JP2007191673A - Method for producing phosphate-based polymer - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a method capable of industrially and stably producing a phosphate-based polymer suitable as a dispersing agent for hydraulic composition capable of imparting excellent dispersing effect and viscosity-reducing effect to the hydraulic composition in practical level and good reproducibility. <P>SOLUTION: When copolymerizing a specific monomer 1 having a polyoxyalkylene group with a phosphoric acid monoester-based monomer 2 and a phosphoric acid diester-based monomer 3, a liquid A containing the monomer 1 and a liquid B containing the monomer 2 and the monomer 3 are each separately introduced into a reaction system and ≥90 wt.% of each of total amount of the liquid A and the liquid B introduced into the reaction system is simultaneously introduced into the reaction system to provide the phosphate-based polymer suitable as the dispersing agent for hydraulic composition. <P>COPYRIGHT: (C)2007,JPO&INPIT

Description

  The present invention relates to a method for producing a phosphate ester polymer suitably used for a dispersant for hydraulic composition.

  Among the admixtures for hydraulic compositions, there is one called a high-performance water reducing agent having a large fluidity-imparting effect. Typical examples thereof include naphthalene sulfonic acid formaldehyde condensate salt (naphthalene type), melamine sulfonic acid formaldehyde condensate salt (melamine type), polycarboxylic acid type having a polyoxyalkylene chain, and the like.

  In recent years, concrete, which is a typical hydraulic composition, has become more durable. For example, the amount of water used in concrete has been reduced to increase its strength. Are also expected to increase. In order to reduce the amount of water, it is mainstream to use a polycarboxylic acid-based water reducing agent that is excellent in water reduction and fluidity retention. However, as the amount of water decreases, fresh concrete viscosity (hereinafter also referred to as concrete viscosity) increases, and there is a problem that workability and workability such as pumping, driving and filling into a formwork are lowered. This viscosity increase problem has not been sufficiently solved even with a polycarboxylic acid-based water reducing agent, and an additive having a higher concrete viscosity reducing effect is desired.

  From such a background, Patent Document 1 discloses a monodisperse having a polyalkylene glycol chain in order to obtain a cement dispersant capable of exhibiting excellent flow characteristics, a high dispersion effect, and quick setting regardless of the mixing ratio of water. It has been proposed to use a polymer of an ester or monoether and a monomer having an unsaturated bond and a phosphate group.

Further, as seen in the method for producing a polycarboxylic acid-based dispersant, the polymer obtained by the monomer charging method is greatly different in performance required as a cement dispersant. For example, Patent Document 2 proposes a method in which a monomer component and a chain transfer agent component are previously charged in a reaction vessel, and a polymerization initiator is added to perform polymerization. Patent Document 3 proposes a method of polymerizing a solution in which a monomer component and a chain transfer agent are mixed in advance and a polymerization initiator, respectively.
JP 2000-327386 A JP-A-1-226757 JP-A-9-86990

  An object of the present invention is to provide a copolymer that can impart an excellent dispersion effect and viscosity reduction effect to a hydraulic composition containing a hydraulic powder, and serves as a dispersant for a hydraulic composition with good performance. An object is to provide a method that can be produced stably and reproducibly (with little variation in molecular weight depending on the production lot) at an industrially practical level.

The present invention relates to a monomer 1 represented by the following general formula (1), a monomer 2 represented by the following general formula (2), and a monomer 3 represented by the following general formula (3). A method for producing a phosphate ester polymer obtained by polymerizing
A liquid A containing the monomer 1 and a liquid B containing the monomer 2 and the monomer 3 are separately introduced into the reaction system, respectively.
90% by weight or more of each of the total amount of liquid A and liquid B introduced into the reaction system is introduced into the reaction system in parallel.
The present invention relates to a method for producing a phosphate ester polymer.

[Wherein R ¹ and R ² are each a hydrogen atom or a methyl group, R ³ is a hydrogen atom or —COO (AO) _n X, AO is an oxyalkylene group or oxystyrene group having 2 to 4 carbon atoms, n is It is the average added mole number of AO, the number of 3-200, X represents a hydrogen atom or a C1-C18 alkyl group. ]

[Wherein, R ⁴ represents a hydrogen atom or a methyl group, R ⁵ represents an alkylene group having 2 to 12 carbon atoms, m1 represents a number of 1 to 30, and M represents a hydrogen atom, an alkali metal or an alkaline earth metal. ]

[Wherein R ⁶ and R ⁸ are each a hydrogen atom or a methyl group, R ⁷ and R ⁹ are each an alkylene group having 2 to 12 carbon atoms, m2 and m3 are each a number from 1 to 30 and M is hydrogen. Represents an atom, an alkali metal or an alkaline earth metal. ]

  The present invention also relates to a hydraulic composition containing hydraulic powder, water, and a phosphate ester polymer obtained by the production method of the present invention.

According to the present invention, even when a monomer containing a phosphate ester having a large amount of a diester is used, a phosphate ester system suitable as a dispersant for a hydraulic composition, which can suppress high molecular weight and performance degradation due to crosslinking. Provided is a method capable of stably producing a polymer with good reproducibility. Moreover, the production method of the present invention does not impair the properties of the phosphate ester polymer as a dispersant for a hydraulic composition. The dispersant containing the phosphate ester polymer obtained by the production method of the present invention can impart an excellent dispersion effect and viscosity reduction effect to a hydraulic composition containing hydraulic powder, and has performance. It is good.

<< Production Method of Phosphate Ester Polymer >>
In the present invention, the liquid A containing the monomer 1 and the liquid B containing the monomer 2 and the monomer 3 are separately introduced into the reaction system. The present invention relates to a method for producing a phosphate ester polymer in which 90% by weight or more of each of the total amount of liquid A and liquid B is introduced into a reaction system in parallel. Any of the phosphate ester polymers according to the present invention can be produced by this production method.

  The inventors of the present invention are effective in reducing the viscosity of a hydraulic composition, which is one of the problems of the present invention, by using a polymer derived from a specific phosphate ester, and a production method suitable for industrialization to obtain such a polymer. I found it.

  Hereinafter, the manufacturing method of the phosphate ester type polymer using the monomers 1-3 is demonstrated.

  Industrially, the phosphate ester monomer is usually obtained as a mixture containing a monoester (monomer 2) and a diester (monomer 3). Among these, since diesters are likely to have a high molecular weight (gelation) by crosslinking, such a mixture is restricted in production in fields using the properties, for example, thickeners, adhesives, coatings, etc. Can be used suitably without receiving much. On the other hand, for admixtures for hydraulic compositions (dispersants, water reducing agents, etc.), copolymers containing phosphate groups are preferred because of their excellent adsorptive power to hydraulic substances, but dispersibility and viscosity are reduced by increasing the molecular weight. This is not preferable from the viewpoint of handleability. However, it is industrially disadvantageous to separate the monoester form and the diester form from the mixture of phosphate esters as raw materials from the application and economical properties of the hydraulic composition. In the production method of the present invention, the liquid A containing the monomer 1 and the liquid B containing the monomer 2 and the monomer 3 are separately introduced into the reaction system and introduced into the reaction system. 90% by weight or more of each of the total amount of the liquid A and the liquid B is introduced into the reaction system in parallel, and copolymerization is performed. This production method can suppress the occurrence of cross-linking (high molecular weight, gelation) even if a raw material containing a diester is used, can stably produce a polymer with good reproducibility, and the hydraulic composition of the phosphate ester polymer. This production method is extremely advantageous in the field of hydraulic compositions because it can maintain excellent performance as a physical dispersant.

  The phosphoric acid ester polymer according to the present invention is represented by the monomer 1 having an oxyalkylene group represented by the general formula (1) and the general formulas (2) and (3) having a phosphoric acid group. It is a polymer obtained by copolymerizing the monomers 2 and 3 to be produced.

  Preferable monomers 1 to 3 used in the present invention are as follows, and commercially available products and reaction products can also be used.

[Monomer 1]
For monomer 1, R ³ in general formula (1) is preferably a hydrogen atom, and AO is preferably an oxyalkylene group having 2 to 4 carbon atoms, and more preferably contains an ethyleneoxy group (hereinafter referred to as EO group). The EO group is 70 mol% or more, more preferably 80 mol% or more, more preferably 90 mol% or more, and particularly preferably all AO is an EO group in the total AO. X is preferably a hydrogen atom or an alkyl group having 1 to 18, more preferably 1 to 12, further 1 to 4, and 1 or 2 carbon atoms, and particularly preferably a methyl group. Specific examples include ω-methoxypolyoxyalkylene methacrylate and ω-methoxypolyoxyalkylene acrylate, and ω-methoxypolyoxyalkylene methacrylate is more preferable. Here, n in the formula (1) is the average added mole number. In terms of dispersibility of the polymer in the hydraulic composition and the effect of imparting viscosity, n is 3 to 200, preferably 4 to 120. In addition, AO is different among n repeating units on average, and random addition, block addition, or a mixture thereof may be included. AO can also contain a propyleneoxy group etc. besides EO group.

[Monomer 2]
Examples of the monomer 2 include phosphoric acid monoesters of organic hydroxy compounds. Specific examples include polyalkylene glycol mono (meth) acrylate acid phosphates. For example, phosphoric acid mono-[(2-hydroxyethyl) methacrylic acid] ester, phosphoric acid mono-[(2-hydroxyethyl) acrylic acid ester] and the like can be mentioned. Among these, phosphoric acid mono-[(2-hydroxyethyl) methacrylic acid] ester is preferable from the viewpoint of ease of production and product quality stability.

[Monomer 3]
Examples of the monomer 3 include phosphoric acid diesters of organic hydroxy compounds. Specific examples include polyalkylene glycol di (meth) acrylate acid phosphoric acid diester. Examples include phosphoric acid di-[(2-hydroxyethyl) methacrylic acid] ester, phosphoric acid di-[(2-hydroxyethyl) acrylic acid] ester, and the like. Among these, di-[(2-hydroxyethyl) methacrylic acid] ester phosphate is preferable from the viewpoint of ease of production and quality stability of the product.

  Any of the monomers 2 and 3 may be a salt, and may be an alkali metal salt, alkaline earth metal salt, ammonium salt, alkylammonium salt or the like of these compounds.

  M1 of the monomer 2 and m2 and m3 of the monomer 3 are each preferably 1 to 20, more preferably 1 to 10, and particularly preferably 1 to 5.

  Moreover, in the manufacturing method of this invention, the mixed monomer containing the monomer 2 and the monomer 3 can be used.

  As the mixed monomer containing the monomer 2 and the monomer 3, a commercial product containing a monoester and a diester can be used. For example, Phosmer M, Phosmer PE, Phosmer P ( Unichemical), JAMP514, JAMP514P, JMP100 (all Johoku Chemical), light ester P-1M, light acrylate P-1A (all Kyoeisha Chemical), MR200 (Daihachi Chemical), Kayamar (Nippon Kayaku), Ethyleneglycol methacrylate Available as phosphate (Aldrich reagent).

Moreover, the mixed monomer containing the monomer 2 and the monomer 3 is, for example, an organic hydroxy compound represented by the general formula (4), phosphoric anhydride (P ₂ O ₅ ), and water in a predetermined charging ratio. Can be produced as a reaction product.

[Wherein, R ¹⁰ represents a hydrogen atom or a methyl group, R ¹¹ represents an alkylene group having 2 to 12 carbon atoms, and m4 represents a number of 1 to 30. ]

  That is, a phosphate ester obtained by reacting the organic hydroxy compound represented by the general formula (4) with a phosphorylating agent can be used.

  1-20 are preferable, as for m4 in General formula (4), 1-10 are more preferable, and 1-5 are especially preferable.

  This phosphate ester is obtained by phosphorylating the organic hydroxy compound represented by the general formula (4) with a phosphorylating agent.

  Examples of the phosphorylating agent include orthophosphoric acid, phosphorus pentoxide (anhydrous phosphoric acid), polyphosphoric acid, phosphorus oxychloride and the like, and orthophosphoric acid and phosphorus pentoxide are preferable. These may be used alone or in combination of two or more. Further, the phosphorylating agent described below [hereinafter referred to as phosphorylating agent (Z)] is also preferable. In this invention, the quantity of the phosphorylating agent at the time of making an organic hydroxy compound and a phosphorylating agent react can be determined timely according to the target phosphate ester composition.

  In the phosphate ester, the ratio of the organic hydroxy compound and the phosphorylating agent defined by the following formula (I) is 2.0 to 4.0, more preferably 2.5 to 3.5, and particularly 2.8 to 3. What was obtained by making it react on the conditions of 2 is preferable.

In the present invention, in the formula (I), the phosphorylating agent is treated as P ₂ O ₅ .n (H ₂ O) for convenience.

In particular, the phosphorylating agent is preferably phosphorous pentoxide (Z-1) and phosphorylating agent (Z) containing at least one (Z-2) selected from the group consisting of water, phosphoric acid and polyphosphoric acid. In formula (I), a phosphorylating agent (Z) containing phosphorus pentoxide (Z-1) and at least one (Z-2) selected from the group consisting of water, phosphoric acid and polyphosphoric acid, For convenience, it will be treated as P ₂ O ₅ .n (H ₂ O).

Further, the number of moles of the phosphorylating agent defined by the formula (I) means the amount of phosphorous agent introduced into the reaction system as a raw material, particularly the amount of P ₂ O ₅ units derived from the phosphorylating agent (Z) (mole). ). The number of moles of water indicates the amount (mole) of water (H ₂ O) derived from the phosphorylating agent (Z) introduced into the reaction system as a raw material. That is, the reaction system includes water when polyphosphoric acid is represented as (P ₂ O ₅ .xH ₂ O) and orthophosphoric acid is represented as [1/2 (P ₂ O ₅ .3H ₂ O)]. It will contain all the water present in it.

  Moreover, 20-100 degreeC is preferable and, as for the temperature at the time of adding a phosphorylating agent to an organic hydroxy compound, 40-90 degreeC is more preferable. The time required for adding the phosphorylating agent to the reaction system (the time from the start of addition to the end of addition) is preferably 0.1 hour to 20 hours, and more preferably 0.5 hour to 10 hours.

  The temperature of the reaction system after adding the phosphorylating agent is preferably 20 to 100 ° C, more preferably 40 to 90 ° C. The copolymerization can be performed based on the above-described method for producing a phosphate ester polymer.

  After completion of the phosphorylation reaction, the resulting phosphoric acid condensate (an organic compound or a phosphoric acid having a pyrophosphate bond) may be reduced by hydrolysis, or even without hydrolysis, the phosphoric acid of the present invention. It is suitable as a monomer for producing an ester polymer.

  Monomers 2 and 3 are phosphoric acid esters of monomers having unsaturated bonds and hydroxyl groups, and the above-mentioned commercially available products and reaction products include monoester (monomer 2) and diester ( It has been confirmed that it contains compounds other than monomer 3). These other compounds are considered to be a mixture of polymerizable and non-polymerizable compounds, but in the present invention, such a mixture (mixed monomer) can be used as it is.

The contents of monomers 2 and 3 in the mixed monomer can be calculated based on ³¹ P-NMR measurement results.
< ³¹ P-NMR measurement conditions>
・ Inverse-gated-decoupling method
・ Measurement range: 6459.9Hz
・ Pulse delay time 30sec
Observation data point 10336
・ Pulse width (5.833μsec) 35 ° pulse ・ Solvent CD ₃ OH (deuterated methanol) (30% by weight)
・ Number of integration 128

  Under these conditions, the signal of the obtained chart belongs to the following compound, so that it is possible to determine the relative quantitative ratio from the area ratio.

For example, when the organic hydroxy compound is a phosphorous oxide of “2-hydroxyethyl methacrylate”, it can be assigned as follows.
・ 1.8ppm to 2.6ppm: phosphoric acid ・ 0.5ppm to 1.1ppm: Monomer 2 (monoester)
-0.5 ppm to 0.1 ppm: monomer 3 (diester form)
-1.0 ppm to -0.6 ppm: Triester form -11.1 ppm to -10.9 ppm, -12.4 ppm to -12.1 ppm: Pyrophosphate monoester --12.0 ppm to -11.8 ppm: Pyrophosphate diester -11.2 ppm to -11.1ppm: pyrophosphoric acid, other peaks: unknown

  In the present invention, the phosphoric acid content in the mixed monomer is quantified to determine the ratio of the monomer 2 and the monomer 3 in the mixed monomer. Specifically, the calculation is performed as follows.

The absolute amount (% by weight) of the phosphoric acid content in the sample is determined by gas chromatography. ^Since the relative molar ratio of phosphoric acid, mono-isomer, and di-isomer in the sample can be obtained from the ³¹ P-NMR result, the absolute amount of mono-isomer and di-isomer is calculated based on the absolute amount of phosphoric acid.

[Phosphoric acid content]
The conditions for gas chromatography are as follows.
Sample: Methylation with diazomethane Example) Methylation by adding 1 to 1.5 cc of diazomethane in diethyl ether to 0.1 g of sample Column: Ultra ALLOY, 15 m × 0.25 mm (inner diameter) × 0.15 μmdf
Carrier gas: He, split ratio 50: 1
Column temperature: 40 ° C. (5 min) (hold) → 10 ° C./min (temperature rise) → 15 min after reaching 300 ° C. Hold inlet temperature: 300 ° C.
Detector temperature: 300 ° C
Under the above conditions, a phosphate-derived peak is detected around 9 minutes, and the phosphate content in the unknown sample can be calculated by a calibration curve method.

  From the viewpoint of fluidity and viscosity reduction, it is better to use a mixture of phosphate esters containing a large amount of monoester, but even if it contains a large amount of diester, By controlling the polymerization molar ratio, fluidity and viscosity reduction can be adjusted.

  In the copolymerization of the monomers, the molar ratio between the monomer 1 and the monomers 2 and 3 is as follows: monomer 1 / (monomer 2 + monomer 3) = 5/95 to 95/5 Furthermore, 10/90 to 90/10 are preferable. The molar ratio of monomer 1, monomer 2 and monomer 3 is as follows: monomer 1 / monomer 2 / monomer 3 = 5 to 95/3 to 90/1 to 80 / (this Means that the monomer 1 is 5 to 95, the monomer 2 is 3 to 90, and the monomer 3 is 1 to 80 (the total is 100), and further 5 to 96/3 80 / 1-60 are preferred. In addition, about the monomer 2 and the monomer 3, the molar ratio and mol% shall be calculated based on an acid type compound (hereinafter the same).

Moreover, in this invention, the ratio of the monomer 3 can be 1-60 mol% in all the monomers used for reaction, and also can be 1-30 mol%.
Further, the molar ratio of the monomer 2 and the monomer 3 can be set to monomer 2 / monomer 3 = 99/1 to 4/96, and more preferably 99/1 to 5/95.

Hereinafter, more preferable production conditions will be described from the viewpoints of gelation suppression, adjustment of a suitable molecular weight, and performance design of a dispersant for hydraulic composition. From this point of view, in the present invention, at the time of copolymerization, 4 mol% or more, further 6 mol% or more, particularly 8 mol% or more of the chain transfer agent is added to the total number of moles of monomers 1 to 3. It is preferable to use it. Further, the upper limit of the amount of chain transfer agent used is preferably 100 mol% or less, more preferably 60 mol% or less, still more preferably 30 mol% or less, particularly preferably based on the total number of moles of monomers 1 to 3. May be 15 mol% or less. For more details,
(1) When n of monomer 1 is 3 to 30,
(1-1) When the molar ratio of the monomer 2 and the monomer 3 in the monomers 1 to 3 is 50 mol% or more, the chain transfer agent is 6 to It is preferable to use 100 mol%, in particular 8 to 60 mol%,
(1-2) When the molar ratio of the monomer 2 and the monomer 3 in the monomers 1 to 3 is less than 50 mol%, the chain transfer agent is 4 to 4 with respect to the monomers 1 to 3. It is preferable to use 60 mol%, in particular 5 to 30 mol%,
(2) When n of monomer 1 exceeds 30, the chain transfer agent is preferably used in an amount of 6 to 50 mol%, particularly 8 to 40 mol%, based on monomers 1 to 3.

  As the chain transfer agent, those described later can be used, and it is preferable that the chain transfer agent is introduced into the reaction system as a solution, preferably in a mixed solution containing the monomers 1 to 3. The amount to be contained in the mixed solution may be all or a part of the final charged amount, but it is preferable to contain the whole amount.

  In the production method of the present invention, the reaction rate of the monomers 2 and 3 is preferably 60% or more, more preferably 70% or more, further 80% or more, further 90% or more, and particularly preferably 95% or more. The amount of transfer agent used can be selected from this viewpoint. Here, the reaction rate of the monomers 2 and 3 is calculated by the following equation.

In addition, the ratio (mol%) of the monomer 2 and the monomer 3 in the phosphorus-containing compound in the reaction system at the start of the reaction and at the end of the reaction can be calculated based on the measurement result of ¹ H-NMR. .

  In the production of the phosphate ester polymer according to the present invention, in addition to the monomers 1 to 3, other monomers capable of copolymerization may be used. Examples of the other copolymerizable monomer include sulfonic acid or carboxylic acid having an unsaturated group, and salts thereof. For example, allyl sulfonic acid, methallyl sulfonic acid, alkali metal salt, alkaline earth metal salt, ammonium salt, or amine salt of any of these can be mentioned. In addition, acrylic monomers such as acrylic acid, methacrylic acid, crotonic acid, maleic acid, fumaric acid, itaconic acid, citraconic acid, and the like, and any one or more of alkali metal salts, alkalis Anhydrous compounds such as earth metal salts, ammonium salts, amine salts, methyl esters, ethyl esters and maleic anhydride may also be used. Furthermore, (meth) acrylamide, N-methyl (meth) acrylamide, N, N-dimethyl (meth) acrylamide, 2- (meth) acrylamide-2-metasulfonic acid, 2- (meth) acrylamide-2-ethanesulfonic acid, Examples include 2- (meth) acrylamide-2-propanesulfonic acid, styrene, styrenesulfonic acid and the like. The total proportion of monomers 1 to 3 in all monomers is preferably 30 to 100 mol%, more preferably 50 to 100 mol%, and particularly preferably 75 to 100 mol%. From the viewpoint of achieving the performance as a dispersant described in the coalescence, it is more than 95 mol% to 100 mol%, and more preferably 97 to 100 mol%. Other monomers that can be copolymerized can be contained in the mixed solution and introduced into the reaction system, introduced into the reaction system separately from the mixed solution, or further combined into the reaction system. Also, any of them may be used.

  The total amount of the monomers 1, 2, 3 in the reaction system and other monomers copolymerizable is preferably 5 to 80% by weight, more preferably 10 to 65% by weight in the reaction system, and 20 to 50% by weight. Is particularly preferred.

  In the production method of the present invention, the reaction temperature of the monomers 1 to 3 is preferably 40 to 100 ° C., more preferably 60 to 90 ° C., and the reaction pressure is 101.3 to 111.5 kPa (1 to 1.1 atm) as a gauge pressure. ) And 101.3-106.4 kPa (1-1.05 atm).

  In the present invention, it is preferable to react the monomer 1, the monomer 2 and the monomer 3 at a pH of 7 or less from the viewpoint of preventing gelation. In the present invention, the pH at 20 ° C. of the reaction solution collected during the reaction (from the start of the reaction to the end of the reaction) is defined as the pH during the reaction. Usually, the reaction may be started under conditions that clearly show that the pH during the reaction is 7 or less (monomer ratio, solvent, other components, etc.).

  When the reaction system is non-aqueous, it can be measured by adding an amount of water capable of measuring pH to the reaction system.

  In the present invention, the liquid A containing the monomer 1 and the liquid B containing the monomers 2 and 3 are introduced into the reaction system and used for the copolymerization reaction. Liquid A and liquid B are separately introduced into the reaction system. Further, 90% by weight or more of each of the total amount of the liquid A and the liquid B introduced into the reaction system is introduced into the reaction system in parallel. The introduction into the reaction system in parallel in the present invention means that the liquid A and the liquid B are simultaneously introduced into the reaction system from different inlets. Specific examples of the method of introducing the liquid A and the liquid B into the reaction system include dropping and spraying, and the dropping is preferable from the viewpoint of the viscosity of the liquid A and the liquid B. The liquid A is preferably a solvent containing water from the viewpoint of the freezing point, and the liquid B is preferably a solvent not containing water from the viewpoint of hydrolysis. The distance between the liquid A nozzle (introduction port) and the liquid B nozzle (introduction port) can be set arbitrarily. Moreover, although dripping can be carried out in air or in liquid, air dripping is preferred from the viewpoint of introducing all of the liquid. The nozzle diameter is preferably smaller from the viewpoint of increasing the surface area of the droplet and the solubility. Thus, by introducing the liquid A and the liquid B separately into the reaction system, the opportunity of contact of the monomer 2 and the monomer 3 with water is reduced and hydrolysis is suppressed. Moreover, the copolymer in which each monomer was introduce | transduced at random is obtained by introduce | transducing into the reaction system in parallel 90% or more of the total amount of the liquid A and the liquid B respectively introduced into the reaction system. In other words, 90% by weight or more of the total amount of the liquid A and the liquid B means that the amount of the liquid A and the amount of the liquid B introduced independently into the reaction system are the total amount and the liquid A of the liquid A introduced into the reaction system. Each of the total amount of B is less than 10% by weight.

  In the copolymerization reaction, the pH during the reaction is preferably 7 or less in consideration of other conditions. For this reason, it is preferable that pH of a mixed solution is 7 or less. Further, the pH may temporarily exceed 7 in the initial stage of the reaction as long as it does not affect the entire reaction, such as no gel is formed.

  The pH of the reaction system can be adjusted using an inorganic acid (phosphoric acid, hydrochloric acid, nitric acid, sulfuric acid, etc.), sodium hydroxide, potassium hydroxide, triethanolamine, or the like, if necessary.

  In the present invention, the pH of the liquid A and the liquid B is preferably 7 or less in order to make the pH of the reaction system during the reaction 7 or less. Here, the liquid A and the liquid B are preferably a water-containing system (that is, the solvent contains water) for pH measurement, but in the case of a non-aqueous system, a necessary amount of water may be added and measured. good. From the viewpoint of uniformity of the mixed solution, prevention of gelation, and suppression of performance degradation, the pH is 7 or less, preferably 0.1 to 6, and more preferably 0.2 to 4.5.

  The pH of the reaction system (polymerization system) before the reaction in which the monomer is finally introduced is 20 ° C. from the viewpoint of stability when controlling the molecular weight of the polymer and ease of pH control during the reaction. It is preferably 6 or less, more preferably 5 or less, still more preferably 4 or less, and particularly preferably 2 or less. Preferably, the pH of the mixed solution (the pH of the reaction system at the start of the reaction), the pH of the reaction system during the reaction, and the pH of the reaction system at the end of the reaction are all 7 or less.

[Chain transfer agent]
The chain transfer agent has a function of causing a chain transfer reaction in radical polymerization (a reaction in which a growing polymer radical reacts with another molecule to move a radical active site). It is a substance to be added. The chain transfer agent is preferably contained in the liquid A from the viewpoint of solubility and uniform mixing.

  Examples of the chain transfer agent include thiol chain transfer agents and halogenated hydrocarbon chain transfer agents, and thiol chain transfer agents, particularly water-soluble thiol chain transfer agents are preferred.

As the thiol chain transfer agent, those having a —SH group are preferable, and in particular, the general formula HS—R—Eg (wherein R represents a hydrocarbon-derived group having 1 to 4 carbon atoms, and E is − OH, —COOM, —COOR ′ or —SO ₃ M group, M represents a hydrogen atom, monovalent metal, divalent metal, ammonium group or organic amine group, and R ′ represents an alkyl having 1 to 10 carbon atoms. In which g represents an integer of 1 to 2, for example, mercaptoethanol, thioglycerol, thioglycolic acid, 2-mercaptopropionic acid, 3-mercaptopropionic acid, thiomalic acid, Examples include octyl thioglycolate, octyl 3-mercaptopropionate, and the like from the viewpoint of chain transfer effect in a copolymerization reaction including monomers 1 to 3. Mercaptoethanol are preferable, more preferably mercaptopropionic acid. These 1 type (s) or 2 or more types can be used.

  Examples of the halogenated hydrocarbon chain transfer agent include carbon tetrachloride and carbon tetrabromide.

  Examples of other chain transfer agents include α-methylstyrene dimer, terpinolene, α-terpinene, γ-terpinene, dipentene, 2-aminopropan-1-ol and the like. A chain transfer agent can use 1 type (s) or 2 or more types.

[Polymerization initiator]
In the production method of the present invention, it is preferable to use a polymerization initiator from the viewpoint of polymerization efficiency such as initiation of polymerization, improvement of reaction rate, shortening of polymerization time and the like. The polymerization initiator is preferably used in an amount of 5 mol% or more, more preferably 7 to 50 mol%, particularly preferably 10 to 30 mol%. The polymerization initiator is preferably introduced into the reaction system separately from the mixed solution. Moreover, it is preferable to introduce | transduce into a reaction system separately from the liquid A and the liquid B in parallel with the liquid A and the liquid B from a viewpoint of the polymerization reaction prevention suppression before reaction system introduction, and the structure of the polymer obtained.

  As an aqueous polymerization initiator, persulfuric acid ammonium salt or alkali metal salt or hydrogen peroxide, 2,2′-azobis (2-amidinopropane) dihydrochloride, 2,2′-azobis (2-methylpropionamide) Water-soluble azo compounds such as dihydrate are used. In addition, an accelerator such as sodium bisulfite and an amine compound can be used in combination with the polymerization initiator.

[Reaction system solvent]
The production method of the present invention is carried out by a solvent polymerization method. Examples of the solvent used at that time include water-soluble organic solvents such as water, methyl alcohol, ethyl alcohol, isopropyl alcohol acetone, and methyl ethyl ketone. In view of handling and reaction equipment, water is preferred. In particular, when an aqueous solution is used, a monomer solution containing monomer 2 and / or monomer 3 is used for the reaction at a pH of 7 or less, further 0.1 to 6, particularly 0.2 to 4, and a copolymerization reaction is performed. It is preferable to perform it from the viewpoint of uniformity (handleability) of the monomer mixture, monomer reaction rate, and crosslinking by hydrolysis of the pyro compound of the phosphoric acid compound. In the production method of the present invention, the polymerization solvent is preferably used in a ratio of 0.1 to 5 times by weight, particularly 0.5 to 4 times by weight, based on the total weight of the monomers.

  In the production method of the present invention, the liquid A containing the monomer 1 and the liquid B containing the monomer 2 and the monomer 3 are prepared separately. That is, the present invention is a production method in which the polymerization reaction is carried out while suppressing contact with water as much as possible until the liquid B is introduced (dropped) into the reaction system. A manufacturing method in which all monomers are mixed in advance and dropped and polymerized as a mixed monomer is also conceivable. However, from the viewpoint of the freezing point, the monomer 1 is often handled as an aqueous solution. When the mixed solution of monomer 2 and monomer 3 comes into contact before the start of polymerization, the phosphate ester is hydrolyzed, and depending on the environment (temperature, contact time with water, etc.) The coalescence has a low purity, and its performance as a dispersant for a hydraulic composition tends to decrease. Therefore, in the present invention, liquid A and liquid B are separately introduced into the reaction system from the viewpoint of suppressing hydrolysis of the phosphate ester. Note that the liquid A and the liquid B may be mixed while being introduced into the reaction system as long as the influence of the water contact is small or the contact is short. For example, the dropped liquid A and liquid B may be introduced into the reaction system in a state of being mixed and mixed before reaching the reaction solvent.

  Furthermore, from the viewpoint of a copolymerization reaction, 90% by weight or more of the total amount of the liquid A and the liquid B introduced into the reaction system is introduced into the reaction system in parallel. Preferably, 95% by weight or more, more preferably 98% by weight or more of each of the total amount of liquid A and liquid B introduced into the reaction system is introduced into the reaction system in parallel. Further, it is particularly preferable that the introduction is substantially 100% by weight, that is, the introduction is started at the same time and the introduction is finished at the same time.

  In addition, the introduction rate of the liquid A and the liquid B into the reaction system is constantly supplied from the start of introduction to the end of introduction for the purpose of obtaining a copolymer having the same composition (polymerization molar ratio of the copolymer) with high purity. It is preferable to do. Also, the purpose is to produce a copolymer having a wide distribution of the copolymerization ratio by varying the introduction speed of at least one of liquid A and liquid B at least twice from the start of introduction to the end of introduction, and controlling it. In this case, it is more preferable from the viewpoint that characteristics can be found in the obtained performance (for example, compatibility between low viscosity and retention). Further, it is preferable that the introduction speed of at least one of the liquid A and the liquid B is changed at least twice from the start of introduction to the end of introduction, and the fluctuation of the introduction speed is performed in the range of 50 to 150% of the average introduction speed. Further, it is preferable not to perform the next fluctuation for a time corresponding to 5% or more of the time from the start of introduction to the end of introduction after the fluctuation.

  Here, the average introduction speed is a concept of the amount of liquid A or liquid B that is introduced into the reaction system in parallel, and is calculated based on the time required from the start of introduction into the reaction system to the end of introduction. The amount of monomer introduced per unit time (% by weight relative to the total weight of monomers in liquid A or liquid B). Usually, the unit is weight% / min.

  The liquid A and the liquid B each preferably have a viscosity at 20 ° C. in the range of 50 to 6000 mPa · s from the viewpoint of introduction (for example, dropping) into the reaction system and workability. The viscosity is measured with a B-type rotational viscometer (rotation speed: 30 rpm, rotor Nos. 1 to 4 are appropriately used corresponding to the viscosity). In order to obtain such a viscosity, the liquid A is preferably adjusted by diluting with water. The content of water in the liquid A is preferably 10% by weight or more in the liquid A, and more preferably 30% by weight or more. In the case of the liquid B, it is preferable to add a nonaqueous solvent and make the viscosity in 20 degreeC into the range of 50-6000 mPa * s from a viewpoint of hydrolysis suppression of phosphate ester. Furthermore, the viscosity of the liquid B is preferably 50 to 5500 mPa · s, more preferably 100 to 5000 mPa · s, from the viewpoint of uniform solubility or workability when introducing the reaction system.

  Examples of the non-aqueous solvent for adjusting the viscosity of the liquid B include lower alcohols such as methanol, ethanol and isopropanol, organic solvents such as hexane, acetone, toluene, methyl ethyl ketone, dimethoxyethane and tetrahydrofuran, low-viscosity esters, Examples include lower alcohol alkylene oxide adducts (average number of added alkylene oxides of 2 to 10) that are raw materials of body 1, and from the viewpoint of volatility, addition of methyl diglycol or methanol ethylene oxide (hereinafter referred to as EO) A product (EO average added mole number of 3 to 10) is more preferable. The content of water in the liquid B is preferably 10% by weight or less in the liquid B. Moreover, it is preferable not to add water using only a non-aqueous solvent.

  Further, the temperature at the time of introducing the liquid A and the liquid B is preferably 20 to 60 ° C. from the viewpoint of uniform solubility or dispersibility at the time of introducing the reaction system.

  The concentration of the monomer 1 in the liquid A and the concentrations of the monomer 2 and the monomer 3 in the liquid B may be appropriately adjusted depending on the introduction time, the reaction apparatus, and the like.

  In an industrial polymerization reaction, the transition metal ions may be mixed into the reaction system from monomer raw materials, diluted water, or from raw material storage tanks, reaction tanks, piping corrosion, etc. Prediction is very difficult. For this reason, in this invention, it is preferable to superpose | polymerize in presence of a chelating agent.

  An example of the manufacturing method of this invention is shown. A predetermined amount of water is charged into a reaction vessel, the atmosphere is replaced with an inert gas such as nitrogen, and the temperature is raised. Liquid A in which monomer 1 and chain transfer agent are mixed and dissolved in water, liquid B in which monomer 2 and monomer 3 are mixed and dissolved in a non-aqueous solvent, and polymerization start in which a polymerization initiator is dissolved in water An agent solution is prepared and dripping is simultaneously started in the reaction vessel. Furthermore, dripping controls dripping speed over 0.5 to 5 hours, and completes dripping of liquid A and liquid B simultaneously. The temperature of the mixed solution waiting for dripping is maintained at 20 to 60 ° C.

  At that time, the pH of the reaction system is preferably 7 or less from the viewpoint of uniformity of the monomer solution, prevention of gelation, and suppression of performance degradation. Further, the copolymerization reaction is preferably performed with an alkali agent or the like while maintaining the pH at 7 or less, and preferably aging is performed for a predetermined time. The polymerization initiator may be added dropwise at the same time as the mixed solution or may be added in portions, but it is preferable to add in portions in terms of reducing unreacted monomers. For example, in the total amount of the polymerization initiator to be finally used, 1/2 to 5/6 polymerization initiator is added simultaneously with the mixed solution, and the remainder is added after aging for 1-2 hours after completion of the dropwise addition of the mixed solution. It is preferable. If necessary, it is further neutralized with an alkali agent (such as sodium hydroxide) after completion of ripening to obtain the phosphate ester polymer according to the present invention. The phosphate ester polymer obtained by the production method of the present invention can be used as a dispersant for a hydraulic composition even in an acid form, but from the viewpoint of suppressing hydrolysis of an ester due to acidity, it is based on an alkali. Preference is given to the salt form by neutralization. Examples of the alkali include alkali metal salts or hydroxides of alkaline earth metals, ammonia, mono-, di-, and trialkanol (preferably having 2 to 6 carbon atoms) amines.

  The phosphate ester polymer described below is obtained by the method for producing a phosphate ester polymer of the present invention.

  That is, the liquid A containing the monomer 1 and the liquid B containing the monomer 2 and the monomer 3 are separately introduced into the reaction system, and then introduced into the reaction system. It is a phosphate ester polymer obtained by a method for producing a phosphate ester polymer in which 90% by weight or more of each of the total amount of A and liquid B is introduced into the reaction system in parallel.

  The phosphate ester polymer of the present invention preferably has a weight average molecular weight (hereinafter referred to as Mw) of 10,000 to 150,000. Mw is 10,000 or more, preferably 12,000 or more, more preferably 13,000 or more, more preferably 14,000 or more, and particularly preferably 15,000 from the viewpoint of the expression of the dispersion effect and the viscosity reduction effect. From the viewpoints of high molecular weight by crosslinking, suppression of gelation and performance, from the viewpoint of dispersion effect and viscosity reduction effect, it is 150,000 or less, preferably 130,000 or less, more preferably 120,000 or less, more Preferably it is 110,000 or less, Especially preferably, it is 100,000 or less, From the both viewpoints, Preferably it is 12,000-130,000, More preferably, it is 13,000-120,000, More preferably, it is 14,000. To 110,000, particularly preferably 15,000 to 100,000. It is preferable to have Mw in this range and Mw / Mn is 1.0 to 2.6. Here, Mn is a number average molecular weight.

  Mw / Mn of the phosphoric ester polymer of the present invention as described above is 1.0 or more from the viewpoint of ensuring practical production ease, dispersibility, viscosity reduction effect, and versatility with respect to materials and temperature. From the viewpoint of achieving both a dispersibility and a viscosity reducing effect, it is 2.6 or less, preferably 2.4 or less, more preferably 2.2 or less, still more preferably 2.0 or less, and particularly preferably 1. From the viewpoint of combining the above two points, it is preferably 1.0 to 2.4, more preferably 1.0 to 2.2, more preferably 1.0 to 2.0, and particularly preferably 1. 0.0 to 1.8.

Mw and Mn of the phosphate ester polymer of the present invention are those measured by gel permeation chromatography (GPC) method under the following conditions. In addition, Mw and Mn of the phosphate ester-type polymer in this invention shall be computed based on the peak of this polymer.
[GPC conditions]
Column: G4000PWXL + G2500PWXL (Tosoh)
Eluent: 0.2M phosphate buffer / CH ₃ CN = 9/1
Flow rate: 1.0mL / min
Column temperature: 40 ° C
Detection: RI
Sample size: 0.2mg / mL
Reference material: Polyethylene glycol equivalent

  Further, in the chart pattern showing the molecular weight distribution obtained by the GPC method under the above conditions, the area having a molecular weight of 100,000 or more is 5% or less of the total area of the chart, so that dispersibility (required addition amount reduction) It is more preferable in terms of the viscosity reducing effect.

<< Dispersant for hydraulic composition >>
The phosphate ester polymer of the present invention can be used as a dispersant for a hydraulic composition in various inorganic hydraulic powders that exhibit curability by a hydration reaction, including various cements. The dispersant for a hydraulic composition containing the polymer of the present invention may be powdery or liquid. In the case of a liquid form, those using water as a solvent or a dispersion medium (such as an aqueous solution) are preferable from the viewpoint of workability and reduction of environmental load. In the dispersant of the present invention, the content of the polymer of the present invention is preferably 10 to 100% by weight, more preferably 15 to 100% by weight, and still more preferably 20 to 100% by weight in the solid content. In the case of a liquid, the solid content concentration is preferably 5 to 40% by weight, more preferably 10 to 40% by weight, and still more preferably 20 to 35% by weight, from the viewpoints of manufacturability and workability. Further, the dispersant of the present invention may be used in a ratio of 0.02 to 1 part by weight and 0.04 to 0.4 part by weight in solid content concentration of the polymer with respect to 100 parts by weight of the hydraulic powder. From the viewpoint of dispersion effect.

  Examples of the cement include ordinary Portland cement, early-strength Portland cement, ultra-early-strength Portland cement, and eco-cement (for example, JIS R5214). As hydraulic powder other than cement, blast furnace slag, fly ash, silica fume and the like may be included, and non-hydraulic limestone fine powder and the like may be included. Silica fume cement or blast furnace cement mixed with cement may be used.

  The dispersant for hydraulic composition of the present invention can also contain other additives (materials). For example, resin soap, saturated or unsaturated fatty acid, sodium hydroxystearate, lauryl sulfate, alkylbenzene sulfonic acid (salt), alkane sulfonate, polyoxyalkylene alkyl (phenyl) ether, polyoxyalkylene alkyl (phenyl) ether sulfate (salt) ), Polyoxyalkylene alkyl (phenyl) ether phosphates (salts), protein materials, AE agents such as alkenyl succinic acid and α-olefin sulfonate; oxy such as gluconic acid, glucoheptonic acid, alabonic acid, malic acid, citric acid Delayers such as carboxylic acids, dextrins, monosaccharides, oligosaccharides, polysaccharides, etc .; foaming agents; thickeners; silica sand; AE water reducing agents; calcium chloride, calcium nitrite, calcium nitrate , Cal bromide Soluble calcium salts such as um, calcium iodide, chlorides such as iron chloride and magnesium chloride, sulfates, potassium hydroxide, sodium hydroxide, carbonates, thiosulfates, formic acid (salts), alkanolamines, etc. Strongening agent or accelerator; foaming agent; waterproofing agent such as resin acid (salt), fatty acid ester, oil, fat, silicone, paraffin, asphalt, wax; blast furnace slag; fluidizing agent; dimethylpolysiloxane, polyalkylene glycol fatty acid ester Anti-foaming agents such as mineral oils, oils and fats, oxyalkylenes, alcohols, amides, etc .; antifoaming agents; fly ash; melamine sulfonic acid formalin condensates, aminosulfonic acids, polymaleic acids and other polycarboxylic acids High-performance water-reducing agent such as silica; Silica fume; Rust inhibitor such as nitrite, phosphate, zinc oxide; Methyl cellulose , Celluloses such as hydroxyethyl cellulose, natural products such as β-1,3-glucan, xanthan gum, polyacrylic acid amide, polyethylene glycol, EO adduct of oleyl alcohol, or a reaction product of this with vinylcyclohexene diepoxide, etc. Water-soluble polymers such as synthetic systems; polymer emulsions such as alkyl (meth) acrylates.

  Moreover, the dispersing agent for hydraulic compositions of the present invention is not only for ready-mixed concrete and concrete vibration products, but also for self-leveling, for refractories, for plaster, for gypsum slurry, for lightweight or heavy concrete, for AE, for repair. It is useful in any field of various concrete such as prepacked, trayy, ground improvement, grout, and cold.

<< Hydraulic composition >>
In addition, the hydraulic composition that is the target of the dispersant of the present invention has a water / hydraulic powder ratio [weight percentage (% by weight) of water and hydraulic powder in the hydraulic composition, hereinafter referred to as W / P. Is written. ] Is 65% or less, more preferably 10 to 60%, still more 12 to 57%, and particularly 15 to 55% and further 20 to 55% in that the low-viscosity effect is exhibited.

  Further, the hydraulic composition of the present invention is a paste, mortar, concrete, or the like containing a phosphate ester polymer obtained by the production method of the present invention, water and hydraulic powder (cement), You may contain an aggregate. Examples of the aggregate include fine aggregate and coarse aggregate. The fine aggregate is preferably mountain sand, land sand, river sand and crushed sand, and the coarse aggregate is preferably mountain gravel, land gravel, river gravel and crushed stone. Depending on the application, lightweight aggregates may be used. The term “aggregate” is based on “Concrete Overview” (published on June 10, 1998, published by Technical Shoin).

Example 1
《Reaction vessel》
A glass reaction vessel (four-necked flask) equipped with a stirrer was charged with 375 g of water, purged with nitrogen while stirring, and heated to 80 ° C. in a nitrogen atmosphere.
<< mixed solution (1) >>
A suitable amount of water was added to ω-methoxypolyethyleneglycol monomethacrylate (average added mole number of EO of 23) so that the effective content was 60.8% and the water content was 35%. Then, 4.5 g of 3-mercaptopropionic acid is mixed with 450 g of the monomer aqueous solution (mixing temperature 40 ° C.).
<< mixed solution (2) >>
As a non-aqueous solvent, 71.6 g of phosphoric acid ester (A), which is a mixture of phosphoric acid mono-[(2-hydroxyethyl) methacrylic acid] ester and di-[(2-hydroxyethyl) methacrylic acid] ester phosphate 3.6 g of methyl diglycol is mixed (mixed solution viscosity: 4000 mPa · s / temperature 20 ° C.) << mixing temperature 40 ° C. >>.
<Polymerization initiator solution>
Ammonium persulfate. Dissolve 8.5 g in 48 g of water.
<Conditions for introduction of dripping>
After preparing the mixed solutions (1) and (2), the mixture was held at 40 ° C. for 1 hour until the introduction of dropwise addition into the reaction vessel was started.
<Drip introduction conditions>
The mixed solutions (1) and (2) and the polymerization initiator solution were added dropwise to the reaction vessel at the same time, and the three solutions were added dropwise over 100 minutes.
The dropping speeds of the mixed solution (1) and the mixed solution (2) within the dropping time were 1% by weight / min and constant. Further, at that time, the temperature of each mixed solution was maintained at 40 ° C., which is the same temperature as the conditions until the dropwise introduction, until it was introduced into the reaction system.

  After ripening for 1 hour after completion of the dropwise addition, 1.8 g of ammonium persulfate dissolved in 10 g of water was dropped over 30 minutes, and then ripened at the same temperature (80 ° C.) for 1.5 hours. After completion of aging, the mixture was neutralized with 59 g of a 32% aqueous sodium hydroxide solution to obtain a phosphate ester polymer.

The phosphoric acid ester (A) used in this example and the following examples and comparative examples was obtained by adding 200 g of 2-hydroxyethyl methacrylate and 36.0 g of 85% phosphoric acid (H ₃ PO ₄ ) in a reaction vessel. Charge 89.1 g of diphosphorus pentoxide (phosphoric anhydride) (P ₂ O ₅ ) gradually added while cooling so that the temperature does not exceed 60 ° C, then set the reaction temperature to 80 ° C and react for 6 hours. And obtained by cooling.

Example 2
The mixing temperature of << mixed solution (1) >> is 70 ° C., the mixing temperature of << mixed solution (2) >> is 70 ° C., and methanol EO adduct (average EO added mole number: 9 mol) as a non-aqueous solvent is a phosphoric acid ester. 10% of the weight of (A) was blended (mixed solution viscosity: 4500 mPa · s / temperature 20 ° C.), << conditions until introduction of dripping >> was 70 ° C., 1.5 hours, and other conditions were the same as in Example 1. And the same.

Example 3
<< Mixed solution (2) >> as a non-aqueous solvent is blended with 8% of the weight of phosphoric acid ester (A) by adding methanol EO adduct (average EO addition mole number 6 mol) (mixed solution viscosity: 4200 mPa · s / temperature). 20 ° C.), << conditions until dripping introduction >> were set to 40 ° C. for 96 hours, and the other conditions were the same as those in Example 1.

Example 4
The raw materials (monomer and charge ratio) of the copolymer A-2 in Table 1 were used, and the amount of chain transfer agent and the amount of polymerization initiator were adjusted so that the weight average molecular weight of the resulting polymer would be 32000-38000. The other components were used in the same manner as in Example 1.

Example 5
The raw materials (monomer and charge ratio) of the copolymer A-3 in Table 1 are used, and the chain transfer agent amount and the polymerization initiator amount are set so that the weight average molecular weight of the obtained polymer is 20000 to 24000. The other components were used in the same manner as in Example 1.

Comparative Example 1
Prepare a mixed solution in which all the monomers of << Mixed Solution (1) >> and << Mixed Solution (2) >> are mixed together at a mixing temperature of 70 ° C. and no nonaqueous solvent. Conditions until introduction> were set to 70 ° C. for 1.5 hours, and the same procedure as in Example 1 was performed except that the monomer mixed solution and the polymerization initiator solution were separately dropped simultaneously into the reaction vessel.

Comparative Example 2
Prepare a mixed solution in which all the monomers of << Mixed Solution (1) >> and << Mixed Solution (2) >> are mixed together at a mixing temperature of 40 ° C. and without adding a non-aqueous solvent. Conditions until introduction> were set to 40 ° C. for 96 hours, and the same procedure as in Example 1 was performed except that the monomer mixed solution and the polymerization initiator solution were separately dropped into the reaction vessel at the same time.

Example 6
The mixing temperature of << mixed solution (1) >> is 70 ° C., the mixing temperature of << mixed solution (2) >> is 70 ° C., and << conditions until introduction of dripping >> is 70 ° C. for 1 hour. Dropping introduction conditions> were 1.35% by weight / min from the start of dropping to 30 minutes, 1.0% by weight / min from 30 minutes to 70 minutes, and 0.65% by weight / min from 70 minutes to the end of dropping (on average dropping rate). On the other hand, the conditions other than the fluctuation range of 65% to 135% were the same as those in Example 1.

Example 7
The mixed solution (1) << Drip introduction condition >> was added at 1.2 wt% / min from the start of dropping to 10 minutes, 1.0 wt% / min from 10 minutes to 90 minutes, and 0.8 wt% / min from 90 minutes to the end of dropping. The conditions were the same as in Example 1 except that min (the fluctuation range was 80% to 120% with respect to the average dropping speed).

Example 8
<< Drip introduction condition >> of the mixed solution (2) is 1.6% by weight / min from the start of dropping to 30 minutes, 1.0% by weight / min from 30 to 70 minutes, and 0.4% by weight from 70 minutes to the end of dropping. / Min (variation range 40% to 160% with respect to the average dropping rate) was the same as in Example 1.

  The examples and comparative examples described above are polymer Nos. With the charged raw materials shown in Table 1 below. It corresponds to the production of any one of A-1 to A-3. Tables 2 and 3 summarize the weight average molecular weights (Mw) and reaction rates of the phosphate ester polymers when a plurality of examples and comparative examples are performed.

The symbols in the table are as follows.
MEPEG-E: ω-methoxypolyethylene glycol monomethacrylate HEMA-MPE: phosphoric acid mono-[(2-hydroxyethyl) methacrylic acid] ester HEMA-DPE: phosphoric acid di-[(2-hydroxyethyl) methacrylic acid 〕ester

(note)
The polymerization reactions in Tables 2 and 3 were carried out by changing the day without continuously performing the first to third times, and different raw materials were used for each monomer lot. In addition, “separation dropping” means that the mixed solution (1) and the mixed solution (2) are dropped separately, and “mixing dropping” means that the mixed solution in which all the monomers are mixed is dropped. .

<Test example>
Using the phosphate ester polymer obtained by the above production method, a test was conducted on the mortar having the composition shown in Table 4. The results are shown in Tables 5 and 6. Evaluation was performed by the following methods for dispersibility and viscosity.
(1) Mortar combination

The materials used in Table 4 are as follows.
C: Ordinary cement (1: 1 mixture of ordinary Portland cement manufactured by Taiheiyo Cement Co., Ltd. and ordinary Portland cement manufactured by Sumitomo Osaka Cement Co., Ltd.)
W: Ion exchange water S: Mountain sand from Kimitsu, Chiba Prefecture
W / C: percentage by weight (% by weight) of water (W) and cement (C)

(2) Preparation of mortar Into a container (1 L stainless beaker: inner diameter 120 mm), about 1/2 amount of S of the composition shown in Table 4 is added, then C is added, and the remaining S is further added as a stirrer. Mixing of dispersant and water premixed after 200 seconds of air kneading using EYELA Z-2310 (Tokyo Rika Instruments, stirring rod: height 50 mm, inner diameter 5 mm × 6 pieces / length 110 mm) The solution was added over 5 seconds, the material between the wall and the stirring bar was scraped off for 30 seconds after the addition, and water was added and kneaded for 3 minutes to prepare a mortar. In addition, an antifoamer was added as needed, and it adjusted so that entrained air amount might be 2% or less.

(3) Evaluation (3-1) Fluidity Use of a cone having an upper opening diameter of 70 mm, a lower opening diameter of 100 mm, and a height of 60 mm, and an addition amount of a copolymer necessary for a mortar flow value to be 200 mm ( The flowability was evaluated based on 100 parts by weight of an effective part by weight of cement. In addition, 200 mm of this mortar flow value is an average value of the maximum value of the mortar flow value and the mortar flow value measured in the direction perpendicular to the length of ½ of the line segment that gives the maximum value. The smaller the amount added, the stronger the dispersibility.

(3-2) Viscosity A recorder is connected to the torque tester shown in FIG. 1, and a torque of 200 mm in mortar flow is measured. The viscosity was calculated from the torque of the mortar based on the torque-viscosity relational expression created in advance with polyethylene glycol (Mw20,000) shown in FIG. At the time of creating the torque-viscosity relational expression of polyethylene glycol, the torque output voltage value (mV) is recorded from the recorder by the monitor output 60W and the output signal DC0-5V.

(3-3) Flowability The mortar with a mortar flow of 200 mm obtained in the evaluation of the flowability in (3-1) was allowed to stand for 30 minutes, and then lightly stirred with a hand scoop. Was measured, and the difference in fluidity was regarded as an evaluation of fluidity retention.

  In Examples 1 to 5, a copolymer having a small molecular weight variation, a high reaction rate, and a high purity is obtained. Further, in the comparison of the same monomer composition (A-1), Examples 1 to 3 have good reproducibility in dispersion effect (necessary addition amount) and viscosity reduction effect (mortar viscosity) obtained in comparison with Comparative Examples 1 and 2. Similar performance was obtained. Example 4 is a polymer having a small ratio of phosphoric acid groups (monomers 2 and 3) serving as adsorption groups to the hydraulic powder and having an excellent fluid retention effect. Although the mortar viscosity immediately after kneading shows a large value, it exhibits fluidity after 30 to 60 minutes.

  In Examples 6 to 7, the average copolymer composition ratio and the weight average molecular weight are almost the same, but the distribution of the composition ratio can be widened. As a result, the obtained viscosity reducing effect (mortar viscosity) and fluid retention are obtained. Furthermore, good performance was obtained with good reproducibility.

  Furthermore, in the average introduction speed of Example 1 and Examples 6 to 8, it can be seen that the dispersion effect obtained is further improved when the fluctuation range is in the range of about 50 to 150%.

Schematic diagram of torque tester and recorder used for viscosity measurement in Examples and Comparative Examples Torque-viscosity relational expression with polyethylene glycol (Mw 20,000) used for viscosity calculation in Examples and Comparative Examples

Claims (7)

A monomer 1 represented by the following general formula (1), a monomer 2 represented by the following general formula (2), and a monomer 3 represented by the following general formula (3) are polymerized. A method for producing a phosphate ester polymer comprising:
A liquid A containing the monomer 1 and a liquid B containing the monomer 2 and the monomer 3 are separately introduced into the reaction system, respectively.
90% by weight or more of each of the total amount of liquid A and liquid B introduced into the reaction system is introduced into the reaction system in parallel.
A method for producing a phosphate ester polymer.

[Wherein R ¹ and R ² are each a hydrogen atom or a methyl group, R ³ is a hydrogen atom or —COO (AO) _n X, AO is an oxyalkylene group or oxystyrene group having 2 to 4 carbon atoms, n is It is the average added mole number of AO, the number of 3-200, X represents a hydrogen atom or a C1-C18 alkyl group. ]

[Wherein, R ⁴ represents a hydrogen atom or a methyl group, R ⁵ represents an alkylene group having 2 to 12 carbon atoms, m1 represents a number of 1 to 30, and M represents a hydrogen atom, an alkali metal or an alkaline earth metal. ]

[Wherein R ⁶ and R ⁸ are each a hydrogen atom or a methyl group, R ⁷ and R ⁹ are each an alkylene group having 2 to 12 carbon atoms, m2 and m3 are each a number from 1 to 30 and M is hydrogen. Represents an atom, an alkali metal or an alkaline earth metal. ]   The introduction speed of at least one of the liquid A and the liquid B is changed at least twice from the start of introduction to the end of introduction, and the fluctuation of the introduction speed is performed in a range of 50 to 150% of the average introduction speed. A method for producing a phosphate ester polymer.   Furthermore, the manufacturing method of the phosphate ester type polymer of Claim 1 or 2 which introduce | transduces a polymerization initiator into a reaction system in parallel with the liquid A and the liquid B.   The manufacturing method of the phosphate ester type polymer in any one of Claims 1-3 in which A liquid contains a chain transfer agent.   The method for producing a phosphate ester polymer according to any one of claims 1 to 4, wherein the liquid B contains a nonaqueous solvent, and the viscosity of the liquid B at 20 ° C is in the range of 50 to 6000 mPa · s. 6. The ratio Mw / Mn of the weight average molecular weight (Mw) and the number average molecular weight (Mn) of the resulting phosphate ester polymer is 1.0 to 2.6. A method for producing an acid ester polymer.   A hydraulic composition containing hydraulic powder, water, and a phosphate ester polymer obtained by the production method according to claim 1.

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