WO2011061871A1 - カルボン酸系重合体の製造方法 - Google Patents
カルボン酸系重合体の製造方法 Download PDFInfo
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- WO2011061871A1 WO2011061871A1 PCT/JP2010/003913 JP2010003913W WO2011061871A1 WO 2011061871 A1 WO2011061871 A1 WO 2011061871A1 JP 2010003913 W JP2010003913 W JP 2010003913W WO 2011061871 A1 WO2011061871 A1 WO 2011061871A1
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- 0 CCC(CC)C(*)N=O Chemical compound CCC(CC)C(*)N=O 0.000 description 1
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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
Definitions
- the present invention relates to a method for producing a carboxylic acid polymer.
- Carboxylic acid polymers are suitably used as detergent builders, dispersants, scale inhibitors, and the like.
- Patent Documents 1 and 2 include an aqueous solution of a monomer having a pH of 5 to 9 containing an ⁇ -unsaturated carboxylic acid or a salt thereof, and sulfite in the first polymerization reaction step.
- An aqueous solution and oxygen-containing gas are introduced into a flow mixer to polymerize the monomer.
- a reaction product containing the unreacted monomer obtained in the first polymerization reaction step is obtained.
- a method for producing a carboxylic acid polymer to be polymerized is disclosed.
- Patent Document 3 discloses that an acrylic acid monomer is polymerized by an aqueous solution polymerization method while maintaining the pH of the polymerization system in the range of 6-9.
- Patent Document 4 discloses that a polyacrylic polymer is continuously produced by polymerizing an acrylic monomer mainly composed of an acrylic acid monomer or an acrylate monomer in an aqueous medium. It is disclosed that a continuous reaction apparatus that is a tank reactor is used as a reactor, and the pH value of the reaction solution in the first reactor is controlled to 3.5 or less.
- JP 2003-252911 A JP 2008-120939 A Japanese Patent Laid-Open No. 5-86125 Japanese Patent Laid-Open No. 2003-40912
- the present invention relates to a method for producing a carboxylic acid polymer in which a monomer is polymerized using an aqueous solution of a monomer containing an ⁇ -unsaturated carboxylic acid and / or a salt thereof, an aqueous solution containing a sulfite, and a gas containing oxygen.
- concentration of the sulfite introduced into the reaction solution is 0.001 to 0.05 mol / L
- the pH of the reaction solution is controlled to 5.0 to 10.0.
- FIG. 1 It is a figure which shows the structure of a circulation type reaction apparatus. It is a figure which shows the structure of the modification of a circulation type reaction apparatus.
- (A)-(d) is a figure which shows the structure of another modification of a circulation type reactor.
- (A)-(d) is a figure which shows the structure of another modification of the circulation type reactor.
- (A)-(d) is a figure which shows the structure of a tank reactor.
- FIG. 1 shows a circulating reactor 10 used in a method for producing a carboxylic acid polymer (hereinafter referred to as “polymer”) according to this embodiment.
- both ends of the external circulation line 12 are connected to a reaction tank 11 having a stirring function and a temperature control function.
- the external circulation line 12 is provided with a circulation pump 13 (liquid feeding means).
- the circulation pump 13 feeds the reaction liquid in the reaction tank 11 through the external circulation line 12 from the bottom of the tank toward the top of the tank. To circulate.
- a sulfite supply pipe 14 extending from a sulfite supply source and an oxygen-containing gas supply pipe extending from an oxygen-containing gas supply source (for example, a compressor or a blower facility). 15 are connected to each other.
- the sulfite supply pipe 14 supplies an aqueous solution (hereinafter referred to as “sulfite aqueous solution”) in which sulfite is dissolved to the reaction liquid, and the oxygen-containing gas supply pipe 15 supplies oxygen to the reaction liquid.
- oxygen-containing gas supplies a redox initiator composed of sulfite and oxygen to the reaction solution. Therefore, the sulfite supply pipe 14 and the oxygen-containing gas supply pipe 15 constitute a polymerization initiator supply means.
- a flow mixer 16 is interposed so that the connection portion of the sulfite supply pipe 14 and the oxygen-containing gas supply pipe 15 is arranged on the upstream side.
- the flow mixer 16 performs gas-liquid mixing of the reaction liquid flowing through the external circulation line 12 and the oxygen-containing gas.
- the connection part of the oxygen-containing gas supply pipe 15 is arranged on the upstream side of the flow mixer 16, thereby improving the dispersibility of the gas and liquid and the solubility of oxygen in the circulating reaction liquid. Can do.
- Examples of the flow mixer 16 include a static mixer such as a static mixer and an orifice mixer; a jet nozzle such as an ejector; and a pipe stirrer such as a line mixer.
- a static mixer is preferable from the viewpoints of exhibiting high mixing performance even with a small amount of gas, as well as durability of equipment, maintenance, and the like.
- the static mixer for example, “Dispersion-kun” (manufactured by Fujikin Co., Ltd.) can be preferably used.
- a heat exchanger 17 is provided on the downstream side of the flow mixer 16. This heat exchanger 17 adjusts the temperature of the gas-liquid mixed fluid flowing through the portion of the external circulation line 12 downstream of the flow mixer 16.
- a control valve 18 is provided in the external circulation line 12 on the downstream side of the flow mixer 16.
- the control valve 18 adjusts the flow rate of the gas-liquid mixed fluid flowing through the portion of the external circulation line 12 downstream of the flow-type mixer 16, thereby setting the pressure of the circulation line return portion applied to the gas-liquid mixed fluid. .
- a monomer supply pipe 19 extending from a monomer supply source is connected to the reaction tank 11 at the top of the tank.
- the monomer supply pipe 19 supplies monomer to the reaction solution in the reaction tank 11. Therefore, the monomer supply pipe 19 constitutes a monomer supply means.
- reaction tank 11 and the external circulation line 12 may be provided with a neutralizing agent supply line for supplying a neutralizing agent for neutralizing the monomer.
- the sulfite supply pipe 14 and the oxygen-containing gas supply pipe 15 are connected to the external circulation line 12, respectively.
- the present invention is not limited to this, and as shown in FIG.
- the merging pipe 20 to which each of the sulfite supply pipe 14 and the oxygen-containing gas supply pipe 15 is connected may be connected to the external circulation line 12.
- the sulfite supply pipe 14 and the oxygen-containing gas supply pipe 15 are connected to the external circulation line 12, but the present invention is not particularly limited thereto, as shown in FIG.
- Each of the sulfite supply pipe 14 and the oxygen-containing gas supply pipe 15 may be connected to the reaction tank 11, and as shown in FIG. 3B, the sulfite supply pipe 14 and the oxygen-containing gas supply pipe 15 may be used.
- the merging pipe 20 to which each of the gas supply pipes 15 is connected may be connected to the reaction tank 11, and as shown in FIG. 3C, the oxygen-containing gas supply pipe 15 and the monomer supply pipe.
- the confluence pipe 20 to which each of 19 is connected may be connected to the reaction tank 11 and the sulfite supply pipe 14 may be connected to the reaction tank 11, and as shown in FIG. , Sulfite supply pipe 14 and acid Merging pipe 20 each connected in containing gas supply pipe 15 and the monomer supply pipe 19 may be connected to the configuration in the reaction vessel 11.
- a gas-liquid mixing means of the reaction liquid and the oxygen-containing gas for example, from a blowing nozzle installed in the reaction tank 11
- the monomer supply pipe 19 is connected to the reaction tank 11.
- the monomer supply pipe 19 is connected to the external circulation line as shown in FIG. 4, and as shown in FIG. 4B, a merging pipe 20 to which each of the sulfite supply pipe 14 and the oxygen-containing gas supply pipe 15 is connected is connected to the external circulation line 12.
- the monomer supply pipe 19 may be connected to the external circulation line 12, and as shown in FIG. 4C, each of the oxygen-containing gas supply pipe 15 and the monomer supply pipe 19 4 may be connected to the external circulation line 12, and as shown in FIG. 4D, the sulfite supply pipe 14, the oxygen-containing gas supply pipe 15, and the monomer supply Merging pipe 20 each connected to 19 may be connected to the configuration in the external circulation line 12.
- the circulation type reaction apparatus 10 provided with the external circulation line 12 is used.
- the present invention is not particularly limited thereto, and has a stirring function and a temperature control function as shown in FIG. It may be a tank reactor 10 ′ in which the sulfite supply pipe 14, the oxygen-containing gas supply pipe 15, and the monomer supply pipe 19 are connected to the reaction tank 11.
- the tank reactor 10 ′ has a configuration in which a merging pipe 20 to which a sulfite supply pipe 14 and an oxygen-containing gas supply pipe 15 are connected is connected to the reaction tank 11.
- FIG. 5 (b) the tank reactor 10 ′ has a configuration in which a merging pipe 20 to which a sulfite supply pipe 14 and an oxygen-containing gas supply pipe 15 are connected is connected to the reaction tank 11.
- a configuration in which a junction pipe 20 to which each of the oxygen-containing gas supply pipe 15 and the monomer supply pipe 19 is connected is connected to the reaction tank 11 may be used.
- a merging pipe 20 to which each of the sulfite supply pipe 14, the oxygen-containing gas supply pipe 15, and the monomer supply pipe 19 is connected is connected to the reaction tank 11. May be.
- the oxygen-containing gas is supplied from a blowing nozzle installed in the reaction tank 11 and mixed by a stirring blade.
- Method a method of mixing by supplying an oxygen-containing gas to a sintered tube having a fine porous surface, a static mixer, a static mixer such as an orifice mixer, and a jet nozzle of an ejector, etc.
- a method of supplying the reaction gas 11 to the reaction tank 11 after gas-liquid mixing with the contained gas in advance is exemplified.
- the method for producing a polymer according to this embodiment is based on a semi-batch operation using a redox initiator composed of a sulfite and an oxygen-containing gas.
- a redox initiator composed of a sulfite and an oxygen-containing gas.
- it is not particularly limited to this, it may be a batch operation or a continuous operation.
- the monomer is continuously supplied or intermittently supplied from the monomer supply pipe 19 to the reaction liquid in the reaction system, and the sulfite and oxygen-containing gas from the sulfite supply pipe 14 are supplied.
- the monomer is polymerized and a polymer is produced by a semi-batch operation.
- the reaction raw material of the monomer and / or redox initiator may be supplied to the reaction solution at a constant supply rate.
- the reaction solution is thickened in the later stage of the reaction, and the reaction solution of oxygen in the gas Since the dissolution rate in water may decrease and the monomer concentration in the reaction solution may increase, the supply rate may be changed during the process.
- a method of gradually decreasing the supply rate from the initial stage of the reaction is preferable.
- the concentration of the sulfite introduced into the reaction solution is 0.001 to 0.05 mol / L
- the pH of the reaction solution is controlled to 5.0 to 10.0.
- the concentration of sulfite introduced into the reaction solution is defined as A (L), where the total volume of the reaction solution at a certain point in the reaction is B, and the total number of moles of sulfite introduced into the reaction solution up to that point is B ( mol), it is obtained from B / A (mol / L).
- the concentration of sulfite introduced into the reaction solution is 0.001 to 0.05 mol / L, as in the initial stage of semi-batch operation. Even when the concentration of the redox initiator is low, the polymerization of the polymer can be started quickly by controlling the pH of the reaction solution to 5.0 to 10.0.
- Patent Documents 1 to 4 in the case of producing a carboxylic acid polymer by semi-batch operation while supplying a monomer and a redox initiator, the pH in the polymerization reaction at the initial stage where the concentration of the redox initiator is low. None is disclosed about polymerization conditions such as.
- the concentration of the monomer introduced into the reaction solution is, for example, 0.1 to 2.0 mol / L.
- concentration of the monomer introduced into the reaction solution is defined as A (L), where the total volume of the reaction solution at a certain point in the reaction is C, and the total number of moles of monomer introduced into the reaction solution up to that point is C (mol). It is calculated from C / A (mol / L).
- the monomer is supplied as an aqueous monomer solution to the reaction solution.
- the monomer is a reaction raw material and is an ⁇ -unsaturated carboxylic acid and / or a salt thereof.
- ⁇ -unsaturated carboxylic acids and / or salts thereof monomers having acrylic acid and / or a salt thereof as an essential component are preferable because they are suitable for homopolymerization or copolymerization.
- Acrylic acid can be used as an acrylic acid aqueous solution containing 60% by mass or more of acrylic acid anhydride or acrylic acid.
- the aqueous acrylic acid solution may be an aqueous solution of an alkali metal acrylate that is partially or wholly neutralized, such as a sodium acrylate aqueous solution or a potassium acrylate aqueous solution.
- the monomer contains a hydrophilic monomer copolymerizable with ⁇ -unsaturated carboxylic acid and / or a salt thereof, such as maleic acid, acrylamide, 2-hydroxyethyl acrylate, 2-hydroxyethyl methacrylate, and the like. Also good.
- the content of the hydrophilic monomer copolymerizable with the ⁇ -unsaturated carboxylic acid and / or salt thereof in all monomers is 0 to 30 mol% from the viewpoint of increasing the polymerization reaction rate and facilitating the control of the molecular weight. It is preferable to do.
- the monomer concentration in the monomer aqueous solution is preferably 10 to 100% by mass, and more preferably 30 to 100% by mass.
- the temperature of the aqueous monomer solution is preferably 5 ° C. or higher from the viewpoint of handling as an aqueous solution, and 30 ° C. or lower from the viewpoint of suppressing polymerization of the monomer before starting the reaction. From these viewpoints, the temperature of the monomer aqueous solution is preferably 5 to 30 ° C.
- the temperature of the maleate aqueous solution is preferably 50 to 90 ° C.
- the monomer aqueous solution may contain a pH adjusting agent and the like.
- the redox initiator consists of sulfite and oxygen.
- the sulfite is supplied to the reaction solution as an aqueous sulfite solution.
- Oxygen is supplied to the reaction solution as an oxygen-containing gas.
- Examples of the sulfite include sodium hydrogen sulfite, potassium hydrogen sulfite, and magnesium hydrogen sulfite. Among these, sodium bisulfite having a strong reducing action is preferable.
- the concentration of sulfite in the aqueous sulfite solution is preferably 1 to 40% by mass and more preferably 20 to 40% by mass from the viewpoint of productivity.
- the supply amount of the sulfite aqueous solution facilitates control of the molecular weight suitable for the intended use, and at the same time, is an addition reaction substance (hereinafter referred to as “addition product”) of sulfite with ⁇ -unsaturated carboxylic acid and / or its salt. From the viewpoint of suppressing the formation of), the amount is preferably 0.008 to 0.1 mol of sulfite ion (HSO 3 ⁇ ) per mol of the monomer.
- aqueous sulfite solution may contain a pH adjuster and the like.
- oxygen-containing gas air is generally used, but pure oxygen or a gas obtained by diluting pure oxygen with an inert gas may be used.
- the oxygen concentration in the oxygen-containing gas is preferably 10% by volume or more, and more preferably 20% by volume or more from the viewpoint of reactivity with sulfite. Further, from the viewpoint of stabilizing the reaction, it is preferable to supply the oxygen-containing gas at a constant pressure and a constant volume.
- the oxygen-containing gas flow rate (273K, 101) in the standard state with respect to the reaction liquid flow rate per unit time in the reaction fluid introduced into the external circulation line 12 is used.
- the volume ratio of .3 kPa) is preferably 0.1 or more, more preferably 0.5 or more from the viewpoint of increasing the solubility of the oxygen-containing gas in the reaction solution and performing a polymerization reaction with high initiator efficiency. preferable.
- the pressure is preferably 50 or less, and more preferably 20 or less. From these viewpoints, the ratio of the oxygen-containing gas flow rate in the standard state to the reaction liquid flow rate per unit time in the reaction fluid introduced into the external circulation line 12 is preferably 0.1 to 50, preferably 0.5 to More preferably, it is 20 mm.
- the pH of the reaction solution is more preferably controlled to 5.5 to 10.0, still more preferably 5.5 to 9.5, and more preferably 6.0 to 9.5. Particularly preferred.
- the pH control means is not particularly limited, and examples thereof include a means for adjusting the pH of the monomer aqueous solution and / or the sulfite aqueous solution in advance, a means for adding a pH adjuster to the reaction solution, and the like.
- the monomer supply time is preferably 0.5 hours or more, and more preferably 1 hour or more, from the viewpoint of heat generation control by reaction. Moreover, it is preferable to set it as 50 hours or less from a viewpoint of productivity, and it is more preferable to set it as 30 hours or less.
- the reaction temperature is preferably 50 ° C. or less, more preferably 45 ° C. or less, from the viewpoints of suppressing molecular chain branching and hue deterioration of the polymer and suppressing the formation of adducts.
- the reaction temperature is preferably 20 ° C. or higher, more preferably 25 ° C. or higher. From these viewpoints, the reaction temperature is preferably 20 to 50 ° C, more preferably 25 to 45 ° C.
- the monomer and / or redox initiator reaction raw material may be supplied to the reaction solution at a constant supply rate.
- the reaction solution is thickened in the later stage of the reaction, and the reaction solution of oxygen in the gas. Since the dissolution rate in water may decrease and the monomer concentration in the reaction solution may increase, the supply rate may be changed during the process.
- the number of times the reaction liquid is circulated to the external circulation line 12 refers to the number of times the reaction liquid is circulated to the external circulation line 12 during the monomer supply time.
- the average value can be obtained as follows.
- the average number of circulation of the reaction solution during the monomer supply time is preferably 17 times or more, and more preferably 18 times or more. Also, from the viewpoint of reducing the load on the circulation pump 13, it is preferably 100 times or less, and more preferably 80 times or less.
- the polymerization rate of the obtained polymer is preferably 98% or more.
- the polymerization rate of a polymer is represented by following formula (1).
- the amount of unreacted monomers by aging the reaction solution after stopping the supply of the monomer and the redox initiator.
- the aging time is, for example, 1 to 10 hours.
- the content of unreacted monomer is preferably 1.5% by mass or less, more preferably 1.0% by mass or less, based on the solid content of the polymer. preferable.
- content of an adduct is 4.0 mass% or less with respect to polymer solid content from a viewpoint of raising the quality and yield of a polymer.
- the content of the unreacted monomer and the content of the adduct are concentrations determined by measuring the polymer aqueous solution by HPLC (high performance liquid chromatography) and based on a calibration curve of the unreacted monomer and the adduct having a known concentration. It can be calculated from
- the weight average molecular weight (Mw) of the polymer is usually preferably from 1,000 to 100,000 from the viewpoint of enhancing dispersibility and adsorptivity, and when the polymer is used for a builder for detergent, a dispersant, a scale inhibitor or the like. Is preferably 2000 to 30000cm. Further, the dispersion index represented by the following formula (2) serving as an index of molecular weight distribution is preferably 7 or less, and more preferably 5 or less.
- Example 1 A 1 L flask having a stirrer, a thermometer, a cooler, an air introduction tube, a pH meter, and a dropping nozzle was prepared, and 306 g of water was charged therein and kept in a 25 ° C. water bath. In addition, a beaker with a capacity of 100 ml was prepared, and 27.8 g (0.378 mol) of 98% acrylic acid and 34.1 g of water were added to make a mixed solution, and further 29.4 g of 50% sodium hydroxide under ice cooling. Was added to prepare a monomer aqueous solution having a pH of 6.4.
- the monomer aqueous solution was dropped into the flask in 45 minutes with a metering pump while air was blown into the water in the flask through the air introduction tube at a rate of 1 NL / min.
- 14.9 g of 10% aqueous sodium hydrogen sulfite solution was added dropwise over 45 minutes using another metering pump.
- the flask containing the reaction solution was kept in a water bath for 30 minutes while air was blown from the air introduction tube at a rate of 1 NL / min.
- the supply amount of air (NL / min) is the supply amount in the standard state (273K, 101.3 kPa).
- the concentration of sodium bisulfite introduced into the reaction solution was 0.014 mol / L after 15 minutes from the start of dropping, 0.025 mol / L after 30 minutes from the start of dropping, and the end of dropping 45 minutes after the start of dropping. 0.035 mol / L.
- the concentration of the monomer introduced into the reaction solution was 0.37 mol / L 15 minutes after the start of dropping, 0.67 mol / L 30 minutes after the start of dropping, and 0 at the end of dropping 45 minutes after the start of dropping. .92 mol / L.
- the pH of the reaction solution was 8.8 before dropping of the monomer aqueous solution and sodium hydrogen sulfite aqueous solution, 6.7 after 15 minutes from the start of dropping, 6.8 after 30 minutes from the start of dropping, and 45 minutes after the start of dropping.
- the end of dropping was 6.9, and the end of 30 minutes aging was 7.2.
- curing it measures by HPLC, The content is calculated from the density
- HPLC measurement conditions were as follows. -Column: Tosoh Corporation product name: TSK-GEL ODS-80TS -Mobile phase: 0.02 mol / L Aqueous solution adjusted to pH 2.5 by adding phosphoric acid to potassium dihydrogen phosphate-Detector: UV detector (wavelength: 210 nm) -Column temperature: 30 ° C ⁇ Flow rate: 1.0 mL / min Sample: Ion exchange water was added to a polymer aqueous solution containing a solid content of 0.8 g, and the total liquid volume was adjusted to 200 mL.
- Example 2 As an aqueous monomer solution, 29.3 g (0.367 mol) of 98% acrylic acid and 34.1 g of water were added with 29.3 g of 50% sodium hydroxide under ice cooling to adjust the pH to 8.1. A polymer was produced in the same manner as in Example 1 except that the amount of the 10% aqueous sodium hydrogen sulfite solution added was 15.3 g.
- the concentration of sodium hydrogen sulfite introduced into the reaction solution was 0.014 mol / L after 15 minutes from the start of dropping, 0.026 mol / L after 30 minutes from the start of dropping, and at the end of dropping 45 minutes after the start of dropping. 0.036 mol / L.
- the concentration of the monomer introduced into the reaction solution was 0.36 mol / L 15 minutes after the start of dropping, 0.65 mol / L after 30 minutes from the start of dropping, and 0 at the end of dropping 45 minutes after the start of dropping. .89 mol / L.
- the pH of the reaction solution was 8.9 before dropping of the monomer aqueous solution and sodium hydrogen sulfite aqueous solution, 7.2 after 15 minutes from the start of dropping, 7.6 after 30 minutes from the start of dropping, and 45 minutes after the start of dropping.
- the end of dropping was 7.7, and the end of aging for 30 minutes was 8.1.
- the polymerization rate of the polymer was 76.5% at the end of dropping and 97.4% at the end of ripening.
- Example 3 A circulation reactor having the same configuration as that shown in FIG. 1 and having a 300 L reaction vessel with an external circulation line was used.
- a circulation pump In the external circulation line, in order of the liquid flow direction, a circulation pump, a static mixer (manufactured by Fujikin Co., Ltd., trade name: Dispersion Kim 15D type, flow path constriction part flow path inner diameter 3 mm, 2 units) and A heat exchanger was attached.
- the reaction tank was accompanied by an inclined paddle stirring blade.
- the stirring rotation speed of the inclined paddle stirring blade of the reaction tank is set to 135 rpm, and the circulating reaction liquid flow rate Q is set to 400 L / h, respectively.
- the stirring rotation speed of the inclined paddle stirring blade of the reaction tank is set to 135 rpm, and the circulating reaction liquid flow rate Q is set to 400 L / h, respectively.
- the reaction vessel was supplied with 98 mass% acrylic acid at a rate of 3.7 kg / h and caustic soda with a concentration of 50 mass% at a constant rate of 3.9 kg / h.
- 35 mass% sodium bisulfite aqueous solution is supplied to the external circulation line at 0.68 kg / h, and air as oxygen-containing gas is supplied at a constant rate of 2,200 NL / h, respectively, and the monomer supply time T is set to 14 hours for the polymerization reaction. Went.
- the volume ratio of the oxygen-containing gas flow rate in the standard state to the reaction solution flow rate per unit time in the reaction fluid introduced into the external circulation line 12 was 5.5.
- the gas-liquid mixed fluid was not pressurized with the circulation line return section pressure. During this time, the temperature of the liquid in the tank was controlled at 35 ° C.
- the concentration of sodium hydrogensulfite introduced into the reaction solution is 0.030 mol / L after 1 hour from the start of dropping, 0.054 mol / L after 2 hours from the start of dropping, and 0.17 mol / L at the end of dropping.
- the monomer concentration introduced into the reaction solution is 0.65 mol / L after 1 hour from the start of dropping, 1.18 mol / L after 2 hours from the start of dropping, and 3.82 mol / L at the end of dropping.
- the pH of the reaction solution was 8.2 before dropping of the monomer aqueous solution and sodium hydrogensulfite aqueous solution, 7.9 after 1 hour from the start of dropping, 7.2 after 2 hours from the start of dropping, and 14 hours after the start of dropping.
- the end of dropping was 6.5 and the end of aging for 2 hours was 6.6.
- the polymerization rate of the polymer was 91.4% 2 hours after the start of dropping, 99.1% at the end of dropping, and 99.9% at the end of ripening.
- the concentration of sodium hydrogen sulfite introduced into the reaction solution was 0.015 mol / L after 15 minutes from the start of dropping, 0.027 mol / L after 30 minutes from the start of dropping, and the end of dropping 45 minutes after the start of dropping. 0.037 mol / L.
- the concentration of the monomer introduced into the reaction solution was 0.45 mol / L 15 minutes after the start of dropping, 0.81 mol / L 30 minutes after the start of dropping, and 1 at the end of dropping 45 minutes after the start of dropping. .11 mol / L.
- the pH of the reaction solution was 7.7 before dropping of the monomer aqueous solution and sodium hydrogen sulfite aqueous solution, 4.4 after 15 minutes from the start of dropping, 4.4 after 30 minutes from the start of dropping, and 45 minutes after the start of dropping.
- the end of dropping was 4.3, and the end of aging for 30 minutes was 4.4.
- the polymerization rate of the polymer was 0.0% at the end of dropping and 7.4% at the end of ripening.
- the present invention is useful for a method for producing a carboxylic acid polymer.
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Abstract
Description
図1は本実施形態に係るカルボン酸系重合体(以下、「重合体」という。)の製造方法において用いられる循環型反応装置10を示す。
本実施形態に係る重合体の製造方法は、亜硫酸塩と酸素含有ガスとからなるレドックス開始剤を用いた半回分操作によるものである。但し、特にこれに限定されるものではなく、回分操作によるものであってもよく、また、連続操作によってもよい。
モノマーは反応液に対してモノマー水溶液として供給する。
レドックス開始剤は、亜硫酸塩と酸素とからなる。亜硫酸塩は反応液に対して亜硫酸塩水溶液として供給する。酸素は反応液に対して酸素含有ガスとして供給する。
本実施形態に係る重合体の製造方法では、反応液に導入された亜硫酸塩の濃度が0.001~0.05mol/Lであるとき、すなわち重合の初期段階において、重合反応を進める観点から該反応液のpHを5.0~10.0に制御する。
モノマー供給時間は、反応による発熱制御の観点から、0.5時間以上とすることが好ましく、1時間以上とすることがより好ましい。また、生産性の観点から、50時間以下とすることが好ましく、30時間以下とすることがより好ましい。
反応温度は、重合体の分子鎖の分岐や色相劣化を抑制すると共に付加物の生成を抑制する観点から、50℃以下とすることが好ましく、45℃以下とすることがより好ましい。一方、得られる反応生成物を重合体水溶液として取扱う観点から、20℃以上とすることが好ましく、25℃以上とすることがより好ましい。これらの観点から、反応温度は20~50℃とすることが好ましく、25~45℃とすることがより好ましい。
モノマー及び/又はレドックス開始剤の反応原料は、反応液へ一定の供給速度で供給してもよく、また、半回分式操作では反応後期に反応液が増粘してガス中の酸素の反応液への溶解速度が低下し、反応液中のモノマー濃度が増加する場合があるため、途中で供給速度を変更してもよい。反応原料の供給速度を途中で変更する場合は、反応初期から段階的に供給速度を低下させることが好ましい。
外部循環ライン12への反応液の循環回数とは、モノマー供給時間に反応液が外部循環ライン12に循環した回数をいう。具体的には下記のようにして平均値で求めることができる。
N[回/h]=Q[L/h]/V[L]
となる。
モノマー供給時間の平均循環回数[回]=N[回/h]×T[h]
である。
得られる重合体の重合率は98%以上であることが好ましい。なお、重合体の重合率は下記式(1)で表されるものである。
撹拌機、温度計、冷却機、空気導入管、pH計、及び滴下ノズルを具備した容量1Lのフラスコを準備し、それに水306gを仕込んで25℃の水浴中に保持した。また、容量100mlのビーカーを準備し、それに98%アクリル酸27.8g(0.378mol)と水34.1gとを仕込んで混合液とし、さらに、氷冷下で50%水酸化ナトリウム29.4gを加えることによりpHを6.4としたモノマー水溶液を調製した。
・カラム:東ソー社製 商品名:TSK-GEL ODS-80TS
・移動相:0.02mol/Lリン二水素カリウムにリン酸を加えてpHを2.5に調整した水溶液
・検出器:紫外線検出器(波長:210nm)
・カラム温度:30℃
・流速:1.0mL/min
・試料:固形分0.8gを含む重合体水溶液にイオン交換水を添加し、総液量が200mLとなるように調製し、この調製液から10μLを分取してカラムに注入した。
モノマー水溶液として、98%アクリル酸27.0g(0.367mol)と水34.1gとの混合液に、氷冷下で50%水酸化ナトリウム29.3gを加えることによりpHを8.1としたものを用い、また、10%亜硫酸水素ナトリウム水溶液の滴下量を15.3gとしたことを除いて実施例1と同様にして重合体を製造した。
外部循環ラインの付帯した300Lの反応槽を備えた図1と同様の構成の循環型反応装置を用いた。外部循環ラインには液の流れ方向に順に、循環ポンプ、静止型混合器(株式会社フジキン社製、商品名:分散君15D型、流路孔の縮流部流路内径3mm、2ユニット)及び熱交換器を付帯した。また反応槽には傾斜パドル撹拌翼が付帯していた。
モノマー水溶液として、98%アクリル酸32.9g(0.447mol)と水40.4gとの混合液に、氷冷下で50%水酸化ナトリウム20.8gを加えることによりpHを5.0としたものを用い、また、10%亜硫酸水素ナトリウム水溶液の滴下量を16.3gとしたことを除いて実施例1と同様にして重合体を製造した。
10’ 槽型反応装置
11 反応槽
12 外部循環ライン
13 循環ポンプ
14 亜硫酸塩供給管
15 酸素含有ガス供給管
16 流通式混合器
17 熱交換器
18 コントロールバルブ
19 モノマー供給管
20 合流管
Claims (4)
- α-不飽和カルボン酸及び/又はその塩を含有するモノマーの水溶液、亜硫酸塩を含有する水溶液、及び酸素を含有するガスを用いてモノマーを重合させるカルボン酸系重合体の製造方法であって、
反応液に導入された亜硫酸塩の濃度が0.001~0.05mol/Lであるとき、該反応液のpHを5.0~10.0に制御するカルボン酸系重合体の製造方法。 - 重合反応時の反応液の温度を20~50℃に制御する請求項1に記載されたカルボン酸系重合体の製造方法。
- 亜硫酸塩が亜硫酸水素ナトリウムである請求項1又は2に記載のカルボン酸系重合体の製造方法。
- 反応液に、モノマー水溶液、亜硫酸塩水溶液、及び酸素含有ガスを供給しながら半回分操作によりモノマーを重合させる請求項1乃至3のいずれかに記載のカルボン酸系重合体の製造方法。
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JPH1038403A (ja) * | 1996-07-19 | 1998-02-13 | Sanyo Electric Co Ltd | 吸収冷温水機の入熱制御装置 |
JP2002241428A (ja) * | 2001-02-15 | 2002-08-28 | Kao Corp | (メタ)アクリル酸(共)重合体の製造法 |
JP2003048915A (ja) * | 2001-05-31 | 2003-02-21 | Kao Corp | アクリル酸系重合体の製造法 |
JP2009242594A (ja) * | 2008-03-31 | 2009-10-22 | Nippon Shokubai Co Ltd | (メタ)アクリル酸系重合体の製造方法 |
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JPH1038403A (ja) * | 1996-07-19 | 1998-02-13 | Sanyo Electric Co Ltd | 吸収冷温水機の入熱制御装置 |
JP2002241428A (ja) * | 2001-02-15 | 2002-08-28 | Kao Corp | (メタ)アクリル酸(共)重合体の製造法 |
JP2003048915A (ja) * | 2001-05-31 | 2003-02-21 | Kao Corp | アクリル酸系重合体の製造法 |
JP2009242594A (ja) * | 2008-03-31 | 2009-10-22 | Nippon Shokubai Co Ltd | (メタ)アクリル酸系重合体の製造方法 |
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