IMPROVED METHOD FOR PRODUCING HYDROXYL GROUP-CONTAINING VINYL ETHER POLYMER

Abstract

A method for producing a hydroxyl group-containing vinyl ether polymer according to the present invention includes: a step of radical polymerizing at least one vinyl ether selected from vinyl ether having a hydroxyl group represented by the following formula (2):

##STR00001##

wherein R.sup.7 represents an alkylene group which is straight-chained, branched or comprises an alicyclic structure, and p is 1, 2, or 3, in the presence of water as a polymerization solvent and an azo compound represented by the following formula (1) as a polymerization initiator:

##STR00002##

wherein R.sup.1 to R.sup.4 each independently represent a hydrogen atom or an alkyl group and R.sup.5 and R.sup.6 each independently represent an alkoxy group optionally having a substituent group or an alkyl amino group optionally having a substituent group.

Claims

1. A method for producing a hydroxyl group-containing vinyl ether polymer, comprising: a step of radical polymerizing at least one vinyl ether selected from vinyl ether having a hydroxyl group represented by the following formula (2). ##STR00009## wherein R.sup.7 represents an alkylene group which is straight-chained, branched or comprises an alicyclic structure, and p is 1, 2, or 3, in the presence of water as a polymerization solvent and an azo compound represented by the following formula (1) as a polymerization initiator: ##STR00010## wherein R.sup.1 to R.sup.4 each independently represent a hydrogen atom or an alkyl group and R.sup.5 and R.sup.6 each independently represent an alkoxy group optionally having a substituent group or an alkyl amino group optionally having a substituent group.

2. The method for producing a polymer according to claim 1, wherein said azo compound is an ester type azo compound and R.sup.5 and R.sup.6 in said formula (1) are each independently an alkoxy group having 1 to 4 carbon atoms.

3. The method for producing a polymer according to claim 1, wherein the amount of residual monomers in the hydroxyl group-containing vinyl ether polymer is 20 mol % or less.

4. The method for producing a polymer according to claim 1, wherein the amount of said azo compound added is from 0.01 to 1 mol % based on said vinyl ether and the number average molecular weight Mn of the hydroxyl group-containing vinyl ether polymer is from 10,000 to 600,000.

5. The method for producing a polymer according to claim 1, wherein the amount of said azo compound added is from 0.1 to 35 mol % based on said vinyl ether and the number average molecular weight Mn of the hydroxyl group-containing vinyl ether polymer is from 1,000 to 10,000.

6. A method for producing an aqueous hydroxyl group-containing vinyl ether polymer solution comprising water and a hydroxyl group-containing vinyl ether polymer, the method comprising: a step of radical polymerizing at least one vinyl ether selected from vinyl ether having a hydroxyl group represented by the following formula (2): ##STR00011## wherein R.sup.7 represents an alkylene group which is straight-chained, branched or comprises an alicyclic structure, and p is 1, 2, or 3, in the presence of water as a polymerization solvent and an azo compound represented by the following formula (1) as a polymerization initiator: ##STR00012## wherein R.sup.1 to R.sup.4 each independently represent a hydrogen atom or an alkyl group and R.sup.5 and R.sup.6 each independently represent an alkoxy group optionally having a substituent group or an alkyl amino group optionally having a substituent group; and a step of storing the obtained hydroxyl group-containing vinyl ether polymer in an aqueous solution.

7. The method for producing an aqueous polymer solution according to claim 6, wherein said azo compound is an ester type azo compound and R.sup.5 and R.sup.6 in the said formula (1) are each independently an alkoxy group having 1 to 4 carbon atoms.

8. The method for producing an aqueous polymer solution according to claim 6, wherein the amount of residual monomers in the hydroxyl group-containing vinyl ether polymer is 20 mol % or less.

9. The method for producing an aqueous polymer solution according to claim 6, wherein the amount of said azo compound added is from 0.01 to 1 mol % based on said vinyl ether and the number average molecular weight Mn of the hydroxyl group-containing vinyl ether polymer is from 10,000 to 600,000.

10. The method for producing an aqueous polymer solution according to claim 6, wherein the amount of said azo compound added is from 0.1 to 35 mol % based on said vinyl ether and the number average molecular weight Mn of the hydroxyl group-containing vinyl ether polymer is from 1,000 to 10,000.

11. An aqueous hydroxyl group-containing vinyl ether polymer solution produced from the method for producing an aqueous polymer solution according to claim 6.

12. Use of the aqueous hydroxyl group-containing vinyl ether polymer solution according to claim 11 for producing an aqueous composition used for paints, inks, adhesives, resin modifiers, metal recovery resins, compatibilizers, surfactants, dispersing agents, and binding agents.

Description

MODE FOR CARRYING OUT THE INVENTION

<Method for Producing Polymer and Aqueous Polymer Solution>

[0034] The methods for producing a polymer and an aqueous polymer solution according to the present invention are both characterized by comprising a step for radical polymerizing vinyl ether having a hydroxyl group under a certain condition. The method for producing an aqueous polymer solution is characterized by further comprising a step of storing the hydroxyl group-containing vinyl ether obtained by the radical polymerization step. Such radical polymerization step will be described in detail below.

<Polymerization Solvent>

[0035] It is essential to use water as a polymerization solvent in the present invention. An aqueous organic solvent may be used in combination to the extent that the effect of the present invention is not impaired. As used herein, aqueous means solubility in water (the amount of solute based on 100 g of water) at 25 C. is 1 g or more. The amount of water used is not particularly limited and is from 5 to 2000 parts by mass, preferably from 10 to 1000 parts by mass, based on 100 parts by mass of vinyl ether containing a hydroxyl group (hereinafter may be referred to as a monomer). The amount of water based on the total amount of the polymer solvent is from 10% by mass or more to 100% by mass or less, preferably 20% by mass or more, more preferably 50% by mass or more.

[0036] As for the above-stated aqueous solvent, there can be used, for example, monoalcohols such as methanol, ethanol, isopropanol, n-butyl alcohol, isobutyl alcohol, tert-butyl alcohol, sec-butyl alcohol, tetrahydrofurfuryl alcohol, hexafluoroisopropanol; 2-fluoroethanol, and 3,3,3-trifluoro-1-propanol; polyalcohols such as ethylene glycol, glycerin, and diethylene glycol; ether alcohols such as methyl cellosolve, cellosolve, isopropyropyl cellosolve, butyl cellosolve, ethylene glycol monomethyl ether, ethylene glycol monoethyl ether, diethylene glycol monomethyl ether, and diethylene glycol monoethyl ether; alkyl amides such as dimethylformamide, dimethylacetamide, and N-methylpyrrolidone; alkyl sulfoxides such as dimethyl sulfoxide; ketones such as acetone and methyl ethyl ketone; and cyclic ethers such as tetrahydrofuran and dioxane. These solvents may be used alone or two or more solvents may be mixed to use.

<Radical Polymerization Initiator>

[0037] It is essential in the present invention to use an azo compound represented by the following formula (1) as a radical polymerization initiator.

##STR00007##

[0038] wherein R.sup.1 to R.sup.4 each independently represent a hydrogen atom or an alkyl group and R.sup.5 and R.sup.6 each independently represent an alkoxy group optionally having a substituent group or an alkyl amino group optionally having a substituent group.

[0039] In the above-described formula (1), an alkyl group represented by R.sup.1 to R.sup.4 is preferably an alkyl group having 1 to 4 carbon atoms, in particular, a methyl group, an ethyl group, n-propyl group, isopropyl group, n-butyl group, isobutyl group, tert-butyl group, or the like. Preferably, R.sup.1 to R.sup.4 is preferably a methyl group.

[0040] In the above-described formula (1), an alkoxy group optionally having a substituent group represented by R.sup.5 and R.sup.6 is preferably an alkyl group having 1 to 4 carbon atoms, in particular, a methoxy group, an ethoxy group, n-propoxy group, isopropoxy group, n-butoxy group, isobutoxy group, sec-butoxy group, tert-butoxy group, or the like. Preferably, R.sup.5 and R.sup.6 is preferably a methyl group. An alkyl amino group optionally having a substituent group represented by R.sup.5 and R.sup.6 is preferably an alkyl amino group having 1 to 4 carbon atoms, in particular, a methyl amino group, an ethyl amino group, n-propyl amino group, isopropyl amino group, n-butyl amino group, isobutyl amino group, sec-butyl amino group, tert-butyl amino group, or the like. A substituent group in the alkoxy group and the alkyl amino group include a hydroxyl group, a methoxy group, an ethoxy group, or the like.

[0041] Such radical polymerization initiator includes, in particular, ester type azo compounds such as dimethyl 2,2-azobis(2-methylpropionate) (MAIB), dimethyl 2,2-azobis(2-methylbutyrate), and dimethyl 2,2-azobis(2-methylpentanoate); acid amide type azo compounds such as 2,2-azobis(N-butyl-2-methylpropionamide), 2,2-azobis[N-(2-propenyl)-2-methylpropionamide], and 2,2-azobis[2-methyl-N-(2-hydroxyethyl)propionamide. Amongst these, MAIB and 2,2-azobis[2-methyl-N-(2-hydroxyethyl)propionamide are preferable and MAIB is especially preferable, in view of reactivity and solubility in vinyl ether.

[0042] The amount of polymerization initiator to be used is usually set appropriately, depending on the kind and the amount of monomers to be used, the polymerization temperature, polymerization condition such as polymerization concentration, molecular weight of the polymer of interest, or the like, and the method according to the present invention allows polymerization with a smaller amount of initiator than the conventional method. For example, when a polymer having a number average molecular weight of about 10,000 to 600,000, more preferably about 10,000 to 100,000, further preferably about 10,000 to 50,000 is to be obtained, the amount of initiator to be used based on the total amount of monomers is preferably within the range from 0.01 to 1 mol %, more preferably within the range from from 0.05 to 0.5 mol %. On the other hand, when a low molecular weight polymer having a number average molecular weight of about 1,000 to 10,000, more preferably about 2,000 to 9,000, further preferably about 3,000 to 8,000 is to be obtained, an excessive amount of initiator will be used, which often results in difficulty to improve the monomer conversion rate. However, the method according to the present invention will allow reaction with a relatively small use amount of polymerization initiator (preferably from 0.1 to 35 mol %, more preferably from 1 to 20 mol %) and a high monomer conversion rate, even in the case where such low molecular weight polymer is to be obtained. The polymer has a molecular weight distribution (Mw/Mn) preferably within the range from 1.0 to 5.0, more preferably within the range from 1.0 to 4.0, further preferably within the range from 1.2 to 3.0.

<Monomer Component>

[0043] Vinyl ether containing a hydroxyl group used in the present invention is represented by the following formula (2):

##STR00008##

[0044] wherein R.sup.7 represents an alkylene group which is straight-chained, branched or comprises an alicyclic structure, and p is 1, 2, or 3.

[0045] A straight chained or branched alkylene group represented by R.sup.7 in formula (2) is preferably a straight-chained or branched alkylene group having 2 to 8 carbon atoms, in particular, an ethylene group, a 1,2-propylene group, a 1,3-propylene group, a 1,4-butylene group, a 1,5-pentylene group, a neopentylene group, a 1,6-hexylene group, a 4-methyl-2,2-pentylene group, a 3-methyl-1,5-pentylene group, a 2,3-dimethyl-2,3-butylene group, or the like, and especially preferred are an alkylene group having 2 to 4 carbon atoms such as an ethylene group, a 1,2-propylene group, a 1,3-propylene group, and a 1,4-butylene group.

[0046] An alkylene group comprising a cycloaliphatic structure represented by R.sup.7 is preferably an alkylene group having a monocyclic cycloaliphatic structure, more preferably an alkylene group having a cycloaliphatic structure with a 5 to 6 membered ring, in particular a 1,2-cyclopentylene group, a 1,3-cyclopentylene group, a 1,2-cyclohexylene group, a 1,3-cyclohexylene group, a 1,4-cyclohexylene group, a 1,2-cyclopentane dimethylene group, a 1,3-cyclopentane dimethylene group, a 1,2-cyclohexane dimethylene group, a 1,3-cyclohexane dimethylene group, a 1,4-cyclohexane dimethylene group, or the like.

[0047] Repetitive number p of an oxyalkylene group is preferably 1 or 2 in view of polymerization and p=1 is especially preferred.

[0048] Examples of vinyl ethers represented by formula (2) are 2-hydroxyethyl vinyl ether, 3-hydroxypropyl vinyl ether, propylene glycol monovinyl ether, 1-hydroxypropane-2-yl vinyl ether, 4-hydroxybutyl vinyl ether, diethylene glycol mono vinyl ether, dipropylene glycol mono vinyl ether, triethylene glycol mono vinyl ether, 4-hydroxy cyclohexyl vinyl ether, 1,4-cyclohexane dimethanol monovinyl ether, or the like. These vinyl ethers may be used alone or two or more vinyl ethers may be mixed to use.

[0049] Amongst these vinyl ethers, especially preferred are vinyl ethers comprising a straight chained alkylene group or alkylene oxy alkylene group having about 2 to 4 carbon atoms such as 2-hydroxyethyl vinyl ether, diethylene glycol monovinyl ether, 4-hydroxy butyl vinyl ether, in view of reactivity and simplicity in controlling polymerization.

<Polymerization Condition>

[0050] In the production method according to the present invention, the reaction temperature (polymerization temperature) of the polymerization step may be appropriately selected, depending on the kind of polymerization initiator, and reaction (polymerization) may be performed by changing the temperature in a stepwise manner. Generally, the temperature is preferably within the range from 50 to 180 C., more preferably from 60 to 170 C. When the reaction temperature is 50 C. or more, the reaction will be prevented from falling, and when the temperature is 180 C. or less, decomposition of the radical polymerization initiator will be prevented, and the molecular weight of the polymer to be generated which is caused by elevation of chain transfer, will be prevented from decreasing.

[0051] Polymerization method is not particularly limited, and for example, polymerization may be initiated by introducing beforehand monomers, a polymerization initiator, and a polymerization solvent if necessary in a vessel, deoxidizing the vessel, then elevating the temperature. Polymerization may also be initiated by adding the polymerization initiator in the heated monomers or monomer solution. The polymerization initiator may be added sequentially or batchwise. These may be combined or a part of the polymerization initiator may be introduced in a reactor beforehand and then the rest may be added sequentially to the reaction system. In the case of sequential addition, the operation will become complicated but it is easier to control the polymerization reaction.

[0052] Moreover, when a temperature elevation due to heat generation is in concern or when the reaction rate of multiple monomers becomes high, the monomers or the monomer solution may be added in portions or continuously. In this case, the temperature may be elevated up to the reaction temperature at the time when the monomers or a part of the monomer solution are added into the reactor, and then the rest may be added in portions or sequentially, or the solvent may be introduced in the reactor beforehand, and the monomers or the monomer solution may be added in portions or sequentially into the heated solvent. The polymerization initiator may also be introduced in the reactor beforehand, or it may be added into the reaction system together with or separately from the monomers, or a part of the polymerization initiator may be introduced in the reactor beforehand and the rest may be sequentially added to the reaction system. Such method enables to suppress the temperature elevation due to heat generation and therefore, it is easy to control the polymerization reaction.

[0053] After the completion of the reaction, the obtained hydroxyl group-containing vinyl ether polymer can be treated and isolated by well-known operations and treatment methods.

[0054] In the method of the present invention, the monomer conversion rate in the polymerization reaction is high; the monomer conversion rate being usually 80% or more, preferably 90% or more, more preferably 95% or more, furthers preferably 97% or more, further more preferably 99% or more. Consequently, the amount of residual monomers in the obtained polymers is usually 20 mol % or less, preferably 10 mol % or less, more preferably 5 mol % or less, further preferably 3 mol % or less, further more preferably 1 mol % or less, even without especially undergoing a step for removing the monomers.

[0055] Since the amount of the radical polymerization used is extremely small, it is possible to greatly reduce the residual monomers and catalyst residues in the reaction solution. Further, since generation of polyacetal is suppressed, the reaction solution can be used for a variety of applications as an aqueous hydroxyl group-containing vinyl ether polymer directly, or upon condensation or dilution. For example, the content rate of polyacetal in the polymer is preferably 10 mass % or less, more preferably 5 mass % or less, further preferably 1 mass % or less.

[0056] According to the method of the present invention, reaction can be performed efficiently with a high conversion rate of, such as the monomer conversion rate of 80% or more, even with monomers comprising a cycloaliphatic structure such as 1,4-cyclohexane dimethanol mono vinyl ether and having many carbon atoms and higher hydrophobicity.

<Application>

[0057] Specifically, such aqueous polymer solution can be used for producing an aqueous composition used for paints, inks, adhesives, resin modifiers, metal recovery resins, compatibilizers, surfactants, dispersing agents, binding agents, or the like.

EXAMPLES

[0058] The present invention will be described in more detail below by way of the examples and comparative examples; however the present invention is not interpreted by being limited to the content of the following examples.

[0059] Evaluation of the physical property of polymers that were obtained in the Examples was carried out by the following methods.

[0060] (1) Calculation of the monomer conversion rate (residual amount) and structure analysis of polymer were carried out using .sup.1H NMR (JNM ECX-500II, manufactured by JEOL Ltd.) (solvent: heavy water or heavy chloroform). The value of the residual amount of the monomers is the value measured before undergoing the step of removing the monomers.

[0061] (2) Analysis of weight average molecular weight (Mw) and molecular weight distribution (Mw/Mn) was carried out using gel permeation chromatography (GPC).

Analysis Condition

[0062] Column: TSK gel column G-MHHR-M x2 (manufactured by Tosoh Corporation) [0063] or Shodex GPC KD804 x3 (manufactured by Showa Denko K. K.)

[0064] Solvent: dimethylformamide (containing 10 mmol/L lithium bromide)

[0065] Measurement temperature: 40 C.

[0066] Flow rate: 1.0 ml/min

[0067] Standard curve: standard polystyrene standard

Example 1

Production of poly(2-hydroxyethyl vinyl ether) (1)

[0068] To a test tube, a stirring bar, 500 parts by mol of 2-hydroxyethyl vinyl ether (hereinafter, referred to as HEVE) as a monomer, and 1 mol (0.2 mol % based on a monomer) of MAIB (manufactured by Wako Pure Chemical Industries, Ltd., product name V-601) as a radical polymerization initiator were added, and further, water was added as a polymerization solvent so that the HEVE concentration will be 50 mass %, and they were well dissolved. Then, nitrogen was blown through the test tube to deoxidize. After deoxidization, the test tube was sealed and the polymerization reaction was started in an oil bath of 70 C. After 48 hours, the polymerization was terminated by cooling and exposing to air, and .sup.1H NMR analysis and GPC analysis were carried out. As a result, the monomer conversion rate was 99% or more, the number average molecular weight Mn of the obtained polymer was 33900, and the molecular weight distribution Mw/Mn was 2.45 after an elapse of 48 hours.

Example 2

Production of poly(2-hydroxyethyl vinyl ether) (2)

[0069] Polymerization reaction was carried out with the similar operation as Example 1 except that water was added so that the HEVE concentration will be 20 mass %. As a result, the monomer conversion rate was 99% or more, the number average molecular weight Mn of the obtained polymer was 10700, and the molecular weight distribution Mw/Mn was 1.59 after an elapse of 48 hours.

Example 3

Production of poly(2-hydroxyethyl vinyl ether) (3)

[0070] Polymerization reaction was carried out with the similar operation as Example 1 except that 2,2-azobis[2-methyl-N-(2-hydroxylethyl)propionamide (manufactured by Wako Pure Chemical Industries, Ltd., product name V-086) was used as a radical polymerization initiator. As a result, the monomer conversion rate was 99% or more, the number average molecular weight Mn of the obtained polymer was 11400, and the molecular weight distribution Mw/Mn was 1.94 after an elapse of 93 hours.

Example 4

Production of poly(4-hydroxybutyl vinyl ether) (1)

[0071] Polymerization reaction was carried out with the similar operation as Example 1 except that 4-hydroxylbutyl vinyl ether was used as a monomer. As a result, the monomer conversion rate was 99% or more, the number average molecular weight Mn was 15500, and the molecular weight distribution Mw/Mn was 2.20 after an elapse of 48 hours.

Example 5

Production of poly(l,4-cyclohexanedimethanol monovinyl ether)

[0072] Polymerization reaction was carried out with the similar operation as Example 1 except that 1,4-cyclohexanedimethanol monovinyl ether was used as a monomer. As a result, the monomer conversion rate was 81%, the number average molecular weight Mn of the obtained polymer was 12300, and the molecular weight distribution Mw/Mn was 1.89 after an elapse of 48 hours.

Example 6

Production of poly(diethylene glycol monovinyl ether)

[0073] Polymerization reaction was carried out with the similar operation as Example 1 except that diethylene glycol monovinyl ether (hereinafter, referred to as DEGV) was used as a monomer. As a result, the monomer conversion rate was 99% or more, the number average molecular weight Mn of the obtained polymer was 12600, and the molecular weight distribution Mw/Mn was 2.10 after an elapse of 48 hours.

Example 7

Production of poly(2-hydroxylethyl vinyl ether) (4)

[0074] Polymerization reaction was carried out with the similar operation as Example 1 except that the amount of MAIB added was 0.1 mol % based on a monomer. As a result, the monomer conversion rate was 60% or more after an elapse of 48 hours, and when the polymerization was further continued, the monomer conversion rate became 99% or more after an elapse of 96 hours. The number average molecular weight Mn of the obtained polymer was 35500, and the molecular weight distribution Mw/Mn was 1.74.

Comparative Example 1

Production of poly(2-hydroxyethyl vinyl ether) (5)

[0075] Polymerization reaction was carried out with the similar operation as Example 1 except that toluene was used as a polymerization solvent. As a result, the monomer conversion rate was 49%, the number average molecular weight Mn of the obtained polymer was 18900, and the molecular weight distribution Mw/Mn was 1.68 after an elapse of 24 hours.

Comparative Example 2

Production of poly(2-hydroxyethyl vinyl ether) (6)

[0076] Polymerization reaction was carried out with the similar operation as Example 1 except that 2-propanol was used as a polymerization solvent. As a result, the monomer conversion rate was 31%, the number average molecular weight Mn of the obtained polymer was 15800, and the molecular weight distribution Mw/Mn was 1.55 after an elapse of 24 hours.

Comparative Example 3

Production of poly(2-hydroxyethyl vinyl ether) (7)

[0077] Polymerization reaction was carried out with the similar operation as Example 1 except that ethylene glycol was used as a polymerization solvent. As a result, the monomer conversion rate after an elapse of 24 hours was 71% but polyacetal was generated in 60%. The number average molecular weight Mn of the obtained polymer was 10100, and the molecular weight distribution Mw/Mn was 1.73.

Comparative Example 4

Production of poly(4-hydroxyethyl vinyl ether) (8)

[0078] Polymerization reaction was carried out with the similar operation as Example 1 except that 1,4-butanediol was used as a polymerization solvent. As a result, the monomer conversion rate after an elapse of 24 hours was 69% but polyacetal was generated in 40%. The number average molecular weight Mn of the obtained polymer was 9500, and the molecular weight distribution Mw/Mn was 1.79.

Comparative Example 5

Production of poly(4-hydroxybutyl vinyl ether) (2)

[0079] Polymerization reaction was carried out with the similar operation as Example 4 except that 2,2-azobisisobutyronitrile (manufactured by Wako Pure Chemical Industries, Ltd., product name V-60, hereinafter referred to as AIBN) was used as a radical polymerization initiator. As a result, the monomer conversion rate was 37%, the number average molecular weight Mn of the obtained polymer was 29400, and the molecular weight distribution Mw/Mn was 1.73 after an elapse of 48 hours.

Comparative Example 6

Production of poly(4-hydroxybutyl vinyl ether) (3)

[0080] To a glass vessel with a three-way cock, 68.25 g (587.6 mmol) of HBVE and 17.82 g of methanol was added and heated, and a solution in which 1.3393 g (5.82 mmol, 1 mol % based on a monomer) of MAIB was dissolved in 11.91 g of methanol was added drop wise over 1 hour after the internal temperature reached to 70 C. Then, stirring was carried out for 8 hours at 70 C. 70.58 g of methanol was added and the content was cooled down to room temperature, and extraction was carried out three times with 168.8 g of hexane to remove the residual monomers and the polymerization initiator residues. Then, the solvent was removed under reduced pressure to obtain poly(4-hydroxybutyl vinyl ether). As a result, the monomer conversion rate was 56.7%, the number average molecular weight Mn of the obtained polymer was 32000, and the molecular weight distribution Mw/Mn was 1.35.

Comparative Example 7

Production of poly(4-hydroxybutyl vinyl ether) (4)

[0081] Polymerization reaction was carried out with the similar operation as Comparative Example 6 except that the amount of MAIB used was changed to 5 mol % based on a monomer. As a result, the monomer conversion rate was 91.67%, the number average molecular weight Mn of the obtained polymer was 34000, and the molecular weight distribution Mw/Mn was 1.24.

Example 8

Production of poly(4-hydroxybutyl vinyl ether) (5)

[0082] To a glass vessel with a three-way cock, 90 g of water, 90 g (774 mmol) of HBVE, 29.7 g (129 mmol, 16.7 mol % based on the total amount of monomers) of MAIB were introduced and heated at 70 C., then the polymerization was carried out for 10 hours under stirring. After cooling down to room temperature, water and light components were removed by evaporation to obtain poly(4-hydroxybutyl vinyl ether) of interest. The HBVE conversion rate was 99% or more, the number average molecular weight Mn of the obtained polymer was 3090, and the molecular weight distribution Mw/Mn was 2.40.

Example 9

Production of poly(4-hydroxybutyl vinyl ether) (6)

[0083] Polymerization reaction was carried out with the similar operation as Example 8 except that the amount of MAIB added was 3 mol % based on a monomer. As a result, the HBVE conversion rate was 89%, the number average molecular weight Mn of the obtained polymer was 5910, and the molecular weight distribution Mw/Mn was 1.78.

Example 10

Production of 4-hydroxylbutyl vinyl ether/diethylene glycol monovinyl ether copolymer (1)

[0084] To a glass vessel with a three-way cock, 90 g of water, 71.9 g (619 mmol) of HBVE, 20.6 g (156 mmol) of DEGV, 29.7 g (129 mmol, 16.6 mol % based on the total amount of monomers) of MAIB were introduced and heated at 70 C., then the polymerization was carried out for 10 hours under stirring. After cooling down to room temperature, water and light components were removed by evaporation to obtain a HBVE/DEGV copolymer of interest. The HBVE C was 99.6%, the DEGV conversion rate was 94.2%, the number average molecular weight Mn of the obtained polymer was 3160, and the molecular weight distribution Mw/Mn was 2.13.

TABLE-US-00001 TABLE 1 Polymerization Initiator Monomer Polymer Added Residual Number average molecular weight Polymerization Amount Amount molecular weight distribution Solvent Type (mol %) Type (mol %) Mn Mw/Mn Example 1 water MAIB 0.2 HEVE Less than 1 33900 2.45 Example 2 water MAIB 0.2 HEVE Less than 1 10700 1.59 Example 3 water V-086 0.2 HEVE Less than 1 11400 1.94 Example 4 water MAIB 0.2 HBVE Less than 1 15500 2.20 Example 5 water MAIB 0.2 CHDMVE 19 12300 1.89 Example 6 water MAIB 0.2 DEGVE Less than 1 12600 2.10 Example 7 water MAIB 0.1 HEVE Less than 1 35500 1.74 Comparative toluene MAIB 0.2 HEVE 51 18900 1.68 Example 1 Comparative 2-propanol MAIB 0.2 HEVE 69 15800 1.55 Example 2 Comparative Ethylene MAIB 0.2 HEVE 29 10100 1.73 Example 3 glycol Comparative 1,4-butanediol MAIB 0.2 HEVE 31 9500 1.79 Example 4 Comparative water AIBN 0.2 HBVE 63 29400 1.73 Example 5 Comparative methanol MAIB 1 HBVE 43.3 32000 1.35 Example 6 Comparative methanol MAIB 5 HBVE 8.33 34000 1.24 Example 7 Example 8 water MAIB 16.7 HBVE Less than 1 3090 2.40 Example 9 water MAIB 3 HBVE 11 5910 1.78 Example 10 water MAIB 16.6 HBVE/DEGVE 0.4/5.8 3160 2.13