl group-containing water-soluble polymer was increased.
- the present invention relates to a process for producing a carboxyl group-containing water-soluble polymer by reacting a monomer component containing an ⁇ , ⁇ -unsaturated carboxylic acid in an inert solvent.
- This method includes a step A in which a reaction vessel charged with an inert solvent is prepared, and a simple substance in which a monomer component is dissolved in an inert solvent at a concentration of 20 to 50% by volume with respect to the inert solvent charged in the reaction vessel. And a step B of continuously adding the monomer solution.
- the amount of the inert solvent charged into the reaction vessel in the step A is set so that the concentration of the monomer component in the total amount with the monomer solution is 10 to 24% by volume.
- the time required to complete the continuous addition of the entire amount of the monomer solution is set so that the polymerization rate of the monomer component is 60% or more when the addition of the entire amount of the monomer solution is completed.
- This production method involves precipitation polymerization while continuously adding an inert solvent solution of a predetermined monomer component to an inert solvent, and the concentration of the monomer component in the inert solvent solution and the inert solvent used. Controlling the monomer component concentration relative to the total amount and the polymerization rate of the monomer component in the polymerization reaction system after completion of the addition of the entire amount of the inert solvent solution can easily suppress the increase in viscosity of the reaction slurry. The production efficiency of the carboxyl group-containing water-soluble polymer can be increased.
- the production method of the present invention usually further includes a step C in which the reaction is continued after completion of continuous addition of the entire amount of the monomer solution.
- the production method of the present invention usually further includes a step D in which the inert solvent is volatilized and removed from the reaction solution after completion of the reaction in the step C.
- the ⁇ , ⁇ -unsaturated carboxylic acids used in the production method of the present invention include, for example, acrylic acid, methacrylic acid, esters of acrylic acid and higher alcohols having 10 to 30 carbon atoms in the alkyl group, and methacrylic acid and alkyl groups. Is at least one selected from the group consisting of esters with higher alcohols having 10 to 30 carbon atoms.
- the monomer component may further contain, for example, a polymerizable compound having two or more ethylenically unsaturated groups.
- the polymerizable compound having two or more ethylenically unsaturated groups is, for example, at least one selected from the group consisting of pentaerythritol allyl ether, polyallyl saccharose, diethylene glycol diallyl ether, and polyethylene glycol diallyl ether.
- the inert solvent charged in the reaction solution used in the production method of the present invention and the inert solvent in which the monomer component is dissolved in the monomer solution are usually the same.
- a monomer component containing an ⁇ , ⁇ -unsaturated carboxylic acid is polymerized in an inert solvent.
- the ⁇ , ⁇ -unsaturated carboxylic acids used here are not particularly limited, and for example, ⁇ , ⁇ -unsaturated such as acrylic acid, methacrylic acid, crotonic acid, maleic acid, itaconic acid and fumaric acid are used. Mention may be made of carboxylic acids, alkyl acrylates and alkyl methacrylates. These ⁇ , ⁇ -unsaturated carboxylic acids may be used alone or in combination of two or more.
- the acrylic acid alkyl ester and methacrylic acid alkyl ester refer to alkyl esters of acrylic acid and methacrylic acid with an alkyl alcohol, preferably a higher alkyl alcohol having 10 to 30 carbon atoms in the alkyl group, respectively.
- alkyl alcohol preferably a higher alkyl alcohol having 10 to 30 carbon atoms in the alkyl group, respectively.
- the higher alcohol having 10 to 30 carbon atoms of the alkyl group forming the alkyl ester include decanol, lauryl alcohol, myristyl alcohol, cetyl alcohol, stearyl alcohol, eicosanol, behenyl alcohol, and tetracosanol.
- alkyl ester since this alkyl ester is inexpensive and easily available, those having an alkyl group having 18 to 24 carbon atoms such as stearyl acrylate, stearyl methacrylate, eicosanyl acrylate, eicosanyl methacrylate, behenyl acrylate. , Behenyl methacrylate, tetracosanyl acrylate and tetracosanyl methacrylate and mixtures thereof are preferably used.
- alkyl esters of acrylic acid or methacrylic acid can be appropriately prepared and used, but commercially available products can also be used.
- a mixture of stearyl methacrylate, eicosanyl methacrylate, behenyl methacrylate and tetracosanyl methacrylate is commercially available from Nippon Oil & Fat Co., Ltd. under the trade name “Blemmer VMA70”.
- esters of higher alcohols having 10 to 30 carbon atoms in the alkyl group particularly esters of acrylic acid and higher alcohols having 12 to 24 carbon atoms in the alkyl group
- methacrylic acid and alkyl groups having 10 carbon atoms in the alkyl group are particularly preferred.
- esters with higher alcohols of ⁇ 30 especially esters of methacrylic acid and higher alcohols having 12 to 24 carbon atoms in the alkyl group).
- acrylic acid and the above methacrylic acid alkyl ester are used as ⁇ , ⁇ -unsaturated carboxylic acids. It is particularly preferable to use them in combination.
- the monomer component may further contain a polymerizable compound having two or more ethylenically unsaturated groups.
- the carboxyl group-containing water-soluble polymer obtained by using this monomer component can function as a thickener when added to water or various aqueous solutions.
- the polymerizable compound having two or more ethylenically unsaturated groups used here is not particularly limited, but usually a compound having an allyl group as an ethylenically unsaturated group is preferable, for example, pentaerythritol allyl ether. And diethylene glycol diallyl ether, polyethylene glycol diallyl ether and polyallyl saccharose.
- the compounds having two or more ethylenically unsaturated groups may be used alone or in combination of two or more.
- the amount of the compound having two or more ethylenically unsaturated groups is usually preferably set to 2 parts by weight or less with respect to 100 parts by weight of the ⁇ , ⁇ -unsaturated carboxylic acids. More preferably, it is set to 5 parts by weight or less.
- the amount of the compound having two or more ethylenically unsaturated groups is more than 2 parts by weight, a water-insoluble polymer may be easily mixed into the resulting carboxyl group-containing water-soluble polymer.
- the inert solvent used for the polymerization reaction of the monomer component is one that dissolves the monomer component but does not dissolve the resulting carboxyl group-containing water-soluble polymer, and the polymerization reaction of the monomer component As long as they do not interfere with the above, various types can be used. Specific examples include aliphatic hydrocarbon solvents such as normal pentane, normal hexane, normal heptane, cyclopentane and cyclohexane, aromatic hydrocarbon solvents such as benzene and toluene, and halogenated solvents such as 1,2-dichloroethane and methylene chloride. And ester solvents such as ethyl acetate and butyl acetate. These inert solvents may be used alone or in combination of two or more.
- a reaction vessel charged with an inert solvent is prepared (step A).
- a radical polymerization initiator is usually added to the inert solvent.
- the radical polymerization initiator include various known ones such as ⁇ , ⁇ ′-azobisisobutyronitrile, 2,2′-azobis-2,4-dimethylvaleronitrile, and 2,2′-azobismethyl. Isobutyrate or the like can be used.
- the amount of radical polymerization initiator used is preferably set to 0.0001 to 0.0015 mol per 1 mol of ⁇ , ⁇ -unsaturated carboxylic acids contained in the monomer component.
- the amount is less than 0.0001 mol, the reaction rate becomes slow, and the resulting carboxyl group-containing water-soluble polymer tends to be lightened and the bulk specific gravity tends to decrease.
- the amount of the polymerization initiator used exceeds 0.0015 mol, the polymerization proceeds rapidly and it may be difficult to control the reaction.
- the monomer component solution is gradually and continuously added to the inert solvent charged in the reaction vessel (step B).
- the solution of the monomer component continuously added (hereinafter sometimes referred to as monomer solution) is obtained by dissolving the monomer component in an inert solvent.
- the inert solvent used in the monomer solution is the same as that charged in the reaction vessel in Step A, and usually the same inert solvent charged in the reaction vessel is used. Different ones may be used as long as they have solubility.
- the concentration of the monomer component in the monomer solution is set to 20 to 50% by volume. However, the concentration is more preferably set to 24 to 45% by volume, and further preferably set to 28 to 40% by volume.
- concentration of the monomer component is less than 20% by volume, during the polymerization of the monomer component, the viscosity of the reaction solution slurry tends to be high and it becomes difficult to control the reaction heat. It may cause bumping.
- the resulting carboxyl group-containing water-soluble polymer tends to aggregate and agglomerate, it tends to adhere to the inner wall of the reaction vessel and the stirring blade, making it difficult to obtain a powdery product or containing a carboxyl group
- the physical properties of the water-soluble polymer may be adversely affected.
- the concentration of the monomer component exceeds 50% by volume, in addition to the possibility of causing the same problems as when the concentration is less than 20% by volume, the resulting carboxyl group-containing water-soluble polymer There is a possibility that a water-insoluble polymer (a highly crosslinked product of a carboxyl group-containing polymer) is formed as a by-product.
- the water-insoluble polymer is usually obtained by dispersing the produced carboxyl group-containing water-soluble polymer in ion-exchanged water and leaving it to stand still for a whole day and night, followed by suction filtration with a mesh having an opening of 50 microns. Isolated as dandruff white particles.
- the reaction temperature is 50 to 95 ° C., preferably 65 to 90 ° C. by stirring the contents of the reaction vessel and appropriately heating or cooling the reaction vessel. It is preferable to set to.
- the inert solvent in the reaction vessel may be a room temperature of about 20 to 30 ° C., or may be heated to the vicinity of the reaction temperature.
- reaction temperature When the reaction temperature is lower than 50 ° C., the reaction solution slurry viscosity increases, and it may become difficult to uniformly stir the reaction system. Conversely, when the reaction temperature exceeds 90 ° C., the resulting carboxyl group-containing water-soluble polymer tends to aggregate and agglomerate, so it tends to adhere to the inner wall of the reaction vessel and the stirring blade, and is in powder form. It tends to be difficult to obtain as.
- the continuous addition of the monomer solution to the inert solvent in the reaction vessel can be carried out by various methods as long as the monomer solution can be divided infinitely and added in small portions at a substantially constant rate.
- an addition apparatus it is usually preferable to use an addition apparatus because the time for continuous addition is set to a relatively long time as described later.
- a tube pump or the like can be used for small-scale production, and a slurry pump or the like can be used for industrial-scale production.
- the manufacturing method of the present invention is set so as to satisfy the following conditions in the above-described step A and step B.
- the amount of the inert solvent charged into the reaction vessel in the step A is such that the concentration of the monomer component in the total amount of the monomer solution continuously added in the step B is 10 to 24% by volume, preferably 12 to 22% by volume. %, More preferably 14 to 20% by volume.
- this concentration is less than 10% by volume, the production amount per batch decreases, which may be uneconomical.
- it exceeds 24% by volume the viscosity of the reaction solution slurry becomes high and it becomes difficult to control the reaction heat, which may lead to bumping of the reaction solution.
- the generated carboxyl group-containing water-soluble polymer tends to aggregate and agglomerate, it tends to adhere to the inner wall of the reaction vessel and the stirring blade, making it difficult to obtain a powdery product,
- the physical properties of the conductive polymer may be adversely affected.
- Step B The time until the continuous addition of the entire amount of the monomer solution is completed in Step B is set so that the polymerization rate of the monomer component is 60% or more when the addition of the entire amount of the monomer solution is completed. This time varies depending on various factors such as the composition of the monomer solution, the amount of radical polymerization initiator used, and the reaction temperature, so it is not constant, but usually it takes longer to complete the continuous addition. Then, the said polymerization rate can be achieved. In addition, the polymerization rate of a monomer component is calculated
- the amount of the unreacted monomer component means the amount of the unreacted ⁇ , ⁇ -unsaturated carboxylic acid. In the formula, each amount of the monomer component is based on weight.
- the polymerization rate can be confirmed by a method using liquid chromatography such as high performance liquid chromatography.
- the polymerization rate of the monomer component is less than 60% at the completion of addition of the entire amount of the monomer solution, the viscosity of the reaction solution slurry increases during the subsequent polymerization of the monomer component, and the reaction heat is controlled. Since it becomes difficult to do so, there is a possibility that bumping of the reaction solution may occur. In addition, since the generated carboxyl group-containing water-soluble polymer tends to aggregate and agglomerate, it tends to adhere to the inner wall of the reaction vessel and the stirring blade, making it difficult to obtain a powdery product, The physical properties of the conductive polymer may be adversely affected.
- the time from the start to the completion of the continuous addition of the monomer solution needs to be set so as to achieve Condition 2, but it is usually preferably set to 60 to 360 minutes.
- this time is short (that is, when the addition rate of the monomer solution is fast)
- the reaction is inhibited until the concentration of the monomer component reaches a certain level or more due to the dilution effect of the reaction solution by the added monomer solution.
- the reaction does not proceed easily, but the reaction starts abruptly when the monomer component concentration exceeds a certain level, making it difficult to control the reaction by removing heat from the reaction system. ,It is a danger.
- generated carboxyl group-containing water-soluble polymer tends to become light and the bulk specific gravity described later tends to be small.
- this time is too long, the productivity of the carboxyl group-containing water-soluble polymer is lowered, which is uneconomical.
- the reaction time varies depending on various factors such as the reaction temperature, the amount of radical polymerization initiator used, and the 10-hour half-life temperature of the radical polymerization initiator, but it is usually preferably set to 1 to 8 hours.
- the reaction solution is heated to volatilize and remove the inert solvent (step D). Thereby, a fine powdery carboxyl group-containing water-soluble polymer is obtained.
- the heating temperature of the reaction solution is too high, the solubility of the carboxyl group-containing water-soluble polymer in water may be impaired.
- the heating temperature of the reaction solution for removing the inert solvent is usually preferably set in the range of 80 ° C. or higher and 120 ° C. or lower.
- the polymerization reaction rate of the monomer component and the addition rate of the monomer solution are maintained, and as a result Since the slurry concentration (monomer component concentration) of the reaction system can be increased while suppressing an increase in the viscosity of the reaction solution slurry, it is easy to control the reaction, particularly the reaction temperature, and is highly practical. It is possible to produce a carboxyl group-containing water-soluble polymer safely while increasing the production efficiency per unit.
- the carboxyl group-containing water-soluble polymer produced by the production method of the present invention hardly adheres to the inner wall of the reaction vessel or the stirring blade as an aggregate, and easily precipitates as stable fine particles in the reaction solution.
- the carboxyl group-containing water-soluble polymer produced by the production method of the present invention has a bulk specific gravity of 0.20 g / ml or more and a range of 0.27 g / ml or less where solubility in water is hardly impaired.
- the bulk specific gravity obtained by the conventional precipitation polymerization method is different from the light one having a bulk density of less than 0.20 g / ml. For this reason, this carboxyl group-containing water-soluble polymer can reduce the cost required for transportation and the space required for storage.
- a part of the monomer component may be dissolved in advance in the inert solvent charged into the reaction vessel in Step A.
- the amount of the monomer component dissolved in advance is preferably set to less than 50% by weight of the total amount of monomer components used for the production of the carboxyl group-containing water-soluble polymer, and is set to less than 30% by weight. Is more preferable. When this amount is 50% by weight or more, the viscosity of the reaction solution slurry becomes too high, and it becomes difficult to sufficiently stir the reaction solution, which may cause bumping due to partial overheating of the reaction solution.
- Example 1 A reaction vessel consisting of a 500 mL round separable flask (ball diameter 110 mm) equipped with a stirrer, thermometer, nitrogen blowing tube, addition device and cooling tube was prepared.
- the stirrer used here is equipped with a four-paddle type stirring blade (blade diameter 75 mm, blade width 14 mm, pitch degree 45 degrees), and this stirring blade is arranged 5 mm above the bottom of the separable flask. It is.
- the reaction vessel was charged with 207.1 g (165.7 ml) of 1,2-dichloroethane and 0.042 g (0.00026 mol) of 2,2′-azobismethylisobutyrate, and 70 g (0 Monomer solution consisting of 0.63 g (0.66 ml) of pentaerythritol allyl ether and 148.1 g (118.5 ml) of 1,2-dichloroethane (.97 mol, 66.7 ml) Monomer component concentration: 36% by volume) was charged. The concentration of the monomer component in the total amount of solvent and monomer solution charged in the reaction vessel is 19% by volume.
- the stirring of the contents of the reaction container was started, and nitrogen gas was blown into the contents in order to remove oxygen present in the contents of the reaction container and in the upper space. And it heated in the state which maintained the inside of reaction container in nitrogen atmosphere, and the monomer solution was continuously added from the addition apparatus over 110 minutes, when the content of reaction container reached
- the rotational speed of the stirrer was accelerated from the initial 200 rpm by 50 rpm until the reaction solution slurry whose viscosity gradually increased could be uniformly stirred. After the addition of the monomer solution was completed, the reaction was continued (ripened) for an additional hour while maintaining the temperature at 75 ° C.
- the polymerization rate of the monomer component at the completion of the addition of the monomer solution was 75%.
- Example 2 A reaction vessel similar to that used in Example 1 was prepared, and a mixed solvent of 107.9 g (158.7 ml) of normal heptane and 35.7 g (39.7 ml) of ethyl acetate and 2,2′-azo 0.036 g (0.00015 mol) of bismethylisobutyrate was charged.
- a monomer component composed of 60 g of acrylic acid (0.83 mol, 57.1 ml) and 0.33 g (0.35 ml) of pentaerythritol allyl ether was added to 55.3 g (81.3 ml) of normal heptane.
- the stirring of the contents of the reaction container was started, and nitrogen gas was blown into the contents in order to remove oxygen present in the contents of the reaction container and in the upper space. Then, the reaction vessel was heated while being maintained in a nitrogen atmosphere, and the monomer solution was continuously added from the addition apparatus over 180 minutes from when the contents of the reaction vessel reached 70 ° C. At this time, the reaction temperature was controlled to gradually rise to 75 ° C.
- the rotational speed of the stirrer was accelerated from the initial 200 rpm by 50 rpm until the reaction solution slurry whose viscosity gradually increased could be uniformly stirred.
- the reaction was continued (ripened) for 1 hour while maintaining at 75 ° C.
- the polymerization rate of the monomer component at the completion of the addition of the monomer solution was 78%.
- the resulting slurry was transferred to another container and heated to 110 ° C. to distill off normal heptane and ethyl acetate. As a result, 57 g of a white fine powdery alkyl-modified carboxyl group-containing water-soluble polymer was obtained. .
- Example 3 A reaction vessel similar to that used in Example 1 was prepared, and a mixed solvent of 107.9 g (158.7 ml) of normal heptane and 35.7 g (39.7 ml) of ethyl acetate and 2,2′-azo 0.036 g (0.00015 mol) of bismethylisobutyrate was charged.
- a monomer component consisting of 60 g of acrylic acid (0.83 mol, 57.1 ml) and 0.33 g (0.35 ml) of pentaerythritol allyl ether was added to 55.3 g (81.3 ml) of normal heptane.
- the stirring of the contents of the reaction container was started, and nitrogen gas was blown into the contents in order to remove oxygen present in the contents of the reaction container and in the upper space. Then, the reaction vessel was maintained in a nitrogen atmosphere, and the monomer solution was continuously added from the addition apparatus over 300 minutes. At this time, the addition of the monomer solution was started when the temperature of the contents of the reaction vessel was normal temperature (25 ° C.), and the reaction temperature was controlled to gradually increase to 75 ° C. During the addition of the monomer solution, the rotational speed of the stirrer was accelerated from the initial 200 rpm by 50 rpm until the reaction solution slurry whose viscosity gradually increased could be uniformly stirred. After completion of the addition of the monomer solution, the reaction was continued (ripened) for 1 hour while maintaining at 75 ° C. The polymerization rate of the monomer component at the completion of the addition of the monomer solution was 78%.
- the resulting slurry was transferred to another container and heated to 110 ° C. to distill off normal heptane and ethyl acetate. As a result, 57 g of a white fine powdery alkyl-modified carboxyl group-containing water-soluble polymer was obtained. .
- Example 4 In Example 2, a reaction vessel was mixed with a mixed solvent of 54.9 g (80.7 ml) of normal heptane and 18.2 g (20.2 ml) of ethyl acetate and 0.036 g of 0,2′-azobismethylisobutyrate (0 The monomer component consisting of 60 g (0.83 mol, 57.1 ml) of acrylic acid and 0.30 g (0.32 ml) of pentaerythritol allyl ether was added to normal heptane.
- a monomer solution (concentration of monomer component: 36% by volume) dissolved in a mixed solvent of 55.3 g (81.3 ml) and ethyl acetate 18.3 g (20.3 ml) was charged (into the reaction vessel).
- the concentration of the monomer component in the total amount of the charged solvent and the monomer solution was 22% by volume, except that the white fine powdery alkyl was obtained.
- 57 g of a modified carboxyl group-containing water-soluble polymer was obtained.
- the polymerization rate of the monomer component at the completion of the addition of the monomer solution was 81%.
- Example 5 A reaction vessel similar to that used in Example 1 was prepared, and a monomer composed of acrylic acid 24 g (0.33 mol, 22.9 ml) and pentaerythritol allyl ether 0.10 g (0.11 ml) was prepared. Components, a mixed solvent of 111.4 g (163.8 ml) of normal heptane and 36.8 g (40.9 ml) of ethyl acetate and 0.036 g (0.00015 mol) of 2,2′-azobismethylisobutyrate were charged. It is.
- a monomer component consisting of 36 g of acrylic acid (0.50 mol, 34.3 ml) and 0.23 g (0.24 ml) of pentaerythritol allyl ether was added to 51.8 g (76.2 ml) of normal heptane. ) And 17.2 g (19.1 ml) of ethyl acetate were charged with a monomer solution (monomer component concentration: 36% by volume). The concentration of the monomer component in the total amount of the solvent and the monomer component and the monomer solution charged in the reaction vessel is 16% by volume.
- the stirring of the contents of the reaction container was started, and nitrogen gas was blown into the contents in order to remove oxygen present in the contents of the reaction container and in the upper space. Then, the reaction vessel was heated while being maintained in a nitrogen atmosphere, and the monomer solution was continuously added from the addition apparatus over 150 minutes from when the contents of the reaction vessel reached 60 ° C. At this time, the reaction temperature was controlled to gradually rise to 75 ° C.
- the rotational speed of the stirrer was accelerated from the initial 200 rpm by 50 rpm until the reaction solution slurry whose viscosity gradually increased could be uniformly stirred.
- the reaction was continued (ripened) for 1 hour while maintaining at 75 ° C.
- the polymerization rate of the monomer component at the completion of the addition of the monomer solution was 82%.
- the resulting slurry was transferred to another container and heated to 110 ° C. to distill off normal heptane and ethyl acetate. As a result, 57 g of a white fine powdery alkyl-modified carboxyl group-containing water-soluble polymer was obtained. .
- Example 6 When the same operation as in Example 2 was carried out except that the continuous addition time of the monomer solution was changed to 120 minutes, 57 g of a white fine powdery alkyl-modified carboxyl group-containing water-soluble polymer was obtained. The polymerization rate of the monomer component at the completion of the addition of the monomer solution was 62%.
- Example 7 In a reaction vessel, a mixed solvent of 64.8 g (95.3 ml) of normal heptane and 21.4 g (23.8 ml) of ethyl acetate and 0.036 g (0.00015 mol) of 2,2′-azobismethylisobutyrate were added.
- the monomer component consisting of 60 g (0.83 mol, 57.1 ml) of acrylic acid and 0.33 g (0.35 ml) of pentaerythritol allyl ether and 98.4 g of normal heptane (144) 0.7 ml) and a monomer solution (concentration of monomer component: 24% by volume) dissolved in a mixed solvent of ethyl acetate 32.6 g (36.2 ml) (solvent and single amount charged in the reaction vessel) (The concentration of the monomer component in the total amount with the body solution is 16% by volume). 57 g of a group-containing water-soluble polymer was obtained. The polymerization rate of the monomer component at the completion of the addition of the monomer solution was 75%.
- Example 8 A monomer component consisting of 60 g of acrylic acid (0.83 mol, 57.1 ml), 2.4 g (0.009 mol) of lauryl methacrylate and 0.33 g (0.35 ml) of pentaerythritol allyl ether was added to the addition apparatus as normal. A monomer solution (concentration of monomer component: 37% by volume) dissolved in a mixed solvent of 55.3 g (81.3 ml) of heptane and 18.3 g (20.3 ml) of ethyl acetate was charged (into the reaction vessel).
- Example 2 In the same manner as in Example 2 except that the concentration of the monomer component in the total amount of the charged solvent and the monomer solution is 17% by volume, it contains an alkyl-modified carboxyl group in the form of a white fine powder. 57 g of a water-soluble polymer was obtained. The polymerization rate of the monomer component at the completion of the addition of the monomer solution was 81%.
- Example 9 A monomer component consisting of 60 g of acrylic acid (0.83 mol, 57.1 ml) and stearyl methacrylate 3.0 g (0.009 mol, 3.3 ml) was added to the addition apparatus 55.3 g (81.3 ml) of normal heptane. ) And 18.3 g (20.3 ml) of ethyl acetate dissolved in a mixed solvent (monomer component concentration: 37 vol%) (solvent and monomer solution charged in reaction vessel) The concentration of the monomer component in the total amount is 17 vol%, and the same operation as in Example 2 was performed, except that 61 g of a white fine powdery alkyl-modified carboxyl group-containing water-soluble polymer was obtained. It was. The polymerization rate of the monomer component at the completion of the addition of the monomer solution was 83%.
- Comparative Example 1 A reaction vessel consisting of a 500 ml round separable flask (ball diameter 110 mm) equipped with a stirrer, thermometer, nitrogen blowing tube and cooling tube was prepared.
- the stirrer used here is the same as that used in Example 1.
- acrylic acid (monomer component) 45 g (0.63 mol, 42.9 ml)
- 1,2-dichloroethane 392.9 g (314.3 ml)
- pentaerythritol allyl ether 0.36 g (0.38 ml)
- 0.095 g (0.00004 mol) of 2,2′-azobismethylisobutyrate was charged (monomer component concentration: 12% by volume).
- stirring of the contents of the reaction container was started, and nitrogen gas was blown into the contents in order to remove oxygen present in the contents of the reaction container and in the upper space.
- reaction vessel was heated in a nitrogen atmosphere, and kept at 75 ° C. for 200 minutes.
- the rotating speed of the stirrer was accelerated from the initial 200 rpm by 50 rpm until the reaction liquid slurry whose viscosity gradually increased could be uniformly stirred.
- 0.05 g (0.00022 mol) of 2,2'-azobismethylisobutyrate was further added, and the reaction was continued (ripened) for an additional hour while maintaining at 75 ° C.
- Comparative Example 2 A reaction vessel similar to that used in Comparative Example 1 was prepared, and 45 g (0.63 mol, 42.9 ml) of acrylic acid (monomer component) and 0.27 g (0.28 ml) of pentaerythritol allyl ether were added thereto. A mixed solvent of 160.3 g (235.7 ml) of normal heptane and 70.7 g (78.6 ml) of ethyl acetate and 0.081 g (0.0035 mol) of 2,2′-azobismethylisobutyrate were charged. (Monomer component concentration: 12% by volume). Then, stirring of the contents of the reaction container was started, and nitrogen gas was blown into the contents in order to remove oxygen present in the contents of the reaction container and in the upper space.
- reaction vessel was heated in a nitrogen atmosphere, and kept at 75 ° C. for 200 minutes.
- the rotating speed of the stirrer was accelerated from the initial 200 rpm by 50 rpm until the reaction liquid slurry whose viscosity gradually increased could be uniformly stirred. Thereafter, the reaction was continued (ripening) for an additional hour while maintaining the temperature at 75 ° C.
- a monomer component consisting of 60 g (0.83 mol, 57.1 ml) of acrylic acid and 0.30 g (0.32 ml) of pentaerythritol allyl ether and 55.3 g of normal heptane (81 .3 ml) and a monomer solution (monomer component concentration: 36% by volume) dissolved in a mixed solvent of ethyl acetate 18.3 g (20.3 ml) were charged (solvent and single amount charged in the reaction vessel) (The concentration of the monomer component in the total amount with the body solution is 28% by volume). 57 g of a water-soluble polymer was obtained. The polymerization rate of the monomer component at the completion of the addition of the monomer solution was 72%.
- Comparative Example 4 A reaction vessel similar to that used in Example 1 was prepared, and a monomer composed of 45 g of acrylic acid (0.63 mol, 42.8 ml) and 0.25 g (0.26 ml) of pentaerythritol allyl ether. Components, a mixed solvent of 149.4 g (219.7 ml) of normal heptane and 49.4 g (54.9 ml) of ethyl acetate and 0.036 g (0.00015 mol) of 2,2′-azobismethylisobutyrate were charged. It is.
- a monomer component composed of 15 g of acrylic acid (0.21 mol, 14.3 ml) and 0.08 g (0.08 ml) of pentaerythritol allyl ether was added to 13.8 g (20.3 ml) of normal heptane.
- 4.6 g (5.1 ml) of ethyl acetate dissolved in a mixed solvent (monomer component concentration: 36% by volume).
- the concentration of the monomer component in the total amount of the solvent and the monomer solution charged in the reaction vessel is 16% by volume.
- the stirring of the contents of the reaction container was started, and nitrogen gas was blown into the contents in order to remove oxygen present in the contents of the reaction container and in the upper space. Then, the reaction vessel was heated while being maintained in a nitrogen atmosphere, and the monomer solution was continuously added from the addition apparatus over 150 minutes from when the contents of the reaction vessel reached 60 ° C. At this time, the reaction temperature was controlled to gradually rise to 75 ° C. During the addition of the monomer solution, the rotational speed of the stirrer was accelerated from the initial 200 rpm by 50 rpm until the reaction solution slurry whose viscosity gradually increased could be uniformly stirred. After the addition of the monomer solution was completed, the reaction was continued (ripened) for an additional hour while maintaining the temperature at 75 ° C. The polymerization rate of the monomer component at the completion of the addition of the monomer solution was 85%.
- the resulting slurry was transferred to another container and heated to 110 ° C. to distill off normal heptane and ethyl acetate. As a result, 57 g of a white fine powdery alkyl-modified carboxyl group-containing water-soluble polymer was obtained. .
- Comparative Example 5 When the same operation as in Example 2 was carried out except that the continuous addition time of the monomer solution was changed to 80 minutes, 57 g of a white fine powdery alkyl-modified carboxyl group-containing water-soluble polymer was obtained. The polymerization rate of the monomer component at the completion of the addition of the monomer solution was 55%.
- a monomer component consisting of 60 g (0.83 mol, 57.1 ml) of acrylic acid and 0.33 g (0.35 ml) of pentaerythritol allyl ether and 141.6 g of normal heptane (208 .2 ml) and a monomer solution (concentration of monomer component: 18% by volume) dissolved in a mixed solvent of ethyl acetate 46.9 g (52.1 ml) (single solvent and solvent charged in the reaction vessel) (The concentration of the monomer component in the total amount with the body solution is 16% by volume). 57 g of a water-soluble polymer containing was obtained. The polymerization rate of the monomer component at the completion of the addition of the monomer solution was 68%.
- a monomer component consisting of 60 g (0.83 mol, 57.1 ml) of acrylic acid and 0.33 g (0.35 ml) of pentaerythritol allyl ether was added to the addition device and 25.4 g of normal heptane (37 Monomer solution (concentration of monomer component: 55% by volume) dissolved in a mixed solvent of 8.4 g (9.3 ml) and ethyl acetate 8.4 g (9.3 ml). (The concentration of the monomer component in the total amount with the body solution is 16% by volume). 57 g of a water-soluble polymer containing was obtained. The polymerization rate of the monomer component at the completion of the addition of the monomer solution was 80%.
- Comparative Example 8 A reaction apparatus similar to that used in Example 1 was prepared. To this, 45 g of acrylic acid (0.63 mol, 42.9 ml), 1.8 g of lauryl methacrylate (0.007 mol, 2.1 ml) and pentane were added. Monomer component consisting of 0.27 g (0.28 ml) of erythritol allyl ether, a mixed solvent of 160.3 g (235.7 ml) of normal heptane and 70.7 g (78.6 ml) of ethyl acetate, and 2,2′-azo 0.081 g (0.0035 mol) of bismethylisobutyrate was charged. The concentration of the monomer component in the total amount of the solvent and monomer component charged in the reaction vessel is 13% by volume.
- the stirring of the contents of the reaction container was started, and nitrogen gas was blown into the contents in order to remove oxygen present in the contents of the reaction container and in the upper space. And it heated in the state which maintained the inside of reaction container in nitrogen atmosphere, and it was made to react for 200 minutes, maintaining 75 degreeC.
- the rotating speed of the stirrer was accelerated from the initial 200 rpm by 50 rpm until the reaction liquid slurry whose viscosity gradually increased could be uniformly stirred. After completion of the reaction, the reaction was continued (ripened) for 1 hour while maintaining 75 ° C.
- Comparative Example 9 A reaction vessel similar to that used in Comparative Example 1 was prepared, and 5 g of acrylic acid (11 wt% of the total amount of acrylic acid to be added later, 4.8 ml) and 0.03 g of pentaerythritol allyl ether (0 0.03 ml), 0.017 g of ⁇ , ⁇ ′-azobisisobutyronitrile and 210.8 g (314.6 ml) of normal hexane were charged. The concentration of the monomer component in the total amount of the solvent and the monomer component charged in the reaction vessel is 16% by volume.
- the stirring of the contents of the reaction container was started, and nitrogen gas was blown into the contents in order to remove oxygen present in the contents of the reaction container and in the upper space.
- the reaction vessel was heated in a nitrogen atmosphere and kept at 64 to 66 ° C. for 1 hour. At this time, the polymerization rate of the monomer component was 70%. Thereafter, 40 g of acrylic acid (89 wt% of the total amount of acrylic acid previously charged in the reaction vessel, 38.2 ml), 0.24 g (0.25 ml) of pentaerythritol allyl ether and ⁇ , ⁇ ′-azobisiso 0.136 g of butyronitrile was added, and the reaction was further continued for 3 hours.
- the resulting slurry was heated to 90 ° C. to distill off normal hexane and further dried under reduced pressure at 110 ° C. and 10 mmHg for 8 hours to obtain 41 g of a white fine powder of a crosslinked carboxyl group-containing polymer. It was.
- Comparative Example 10 A reaction vessel similar to that used in Comparative Example 1 was prepared, and 22.5 g of acrylic acid (50% by weight of the total amount of acrylic acid to be added later, 21.4 ml) and 0.135 g of pentaerythritol allyl ether were added thereto. (0.14 ml) of a monomer component, ⁇ , ⁇ ′-azobisisobutyronitrile 0.077 g and normal hexane 210.8 g (314.6 ml) were charged. The concentration of the monomer component in the total amount of the solvent and the monomer component charged in the reaction vessel is 12% by volume.
- the stirring of the contents of the reaction container was started, and nitrogen gas was blown into the contents in order to remove oxygen present in the contents of the reaction container and in the upper space. Then, the reaction vessel was heated in a nitrogen atmosphere and kept at 64 to 66 ° C. for 2 hours. At this time, the polymerization rate of the monomer component was 82%. Thereafter, 22.5 g of acrylic acid (50% by weight of the total amount of acrylic acid previously charged in the reaction vessel, 21.4 ml), 0.135 g (0.14 ml) of pentaerythritol allyl ether and ⁇ , ⁇ ′-azo 0.077 g of bisisobutyronitrile was added, and the reaction was further continued for 2 hours.
- the resulting slurry was heated to 90 ° C. to distill off normal hexane and further dried under reduced pressure at 110 ° C. and 10 mmHg for 8 hours to obtain 41 g of a white fine powder of a crosslinked carboxyl group-containing polymer. It was.
- Comparative Example 11 A reaction vessel similar to that used in Comparative Example 1 was prepared, and 40 g (0.56 mol, 38.1 ml) of acrylic acid, 0.2 g (0.0008 mol) of lauryl methacrylate, 0.08 g of sodium carbonate were prepared. 0.25 g (0.26 ml) of pentaerythritol allyl ether, 0.16 g (0.001 mol) of ⁇ , ⁇ ′-azobisisobutyronitrile and 177.0 g (264.2 ml) of normal hexane were charged.
- the stirring of the contents of the reaction container was started, and nitrogen gas was blown into the contents in order to remove oxygen present in the contents of the reaction container and in the upper space. Then, the reaction vessel was heated in a nitrogen atmosphere and kept at 60 to 65 ° C. for 60 minutes.
- the total amount of unreacted acrylic acid and lauryl methacrylate in the reaction solution at this time is 0.215 mol, and 38 mol% with respect to the total amount of acrylic acid and lauryl methacrylate charged in the reaction vessel. Met.
- the resulting slurry was transferred to another container and heated to 90 ° C. to distill off normal hexane, whereby 48 g of a white fine powdery alkyl-modified carboxyl group-containing water-soluble polymer was obtained.
- Comparative Example 12 A reaction vessel similar to that used in Comparative Example 1 was prepared, and 40 g of acrylic acid (0.56 mol, 38.1 ml), 0.08 g of potassium carbonate, 0.48 g of diethylene glycol diallyl ether, ⁇ , ⁇ ′- Azobisisobutyronitrile (0.16 g, 0.001 mol) and normal hexane (177.0 g, 264.2 ml) were charged.
- the stirring of the contents of the reaction container was started, and nitrogen gas was blown into the contents in order to remove oxygen present in the contents of the reaction container and in the upper space.
- the reaction vessel was heated in a nitrogen atmosphere and maintained at 60 to 65 ° C. for 90 minutes. At this time, the amount of unreacted acrylic acid in the reaction solution was 0.170 mol, and 30 mol% with respect to the acrylic acid charged in the reaction vessel.
- the produced slurry was transferred to another container and heated to 90 ° C. to distill off normal hexane, whereby 48 g of a white fine powdery alkyl-modified carboxyl group-containing water-soluble polymer was obtained.
- reaction liquid slurry viscosity The level of the viscosity of the reaction liquid slurry was evaluated based on the number of revolutions of the stirring blade necessary for uniformly stirring the reaction liquid slurry during the polymerization with a stirrer (final rotation speed after acceleration). When this rotational speed exceeds 600 rpm, the viscosity of the reaction liquid slurry is high, and it is difficult to control the reaction heat during the polymerization reaction, and there is a risk of causing a sudden boiling of the reaction liquid.
- the ratio between the weight and the volume of the produced carboxyl group-containing water-soluble polymer powder The ratio between the weight and the volume of the produced carboxyl group-containing water-soluble polymer powder. Specifically, 10 g of the carboxyl group-containing water-soluble polymer powder is introduced into a 50 ml empty graduated cylinder from the height of 5 cm within 20 seconds, and the volume occupied by the carboxyl group-containing water-soluble polymer powder ( ml). The bulk specific gravity (g / ml) was calculated by dividing the weight (10 g) of the charged carboxyl group-containing water-soluble polymer powder by the measured volume (ml).
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Abstract
Description
(条件1)
工程Aにおいて反応容器に仕込む不活性溶媒の量は、工程Bで連続添加する単量体溶液の全量との合計量における単量体成分の濃度が10~24容量%、好ましくは12~22容量%、より好ましくは14~20容量%になるよう設定する。この濃度が10容量%未満の場合は、1バッチ当りの生産量が少なくなり、不経済になる可能性がある。逆に、24容量%を超える場合は、反応液スラリーの粘度が高くなって反応熱を制御することが困難になることから、反応液の突沸を招く可能性がある。また、生成したカルボキシル基含有水溶性重合体が凝集して塊状化しやすくなることから反応容器の内壁や攪拌翼に付着する傾向があり、粉末状のものとして得られ難くなったり、カルボキシル基含有水溶性重合体の物性に悪影響を与えたりする可能性がある。
工程Bにおいて単量体溶液の全量の連続添加が完了するまでの時間を、単量体溶液の全量の添加完了時において単量体成分の重合率が60%以上になるよう設定する。この時間は、単量体溶液の組成、ラジカル重合開始剤の使用量および反応温度等の各種要因により変動するため、一定のものではないが、通常は連続添加が完了するまでの時間を長く設定すると、上記重合率を達成することができる。なお、単量体成分の重合率は、下記の式により求められる。
攪拌機、温度計、窒素吹き込み管、添加装置および冷却管を備えた500mL容の丸型セパラブルフラスコ(球径110mm)からなる反応容器を用意した。ここで用いた攪拌機は、4枚パドル型攪拌翼(翼径75mm、翼幅14mm、ピッチ度45度)を備えたものであり、この攪拌翼をセパラブルフラスコの底部から5mm上方に配置したものである。
実施例1で用いたものと同様の反応容器を用意し、これにノルマルヘプタン107.9g(158.7ml)と酢酸エチル35.7g(39.7ml)との混合溶媒および2,2’-アゾビスメチルイソブチレート0.036g(0.00015モル)を仕込んだ。また、添加装置には、アクリル酸60g(0.83モル、57.1ml)およびペンタエリトリトールアリルエーテル0.33g(0.35ml)とからなる単量体成分をノルマルヘプタン55.3g(81.3ml)と酢酸エチル18.3g(20.3ml)との混合溶媒に溶解した単量体溶液(単量体成分の濃度:36容量%)を仕込んだ。反応容器に仕込んだ溶媒と単量体溶液との合計量における単量体成分の濃度は16容量%である。
実施例1で用いたものと同様の反応容器を用意し、これにノルマルヘプタン107.9g(158.7ml)と酢酸エチル35.7g(39.7ml)との混合溶媒および2,2’-アゾビスメチルイソブチレート0.036g(0.00015モル)を仕込んだ。また、添加装置には、アクリル酸60g(0.83モル、57.1ml)とペンタエリトリトールアリルエーテル0.33g(0.35ml)とからなる単量体成分をノルマルヘプタン55.3g(81.3ml)と酢酸エチル18.3g(20.3ml)との混合溶媒に溶解した単量体溶液(単量体成分の濃度:36容量%)を仕込んだ。反応容器に仕込んだ溶媒と単量体溶液との合計量における単量体成分の濃度は16容量%である。
実施例2において、反応容器にノルマルヘプタン54.9g(80.7ml)と酢酸エチル18.2g(20.2ml)との混合溶媒および2,2’-アゾビスメチルイソブチレート0.036g(0.00015モル)を仕込んだ点、および、添加装置にアクリル酸60g(0.83モル、57.1ml)とペンタエリトリトールアリルエーテル0.30g(0.32ml)とからなる単量体成分をノルマルヘプタン55.3g(81.3ml)と酢酸エチル18.3g(20.3ml)との混合溶媒に溶解した単量体溶液(単量体成分の濃度:36容量%)を仕込んだ点(反応容器に仕込んだ溶媒と単量体溶液との合計量における単量体成分の濃度は22容量%である)を除き、実施例2と同様に操作したところ、白色微粉末状のアルキル変性カルボキシル基含有水溶性重合体57gが得られた。なお、単量体溶液の添加完了時における単量体成分の重合率は81%であった。
実施例1で用いたものと同様の反応容器を用意し、これにアクリル酸24g(0.33モル、22.9ml)とペンタエリトリトールアリルエーテル0.10g(0.11ml)とからなる単量体成分、ノルマルヘプタン111.4g(163.8ml)と酢酸エチル36.8g(40.9ml)との混合溶媒および2,2’-アゾビスメチルイソブチレート0.036g(0.00015モル)を仕込んだ。また、添加装置には、アクリル酸36g(0.50モル、34.3ml)とペンタエリトリトールアリルエーテル0.23g(0.24ml)とからなる単量体成分をノルマルヘプタン51.8g(76.2ml)と酢酸エチル17.2g(19.1ml)との混合溶媒に溶解した単量体溶液(単量体成分の濃度:36容量%)を仕込んだ。反応容器に仕込んだ溶媒および単量体成分と単量体溶液との合計量における単量体成分の濃度は16容量%である。
単量体溶液の連続添加の時間を120分に変更した点を除いて実施例2と同様に操作したところ、白色微粉末状のアルキル変性カルボキシル基含有水溶性重合体57gが得られた。なお、単量体溶液の添加完了時における単量体成分の重合率は62%であった。
反応容器にノルマルヘプタン64.8g(95.3ml)と酢酸エチル21.4g(23.8ml)との混合溶媒および2,2’-アゾビスメチルイソブチレート0.036g(0.00015モル)を仕込んだ点、および、添加装置にアクリル酸60g(0.83モル、57.1ml)とペンタエリトリトールアリルエーテル0.33g(0.35ml)とからなる単量体成分をノルマルヘプタン98.4g(144.7ml)と酢酸エチル32.6g(36.2ml)との混合溶媒に溶解した単量体溶液(単量体成分の濃度:24容量%)を仕込んだ(反応容器に仕込んだ溶媒と単量体溶液との合計量における単量体成分の濃度は16容量%である)点を除き、実施例2と同様に操作したところ、白色微粉末状のアルキル変性カルボキシル基含有水溶性重合体57gが得られた。なお、単量体溶液の添加完了時における単量体成分の重合率は75%であった。
添加装置にアクリル酸60g(0.83モル、57.1ml)、メタクリル酸ラウリル2.4g(0.009モル)およびペンタエリトリトールアリルエーテル0.33g(0.35ml)からなる単量体成分をノルマルヘプタン55.3g(81.3ml)と酢酸エチル18.3g(20.3ml)との混合溶媒に溶解した単量体溶液(単量体成分の濃度:37容量%)を仕込んだ(反応容器に仕込んだ溶媒と単量体溶液との合計量における単量体成分の濃度は17容量%である)点を除いて実施例2と同様に操作したところ、白色微粉末状のアルキル変性カルボキシル基含有水溶性重合体57gが得られた。なお、単量体溶液の添加完了時における単量体成分の重合率は81%であった。
添加装置にアクリル酸60g(0.83モル、57.1ml)とメタクリル酸ステアリル3.0g(0.009モル、3.3ml)とからなる単量体成分をノルマルヘプタン55.3g(81.3ml)と酢酸エチル18.3g(20.3ml)との混合溶媒に溶解した単量体溶液(単量体成分の濃度:37容量%)を仕込んだ(反応容器に仕込んだ溶媒と単量体溶液との合計量における単量体成分の濃度は17容量%である)点を除いて実施例2と同様に操作したところ、白色微粉末状のアルキル変性カルボキシル基含有水溶性重合体61gが得られた。なお、単量体溶液の添加完了時における単量体成分の重合率は83%であった。
攪拌機、温度計、窒素吹き込み管および冷却管を備えた500ml容の丸型セパラブルフラスコ(球径110mm)からなる反応容器を用意した。ここで用いた攪拌機は、実施例1で用いたものと同様のものである。この反応容器にアクリル酸(単量体成分)45g(0.63モル、42.9ml)、1,2-ジクロロエタン392.9g(314.3ml)、ペンタエリトリトールアリルエーテル0.36g(0.38ml)および2,2’-アゾビスメチルイソブチレート0.095g(0.00004モル)を仕込んだ(単量体成分濃度:12容量%)。そして、反応容器の内容物の攪拌を開始し、また、反応容器の内容物中および上部空間に存在している酸素を除去するために、内容物中に窒素ガスを吹き込んだ。
比較例1で用いたものと同様の反応容器を用意し、これにアクリル酸(単量体成分)45g(0.63モル、42.9ml)、ペンタエリトリトールアリルエーテル0.27g(0.28ml)、ノルマルヘプタン160.3g(235.7ml)と酢酸エチル70.7g(78.6ml)との混合溶媒および2,2’-アゾビスメチルイソブチレート0.081g(0.0035モル)を仕込んだ(単量体成分濃度:12容量%)。そして、反応容器の内容物の攪拌を開始し、また、反応容器の内容物中および上部空間に存在している酸素を除去するために、内容物中に窒素ガスを吹き込んだ。
反応容器にノルマルヘプタン24.7g(36.3ml)と酢酸エチル8.2g(9.1ml)との混合溶媒および2,2’-アゾビスメチルイソブチレート0.036g(0.00015モル)を仕込んだ点、および、添加装置にアクリル酸60g(0.83モル、57.1ml)とペンタエリトリトールアリルエーテル0.30g(0.32ml)とからなる単量体成分をノルマルヘプタン55.3g(81.3ml)と酢酸エチル18.3g(20.3ml)との混合溶媒に溶解した単量体溶液(単量体成分の濃度:36容量%)を仕込んだ(反応容器に仕込んだ溶媒と単量体溶液との合計量における単量体成分の濃度は28容量%である)点を除いて実施例2と同様に操作したところ、白色微粉末状のアルキル変性カルボキシル基含有水溶性重合体57gが得られた。なお、単量体溶液の添加完了時における単量体成分の重合率は72%であった。
実施例1で用いたものと同様の反応容器を用意し、これにアクリル酸45g(0.63モル、42.8ml)とペンタエリトリトールアリルエーテル0.25g(0.26ml)とからなる単量体成分、ノルマルヘプタン149.4g(219.7ml)と酢酸エチル49.4g(54.9ml)との混合溶媒および2,2’-アゾビスメチルイソブチレート0.036g(0.00015モル)を仕込んだ。また、添加装置には、アクリル酸15g(0.21モル、14.3ml)とペンタエリトリトールアリルエーテル0.08g(0.08ml)とからなる単量体成分をノルマルヘプタン13.8g(20.3ml)と酢酸エチル4.6g(5.1ml)との混合溶媒に溶解した単量体溶液(単量体成分の濃度:36容量%)を仕込んだ。反応容器に仕込んだ溶媒と単量体溶液との合計量における単量体成分の濃度は16容量%である。
単量体溶液の連続添加の時間を80分に変更した点を除いて実施例2と同様に操作したところ、白色微粉末状のアルキル変性カルボキシル基含有水溶性重合体57gが得られた。なお、単量体溶液の添加完了時における単量体成分の重合率は55%であった。
反応容器にノルマルヘプタン21.6g(31.8ml)と酢酸エチル7.1g(7.9ml)との混合溶媒および2,2’-アゾビスメチルイソブチレート0.036g(0.00015モル)を仕込んだ点、および、添加装置にアクリル酸60g(0.83モル、57.1ml)とペンタエリトリトールアリルエーテル0.33g(0.35ml)とからなる単量体成分をノルマルヘプタン141.6g(208.2ml)と酢酸エチル46.9g(52.1ml)との混合溶媒に溶解した単量体溶液(単量体成分の濃度:18容量%)を仕込んだ(反応容器に仕込んだ溶媒と単量体溶液との合計量における単量体成分の濃度は16容量%である)点を除き、実施例2と同様に操作したところ、白色微粉末状のアルキル変性カルボキシル基含有水溶性重合体57gが得られた。なお、単量体溶液の添加完了時における単量体成分の重合率は68%であった。
反応容器にノルマルヘプタン137.8g(202.6ml)と酢酸エチル45.6g(50.7ml)との混合溶媒および2,2’-アゾビスメチルイソブチレート0.036g(0.00015モル)を仕込んだ点、および、添加装置にアクリル酸60g(0.83モル、57.1ml)とペンタエリトリトールアリルエーテル0.33g(0.35ml)とからなる単量体成分をノルマルヘプタン25.4g(37.4ml)と酢酸エチル8.4g(9.3ml)との混合溶媒に溶解した単量体溶液(単量体成分の濃度:55容量%)を仕込んだ(反応容器に仕込んだ溶媒と単量体溶液との合計量における単量体成分の濃度は16容量%である)点を除き、実施例2と同様に操作したところ、白色微粉末状のアルキル変性カルボキシル基含有水溶性重合体57gが得られた。なお、単量体溶液の添加完了時における単量体成分の重合率は80%であった。
実施例1で用いたものと同様の反応装置を用意し、これにアクリル酸45g(0.63モル、42.9ml)、メタクリル酸ラウリル1.8g(0.007モル、2.1ml)およびペンタエリトリトールアリルエーテル0.27g(0.28ml)からなる単量体成分、ノルマルヘプタン160.3g(235.7ml)と酢酸エチル70.7g(78.6ml)との混合溶媒および2,2’-アゾビスメチルイソブチレート0.081g(0.0035モル)を仕込んだ。反応容器に仕込んだ溶媒と単量体成分との合計量における単量体成分の濃度は13容量%である。
比較例1で用いたものと同様の反応容器を用意し、これにアクリル酸5g(後に添加するアクリル酸との合計量の11重量%、4.8ml)とペンタエリトリトールアリルエーテル0.03g(0.03ml)とからなる単量体成分、α,α’-アゾビスイソブチロニトリル0.017gおよびノルマルヘキサン210.8g(314.6ml)を仕込んだ。反応容器に仕込んだ溶媒と単量体成分との合計量における単量体成分の濃度は16容量%である。
比較例1で用いたものと同様の反応容器を用意し、これにアクリル酸22.5g(後に添加するアクリル酸との合計量の50重量%、21.4ml)とペンタエリトリトールアリルエーテル0.135g(0.14ml)とからなる単量体成分、α,α’-アゾビスイソブチロニトリル0.077gおよびノルマルヘキサン210.8g(314.6ml)を仕込んだ。反応容器に仕込んだ溶媒と単量体成分との合計量における単量体成分の濃度は12容量%である。
比較例1で用いたものと同様の反応容器を用意し、これにアクリル酸40g(0.56モル、38.1ml)、メタクリル酸ラウリル0.2g(0.0008モル)、炭酸ナトリウム0.08g、ペンタエリトリトールアリルエーテル0.25g(0.26ml)、α,α’-アゾビスイソブチロニトリル0.16g(0.001モル)およびノルマルヘキサン177.0g(264.2ml)を仕込んだ。
比較例1で用いたものと同様の反応容器を用意し、これにアクリル酸40g(0.56モル、38.1ml)、炭酸カリウム0.08g、ジエチレングリコールジアリルエーテル0.48g、α,α’-アゾビスイソブチロニトリル0.16g(0.001モル)およびノルマルヘキサン177.0g(264.2ml)を仕込んだ。
実施例1~9および比較例1~12について、重合反応中の反応液スラリーの状況を評価した。ここでは、重合中の反応液スラリー粘度および重合生成物の反応容器への付着状況を下記の方法で評価した。結果を表1、2に示す。
重合中の反応液スラリーを攪拌機により均一に攪拌するために必要な攪拌翼の回転数(加速後の最終回転数)により反応液スラリー粘度の高低を評価した。この回転数が600rpmを超える場合は、反応液スラリーの粘度が高く、重合反応中の反応熱の制御が困難であって反応液の突沸を招く危険性がある。
比較例2の重合生成物の反応容器への付着状況を5とし、これとの目視での比較による付着量を1~5の5段階評価した。数字が小さいほど、反応容器への付着が少ないことを意味する。
実施例1~9および比較例1~12で得られたカルボキシル基含有水溶性重合体粉末について、下記の方法で嵩比重、水不溶分の有無および0.5重量%水溶液粘度を調べた。結果を表1、2に示す。
生成したカルボキシル基含有水溶性重合体粉末の重量と容積との比をいう。具体的には、50ml容の空メスシリンダーに対し、その上部5cmの高さからカルボキシル基含有水溶性重合体粉末10gを20秒間以内で投入し、カルボキシル基含有水溶性重合体粉末の占める容積(ml)を測定した。そして、投入したカルボキシル基含有水溶性重合体粉末の重量(10g)を測定した容積(ml)で除することで、嵩比重(g/ml)を算出した。
2,000mlビーカーにイオン交換水1,000gを入れ、ディスパー(プライミクス株式会社の商品名「T.K.ロボミックス」にディスパー翼を取り付けたもの)にて5,000rpmで攪拌しながらカルボキシル基含有水溶性重合体20gを投入した。30分攪拌後、重量既知の250メッシュろ布で吸引ろ過し、ろ布を110℃で3時間乾燥することでろ布上の水分を十分に除去し、重量を測定した。そして、下記の式により水不溶分の割合を算出した。ここでは、水不溶分の割合が0.03%以下のとき、水不溶分がないものと判定した。
容量500mlのビーカーにイオン交換水298.5gを入れ、これを4枚羽根パドル(翼径50mm)を備えた攪拌機を用いて300rpmの回転速度で攪拌しながらカルボキシル基含有水溶性重合体1.5gを一括で投入した。カルボキシル基含有水溶性重合体の溶解を目視により確認し、得られた0.5重量%溶液を水酸化ナトリウムでpH7に中和して中和粘稠液を得た。この中和粘稠液の粘度をB型粘度計により25℃、20rpmで測定した。表1によると、実施例1~8で得られたカルボキシル基含有水溶性重合体は、この粘度が高いことから、増粘剤として有効である。
AA:アクリル酸
LM:メタクリル酸ラウリル
SM:メタクリル酸ステアリル
PEA:ペンタエリトリトールアリルエーテル
DEDA:ジエチレングリコールジアリルエーテル
EDC:1,2-ジクロロエタン
HEP:ノルマルヘプタン
EA:酢酸エチル
HEX:ノルマルヘキサン
Claims (8)
- α,β-不飽和カルボン酸類を含む単量体成分を不活性溶媒中で反応させることでカルボキシル基含有水溶性重合体を製造するための方法であって、
不活性溶媒を仕込んだ反応容器を用意する工程Aと、
前記反応容器に仕込んだ前記不活性溶媒に対し、前記単量体成分を20~50容量%の濃度で不活性溶媒に溶解した単量体溶液を連続添加する工程Bとを含み、
工程Aにおいて前記反応容器に仕込む前記不活性溶媒の量は、前記単量体溶液との合計量における前記単量体成分の濃度が10~24容量%になるよう設定し、
工程Bにおいて前記単量体溶液の全量の連続添加を完了するまでの時間は、前記単量体溶液の全量の添加完了時において前記単量体成分の重合率が60%以上になるよう設定する、
カルボキシル基含有水溶性重合体の製造方法。 - 前記単量体溶液の全量の連続添加の完了後に反応を継続する工程Cをさらに含む、請求項1に記載のカルボキシル基含有水溶性重合体の製造方法。
- 工程Cでの反応終了後に反応溶液から不活性溶媒を揮散させて除去する工程Dをさらに含む、請求項2に記載のカルボキシル基含有水溶性重合体の製造方法。
- 前記α,β-不飽和カルボン酸類が、アクリル酸、メタクリル酸、アクリル酸とアルキル基の炭素数が10~30の高級アルコールとのエステルおよびメタクリル酸とアルキル基の炭素数が10~30の高級アルコールとのエステルからなる群から選択される少なくとも一種である、請求項1から3のいずれかに記載のカルボキシル基含有水溶性重合体の製造方法。
- 前記単量体成分がエチレン性不飽和基を2個以上有する重合性化合物をさらに含む、請求項4に記載のカルボキシル基含有水溶性重合体の製造方法。
- エチレン性不飽和基を2個以上有する前記重合性化合物が、ペンタエリトリトールアリルエーテル、ポリアリルサッカロース、ジエチレングリコールジアリルエーテルおよびポリエチレングリコールジアリルエーテルからなる群から選択される少なくとも一種である、請求項5に記載のカルボキシル基含有水溶性重合体の製造方法。
- 前記反応溶液に仕込んだ前記不活性溶媒と、前記単量体溶液において前記単量体成分を溶解した前記不活性溶媒とが同じものである、請求項1から3のいずれかに記載のカルボキシル基含有水溶性重合体の製造方法。
- 工程Aにおいて前記反応容器に仕込む前記不活性溶媒に対し、前記単量体成分の総量の50重量%未満を予め溶解しておく、請求項1から3のいずれかに記載のカルボキシル基含有水溶性重合体の製造方法。
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Citations (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH01217017A (ja) | 1988-02-19 | 1989-08-30 | B F Goodrich Co:The | 高い増粘性および優れた透明性を有するポリカルボン酸 |
JPH0222312A (ja) | 1988-05-26 | 1990-01-25 | Sumitomo Seika Chem Co Ltd | 架橋型カルボキシル基含有重合体の製造方法 |
JPH02258813A (ja) | 1988-11-28 | 1990-10-19 | B F Goodrich Co:The | 架橋ポリアクリル酸 |
JPH06107720A (ja) | 1992-10-01 | 1994-04-19 | Sumitomo Seika Chem Co Ltd | 架橋型カルボキシル基含有重合体の製造方法 |
US5663253A (en) | 1996-06-20 | 1997-09-02 | 3V Inc. | Policarboxylic acids |
JP2002097205A (ja) | 2000-09-21 | 2002-04-02 | Nippon Junyaku Kk | 水溶性架橋共重合体粉末の製造方法 |
JP2003268009A (ja) | 2002-03-18 | 2003-09-25 | Sumitomo Seika Chem Co Ltd | カルボキシル基含有水溶性重合体の製造方法 |
JP2005126445A (ja) | 2000-03-15 | 2005-05-19 | Kao Corp | ジャスモン酸エステル誘導体及びその中間体の製造法 |
JP2007246917A (ja) * | 2007-05-24 | 2007-09-27 | Nippon Shokubai Co Ltd | (メタ)アクリル酸系重合体の製造方法 |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2032953C3 (de) * | 1970-07-03 | 1978-08-17 | Deutsche Gold- Und Silber-Scheideanstalt Vormals Roessler, 6000 Frankfurt | Verfahren zur Herstellung perlförmiger Polymerisate der Acrylsäure und Verwendung dieser Polyacrylsäuren |
JPH05178919A (ja) * | 1991-12-27 | 1993-07-20 | Sugai Kagaku Kogyo Kk | 高吸水性樹脂及びその製法 |
-
2010
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Patent Citations (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH01217017A (ja) | 1988-02-19 | 1989-08-30 | B F Goodrich Co:The | 高い増粘性および優れた透明性を有するポリカルボン酸 |
JPH0222312A (ja) | 1988-05-26 | 1990-01-25 | Sumitomo Seika Chem Co Ltd | 架橋型カルボキシル基含有重合体の製造方法 |
JPH02258813A (ja) | 1988-11-28 | 1990-10-19 | B F Goodrich Co:The | 架橋ポリアクリル酸 |
JPH06107720A (ja) | 1992-10-01 | 1994-04-19 | Sumitomo Seika Chem Co Ltd | 架橋型カルボキシル基含有重合体の製造方法 |
US5663253A (en) | 1996-06-20 | 1997-09-02 | 3V Inc. | Policarboxylic acids |
JP2005126445A (ja) | 2000-03-15 | 2005-05-19 | Kao Corp | ジャスモン酸エステル誘導体及びその中間体の製造法 |
JP2002097205A (ja) | 2000-09-21 | 2002-04-02 | Nippon Junyaku Kk | 水溶性架橋共重合体粉末の製造方法 |
JP2003268009A (ja) | 2002-03-18 | 2003-09-25 | Sumitomo Seika Chem Co Ltd | カルボキシル基含有水溶性重合体の製造方法 |
JP2007246917A (ja) * | 2007-05-24 | 2007-09-27 | Nippon Shokubai Co Ltd | (メタ)アクリル酸系重合体の製造方法 |
Non-Patent Citations (1)
Title |
---|
See also references of EP2463311A4 |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP2730615A1 (en) * | 2011-07-08 | 2014-05-14 | Sumitomo Seika Chemicals Co. Ltd. | Carboxyl group-containing polymer composition |
EP2730615A4 (en) * | 2011-07-08 | 2015-04-22 | Sumitomo Seika Chemicals | Carboxy group-containing polymer composition |
WO2017164357A1 (ja) * | 2016-03-25 | 2017-09-28 | 住友精化株式会社 | アルキル変性カルボキシル基含有共重合体 |
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CN102471389B (zh) | 2013-09-25 |
EP2463311A4 (en) | 2012-12-26 |
KR101668900B1 (ko) | 2016-10-24 |
US20120108776A1 (en) | 2012-05-03 |
US8629230B2 (en) | 2014-01-14 |
CA2765259A1 (en) | 2011-02-10 |
EP2463311A1 (en) | 2012-06-13 |
CA2765259C (en) | 2017-04-04 |
EP2463311B1 (en) | 2014-03-19 |
CN102471389A (zh) | 2012-05-23 |
JPWO2011016364A1 (ja) | 2013-01-10 |
KR20120047893A (ko) | 2012-05-14 |
JP5674223B2 (ja) | 2015-02-25 |
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