CA2278115A1 - Suspension polymerization process of acrylic monomers - Google Patents
Suspension polymerization process of acrylic monomers Download PDFInfo
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- CA2278115A1 CA2278115A1 CA002278115A CA2278115A CA2278115A1 CA 2278115 A1 CA2278115 A1 CA 2278115A1 CA 002278115 A CA002278115 A CA 002278115A CA 2278115 A CA2278115 A CA 2278115A CA 2278115 A1 CA2278115 A1 CA 2278115A1
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- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F2/00—Processes of polymerisation
- C08F2/12—Polymerisation in non-solvents
- C08F2/16—Aqueous medium
- C08F2/18—Suspension polymerisation
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Abstract
Process for preparing antistatic acrylic polymers wherein the acrylic monomers are polymerized in suspension, said acrylic monomers contain dissolved the antistatic additives selected from the following ones:
(1) C n H2n+1CO-N (CH2CH2OH)2 wherein n is an integer ranging from 9 to 13;
(2) C n H 2n'+1N(CH2CH2OH)2 wherein n' is an integer ranging from 8 to 14;
(3) CH2(OR1)CH(OR2)CH2(OR3) or C(CH2OR1)(CH2OR2)(CH2OR3)(CH2OR4) wherein R1, R2, R3, R4 equal to or different from each other, are H or R, wherein R is a saturated or unsaturated C12-C18 alkylcarboxylate, preferably saturated or monounsaturated C18.
(1) C n H2n+1CO-N (CH2CH2OH)2 wherein n is an integer ranging from 9 to 13;
(2) C n H 2n'+1N(CH2CH2OH)2 wherein n' is an integer ranging from 8 to 14;
(3) CH2(OR1)CH(OR2)CH2(OR3) or C(CH2OR1)(CH2OR2)(CH2OR3)(CH2OR4) wherein R1, R2, R3, R4 equal to or different from each other, are H or R, wherein R is a saturated or unsaturated C12-C18 alkylcarboxylate, preferably saturated or monounsaturated C18.
Description
SUSPENSION POLYMERIZATION PROCESS OF ACRYLIC MONOMERS
The present invention relates to a process for preparing antistatic acrylic polymers.
More specifically it relates to the production of acrylic (co)polymers beads having antistatic properties combined with optical properties comparable with those of the commercial acrylic copolymers, and with good mechanical and thermal properties.
It is known in the art that acrylic polymers do not show antistatic properties wherefore they easily attract dust and generally all the contaminants contained in the air. This represents a disadvantage for all the acrylic polymer applica-tions where a particular cleanness and optical quality are required. As an example of these applications the vendor ma-chine displays (distributing machines), dashboards, phones, etc., can be mentioned. Industrially, in order to avoid the presence of contaminants during the assembly, antistatic sprays or antistatic liquids which are mechanically distribu-ted on the surface, are used. These systems have the inconve-nience to increase the production costs, and the working times with pollution problems. Moreover the efficacy of these systems drastically decreases running the time, of the order of a few days, since they are easily removed from the surface due to any mechanical action. A further disadvantage of these systems is that the uniform distribution on the surface, also using sophisticated and expensive technologies, is not guaranteed. It is to be noted that these treatments are to be repeated during the time in order to maintain the acrylic polymer antistatic properties.
Processes to make antistatic acrylic polymers by prepa ring a compound in hot extruders or mixers (for instance Brabender) by addition of antistatic additives to the prefor med polymer, are also known in the art. These systems have the drawback not to lead to compounds with a good additive di stribution in the polymer. In order to obtain a good additive homogenization in the compound it is necessay to submit the additive to high temperatures for prolonged times. This operating way has the disadvantage to degrade the additive, to deactivate or volatilize it with consequent loss of antistatic properties. Tests carried out by the Applicant on pilot scale with extruders having about a 50 kg/h flow-rate have shown that with the known antistatic additives the acrylic polymer optical properties are worsened.
The need was felt to have available an industrial process for the production of antistatic acrylic polymers having anti-static properties combined with optical properties comparable with those of the commercial acrylic copolymers and with good mechanical and thermal properties wherein the antistatic ad-ditive is homogeneously distributed in the polymer.
It has been surprisingly and unexpectedly found by the Applicant a process to make the acrylic polymers antistatic which overcomes the disadvantage of the prior art and allows to obtain acrylic polymers with the combination of the above mentioned properties.
An object of the present invention is a process for pre-paring antistatic acrylic polymers wherein the acrylic mono-mers are polymerized in suspension, said acrylic monomers contain dissolved the antistatic additives selected from the following:
( 1 } CnHzn+1C0-N ( CHzCH20H) z wherein n is an intger ranging from 9 to 13, preferably n=11;
( 2 } Cn ~ HZ n ~ +~N ( CH2 CHz OH ) 2 wherein n' is an integer ranging from 8 to 14, preferably n'=12;
( 3 } CHz ( OR1 ) CH ( ORz ) CH2 ( OR3 ) or C ( CHZORl ) ( CH20R2 ) ( CHzOR3 ) ( CHzOR4 ) wherein Rl, R2, R3, RQ equal to or different from each other, are H or R, wherein R is a saturated or unsaturated C12-Cle alkylcarboxylate, preferably saturated or monounsaturated Cle, in class (3) monoesters are the preferred compounds; or their mixtures; the amount of total antistatic additive being in the range 0 . 2 -15 phr ( for 10 0 parts of monomers ) , preferably in the range 1-5 phr.
The product obtained in the form of beads, generally with size in the range 50-1, 000 micron, is subsequently transformed into granules by extrusion with the same conventional techni-ques of the acrylic polymers. It has been surprisingly found that the antistatic additive does not undergo a degradation, modification or meaningful loss.
The so obtained granules can be used for the injection molding to obtain manufactured articles having antistatic pro-perties which substantially remain unchanged during the time, combined with optical, mechanical and thermal properties, comparable with those of the starting acrylic polymers.
The suspension polymerization is well known and is a type of polymerization carried out in a system wherein the monomer is suspended under the form of little drops in a continuous phase and polymerized by using a radicalic type initiator soluble in the monomer. The continuous phase is generally water.
The ratio between the continuous phase (water) and the discontinuous phase (monomer) is generally in the range 1:1-3:1.
In the practical carrying out of this kind of process, it is necessary the use of suspension stabilizers which hinder the monomer little drops coalescence in the most advanced po-lymerization stages.
As suspension stabilizers, in the most common technique, hydrosoluble macromolecular compounds having an affinity towards the monomer are used. The stabilizer places itself at the interface between organic phase and aqueous phase, and forms a protective film which hinders the polymeric particle agglomeration.
At the end of the polymerization the suspending agent is removed from the polymer particle surface by washing with water.
See for example EP 457,356, herein incorporated by re-ference, wherein, as suspending and stabilizing agents of the aqueous suspension, polymers selected from the homopolymers of compounds having the formula CH2 = CRa - CO - A - CRbR~ -CHZ - S03 M ( I ) are used, wherein: Ra = H, CH3; Rb and R~, equal to or diffe-rent, are H, C1-C8 alkyls and M - alkaline, alkaline-earth metal or ammonium, A - NH, O or NCH3, or the copolymers of said compounds with acrylic monomers in amounts in the range 0-40~ by weight.
As continuous phase instead of water the polymerization aqueous phase, totally or partially formed by the mother liquors obtained after the acrylic polymer separation, can be used, said mother liquors containing an organic phase compri-sing said suspending agent and other products obtained in polymerization, optionally added with an additional amount of said suspending agent so as to have a suspending medium containing at least 0.05% by weight and up to about 1~ by weight of said suspending agent and at least 0.05 by weight, the maximum extent being up to about 5~ by weight, of the above mentioned other products obtained in polymerization, preferably 0.1-0.5~ by weight of the suspending agent and 0.1 lg by weight of the other products obtained in polymerization.
This process is described in EP 683, 182 in the name of the Applicant herein incorporated by reference.
As suspending agents which can be used in the suspension polymerization besides the suspending agents of formula (I), those known used in this kind of polymerization, such as polyvinylic alcohol, poly(meth)acrylic acid, etc., can be mentioned.
The acrylic polymer is separated from the mother liquors, for instance by centrifugation or filtration. The process can be carried out using the modalities known for the aqueous suspension polymerizations, that is, by operating with ratios between the aqueous phase and the acrylic monomers generally in the range 1:1-3:1, in the presence of suspending agents and of a radical polymerization initiator at temperatures at which the initiator decomposition occurs, generally in the range 50°C-120°C. The aqueous phase is totally (1000 or partially formed, also in the range 30-50~ by weight, by the mother liquors obtained by a previous polymerization provided that the above mentioned limits are observed. It is possible to recycle from 30 to 100 by weight of said mother liquors, if necessary by integrating with further amounts of water optionally containing fresh suspending agent.
The acrylic monomers which can be polymerized according to the process of the present invention are C1-Cg alkylacryla tes or methacrylates such as, for example, methyl (meth) acryla te, ethyl (meth) acrylate, propyl (meth) acrylate, isopropyl (met-h)acrylate, butylacrylate, sec-butylmethacrylate, terbu-tylmethacrylate. Said acrylic monomers can be used singly or in admixture each other, optionally in the presence of other monomers, in amounts of at most 50~ by weight, containing double bonds, such as, for example, styrene, alpha-methyls-tyrene, (meth)acrylonitrile, alkyl-, cycloalkyl- or aryl-maleimides, butadiene, (meth)acrylic acid, (meth)acrylamide.
As radicalic initiators peroxides such as for example t-butylperoxy-2-ethylhexanoate, dibenzoylperoxide, t-butylpe-roxydiethylacetate or unstable azocompounds such as, for example, azodiisobutyronitrile, can be used.
Examples for illustrative but not limitative purposes of the present ivention are given hereinafter.
EXAMPLE 1 (suspendant preparation) In a reactor 120 parts of a 40% by weight NaOH solution and 630 parts of deionized water are introduced. 250 parts of 2-acrylamido-2-methylpropansulphonic (AMPS) acid are slowly fed, then the pH is adjusted in the range 7-8 with small additions of soda or AMPS. After the solution has been fluxed with nitrogen to eliminate oxygen and heated to 50°C, 0.075 parts of potassium persulphate and 0.025 parts of sodium methabisulphite are added. The polymerization is completed in about 60 minutes. Then it is diluted with 4,000 parts of deionized water obtaining a solution with a dry residue at 160°C of 5.5°s by weight and a Brookfield viscosity of 4 Pas, determined at 25°C.
EXAMPLE 2 (comparative) The methylmethacrylate and methylacrylate suspension polymerization is carried out, using as suspending agent the sodic salt homopolymer of the 2-acrylamido-2-methylpropansul-phonic acid obtained in Example 1.
In a stirred, jacketed and pressure-resistant reactor, 193 parts of deionized water and 7 parts of the solution obtained in Example 1, corresponding to 0.385 parts of dry product, are introduced. The oxygen is elimianted by nitrogen flow and the solution is heated to 80°C. Then 100.67 parts of a mixture, it too deoxygenated, formed by: methylmethacrylate 98 parts, methylacrylate 2 parts, benzoyl peroxide 0.5 parts, n-butanthiol 0.17 parts, are fed.
The reactor is hermetically sealed, pressurized at 100 KPa and under continuous stirring the mixture is gradually heated up to 110°C in 120'. The reactor is allowed to stay at 110°C for 15 minutes, then it is cooled.
The polymer, in the form of beads, is separated from the mother liquors by centrifugation, washed with deionized water and dried in stove at 80°C.
The mother liquors, with a dry residue at 160°C of about 0.6% by weight, partly formed by the suspending agent (0.2% by weight) and for the remaining fraction by acrylic polymer in the form of particles in emulsion, are collected in order to be used in the subsequent polymerization tests.
EXAMPLE 3 ! comparat ive ) In the same reactor already used in Example 2 and with the general operating modalities described in said Example, the methylmethacrylate and methylacrylate suspension polymeri-zation is carried out, using as suspending solution the mother liquors coming from the polymerization described in Example 2, without further addition of the suspending agent.
200 parts of mother liquors of Example 2 are then intro-duced in the reactor. The solution is heated to 80°C and then 100.67 parts of a mixture, formed by: methylmethacrylate 98 parts, methylacrylate 2 parts, benzoyl peroxide 0.5 parts, n-butanthiol 0.17 parts, are fed.
The polymerization is carried out according to the 10 procedures already described in Example 2. The reactor is allowed to stay at 110°C for 15 minutes, then it is cooled.
The polymer, in the form of beads, is separated from the mother liquors by centrifugation, washed with deionized water and dried in stove at 80°C.
The mother liquors show a dry residue at 160°C of about 0.7% by weight, partly formed by the suspending agent (0.2% by weight? and for the remaining fraction by acrylic polymer in the form of particles in emulsion.
The methylmethacrylate and methylacrylate suspension polymerization is carried out, using as suspending agent the sodic salt homopolymer of the 2-acrylamido-2-methylpropansul-phonic acid obtained in Example 1.
In a stirred, jacketed and pressure-resistant reactor, 193 parts of deionized water and 7 parts of the solution obtained in Example 1, corresponding to 0.385 parts of dry product, are introduced. The oxygen is eliminated by nitrogen flow and the solution is heated to 80°C. Then 103.67 parts of a mixture, it too deoxygenated, formed by: methylmethacrylate 98 parts, methylacrylate 2 parts, antistatic agent of formula (1) 3 parts, benzoyl peroxide 0.5 parts, n-butanthiol 0.17 parts, are fed.
The reactor is hermetically sealed, pressurized at 100 KPa and under continuous stirring the mixture is gradually heated up to 110°C in 120'. The reactor is allowed to stay at 110°C for 15 minutes, then it is cooled.
The polymer, in the form of beads, is separated from the mother liquors by centrifugation, washed with deionized water and dried in stove at 80°C.
The mother liquors show a dry residue at 160°C of about 0.6% by weight, partly formed by the suspending agent (0.2~ by weight) and for the remaining fraction by acrylic polymer in the form of particles in emulsion.
The obtained polymer beads are dissolved in CHC13 and then reprecipitated in hexane.
The FT-IR analysis of the fraction soluble in hexane of the so obtained beads shows the presence of the additive. This confirms that the additive is wholly englobed in the beads themselves.
In the same reactor already used in Example 2 and with the general operating procedures described in said Example, the methylmethacrylate and methylacrylate suspension polyme-rization is carried out, using as suspending solution the mother liquors coming from the polymerization described in Example 2, without further addition of the suspending agent.
200 parts of mother liquors of Example 2 are then intro-duced in the reactor. The solution is heated to 80°C and then 103.67 parts of a mixture, formed by: methylmethacrylate 98 parts, methylacrylate 2 parts, antistatic agent of formula (1) 3 parts, benzoyl peroxide 0.5 parts, n-butanthiol 0.17 parts, are fed.
The polymerization is carried out according to the procedures already described in Example 2. The reactor is allowed to stay at 110°C for 15 minutes, then it is cooled.
The polymer, in the form of beads, is separated from the mother liquors by centrifugation, washed with deionized water and dried in stove at 80°C.
The mother liquors show a dry residue at 160°C of about 0.7~s by weight, partly formed by the suspending agent (0.2a by weight) and for the remaining fraction by acrylic polymer in the form of particles in emulsion.
The obtained polymer beads are dissolved in CHC13 and then reprecipitated in hexane.
The FT-IR analysis of the fraction soluble in hexane of the so obtained beads shows the presence of the additive. This confirms that the additive is wholly englobed in the beads themselves.
In the same reactor already used in Example 2 and with the general operating procedures described in said Example, the methylmethacrylate and methylacrylate suspension polymeri-zation is carried out, using as suspending solution the mother liquors coming from the polymerization described in Example 2, without further addition of the suspending agent.
200 parts of mother liquors of Example 2 are then intro-duced in the reactor. The solution is heated to 80°C and then 105.67 parts of a mixture, formed by: methylmethacrylate 98 parts, methylacrylate 2 parts, antistatic agent of formula (3) 5 parts, benzoyl peroxide 0.5 parts, n-butanthiol 0.17 parts, are fed.
The polymerization is carried out according to the procedures already described in Example 2. The reactor is allowed to stay at 110°C for 15 minutes, then it is cooled.
The polymer, in the form of beads, is separated from the mother liquors by centrifugation, washed with deionized water and dried in stove at 80°C.
The mother liquors show a dry residue at 160°C of about 0.7~ by weight, partly formed by the suspending agent (0.2~ by weight) and for the remaining fraction by acrylic polymer in the form of particles in emulsion.
The obtained polymer beads are dissolved in CHC1, and then reprecipitated in hexane.
The FT-IR analysis of the fraction soluble in hexane of the so obtained beads shows the additive presence. This confirms that the additive is wholly englobed in the beads themselves.
In a stirred, jacketed and pressure-resistant reactor, 297 parts of deionized water and 3 parts of polyvinylic alcohol having a viscosity in the range 5-20 cPS at a 5~ by weight concentration, are introduced. The oxygen is eliminated by nitrogen flow and the solution is heated to 80°C. Then 103.67 parts of a mixture, it too deoxygenated, formed by:
methylmethacrylate 98 parts, methylacrylate 2 parts, anti-static agent of formula (2) 3 parts, benzoyl peroxide 0.5 parts, n-butanthiol 0.17 parts, are fed.
The polymerization is carried out according to the procedures already described in Example 2. The reactor is allowed to stay at 110°C for 15 minutes, then it is cooled.
The polymer, in the form of beads, is separated from the mother liquors by centrifugation, washed with deionized water and dried in stove at 80°C.
The mother liquors show a dry residue at 160°C of about 0.6~ by weight, partly formed by the suspending agent (0.2~s by weight) and for the remaining fraction by acrylic polymer in the form of particles in emulsion.
The obtained polymer beads are dissolved in CHC13 and then reprecipitated in hexane.
10 The FT-IR analysis of the fraction soluble in hexane of the so obtained beads shows the additive presence. This confirms that the additive is wholly englobed in the beads themselves.
The beads obtained according to the methods described in Examples 2-5 were granulated by monoscrew extruder according to the usual methods for PMMA. The beads arP lnar3ar3 ;n a feedbox from which they are introduced in the extruder. A
Bandera TR30 monoscrew extruder is used, having the following characteristis:
Length/diameter (L/D) - 25 Flow-rate (Kg/h) _ 5 Extruder temperature (°C) lAt zone (15 cm from feeding) - 210 2nd zone (29 cm from feeding) - 230 3rd zone (59 cm from feeding) - 230 4"' zone (75 cm from feeding) - 220.
The Melt Flow Rate (M.f.r.) of the so obtained granules was measured, see Table 1.
The so obtained granules were injection molded so as to obtain specimen suitable to the determination of the thermal, optical and antistatic properties according to the methods indicated in Table 1.
For the thermal properties (Vicat) and antistatic (surface resistivity) the specimen are disks having 66 mm diameter and 3.2 mm thickness for the Vicat and 66 mm diameter and 1.6 mm thickness for the antistatic properties.
As to the optical properties (Transmittance Ts, Haze, Yellow Index Y.I.) the specimen are rectangular plates having 90 x 60 mm sizes and a 4 mm thickness.
The results are shown in Table 1.
EXAMPLE 9 (comparative) Example 8 was repeated using the polymer beads of Example 3 to which 3 phr of additive of formula (1) of Example 5 were added by extrusion.
The results are shown in Table 1.
The comparison of the results of Example 5, beads obtained with the antistatic agent directly in the polymeriza-tion process, and of Example 9, beads charged with the antistatic agent in extruder, reported in Table 1 shows that the antistatic properties are clearly better in Example 5 (lower resistivity value) compared with those of Example 9.
Moreover it is noted that the very good resistivity values of Example 5 are combined with clearly superior optical proper-ties, Haze and Y.I..
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The present invention relates to a process for preparing antistatic acrylic polymers.
More specifically it relates to the production of acrylic (co)polymers beads having antistatic properties combined with optical properties comparable with those of the commercial acrylic copolymers, and with good mechanical and thermal properties.
It is known in the art that acrylic polymers do not show antistatic properties wherefore they easily attract dust and generally all the contaminants contained in the air. This represents a disadvantage for all the acrylic polymer applica-tions where a particular cleanness and optical quality are required. As an example of these applications the vendor ma-chine displays (distributing machines), dashboards, phones, etc., can be mentioned. Industrially, in order to avoid the presence of contaminants during the assembly, antistatic sprays or antistatic liquids which are mechanically distribu-ted on the surface, are used. These systems have the inconve-nience to increase the production costs, and the working times with pollution problems. Moreover the efficacy of these systems drastically decreases running the time, of the order of a few days, since they are easily removed from the surface due to any mechanical action. A further disadvantage of these systems is that the uniform distribution on the surface, also using sophisticated and expensive technologies, is not guaranteed. It is to be noted that these treatments are to be repeated during the time in order to maintain the acrylic polymer antistatic properties.
Processes to make antistatic acrylic polymers by prepa ring a compound in hot extruders or mixers (for instance Brabender) by addition of antistatic additives to the prefor med polymer, are also known in the art. These systems have the drawback not to lead to compounds with a good additive di stribution in the polymer. In order to obtain a good additive homogenization in the compound it is necessay to submit the additive to high temperatures for prolonged times. This operating way has the disadvantage to degrade the additive, to deactivate or volatilize it with consequent loss of antistatic properties. Tests carried out by the Applicant on pilot scale with extruders having about a 50 kg/h flow-rate have shown that with the known antistatic additives the acrylic polymer optical properties are worsened.
The need was felt to have available an industrial process for the production of antistatic acrylic polymers having anti-static properties combined with optical properties comparable with those of the commercial acrylic copolymers and with good mechanical and thermal properties wherein the antistatic ad-ditive is homogeneously distributed in the polymer.
It has been surprisingly and unexpectedly found by the Applicant a process to make the acrylic polymers antistatic which overcomes the disadvantage of the prior art and allows to obtain acrylic polymers with the combination of the above mentioned properties.
An object of the present invention is a process for pre-paring antistatic acrylic polymers wherein the acrylic mono-mers are polymerized in suspension, said acrylic monomers contain dissolved the antistatic additives selected from the following:
( 1 } CnHzn+1C0-N ( CHzCH20H) z wherein n is an intger ranging from 9 to 13, preferably n=11;
( 2 } Cn ~ HZ n ~ +~N ( CH2 CHz OH ) 2 wherein n' is an integer ranging from 8 to 14, preferably n'=12;
( 3 } CHz ( OR1 ) CH ( ORz ) CH2 ( OR3 ) or C ( CHZORl ) ( CH20R2 ) ( CHzOR3 ) ( CHzOR4 ) wherein Rl, R2, R3, RQ equal to or different from each other, are H or R, wherein R is a saturated or unsaturated C12-Cle alkylcarboxylate, preferably saturated or monounsaturated Cle, in class (3) monoesters are the preferred compounds; or their mixtures; the amount of total antistatic additive being in the range 0 . 2 -15 phr ( for 10 0 parts of monomers ) , preferably in the range 1-5 phr.
The product obtained in the form of beads, generally with size in the range 50-1, 000 micron, is subsequently transformed into granules by extrusion with the same conventional techni-ques of the acrylic polymers. It has been surprisingly found that the antistatic additive does not undergo a degradation, modification or meaningful loss.
The so obtained granules can be used for the injection molding to obtain manufactured articles having antistatic pro-perties which substantially remain unchanged during the time, combined with optical, mechanical and thermal properties, comparable with those of the starting acrylic polymers.
The suspension polymerization is well known and is a type of polymerization carried out in a system wherein the monomer is suspended under the form of little drops in a continuous phase and polymerized by using a radicalic type initiator soluble in the monomer. The continuous phase is generally water.
The ratio between the continuous phase (water) and the discontinuous phase (monomer) is generally in the range 1:1-3:1.
In the practical carrying out of this kind of process, it is necessary the use of suspension stabilizers which hinder the monomer little drops coalescence in the most advanced po-lymerization stages.
As suspension stabilizers, in the most common technique, hydrosoluble macromolecular compounds having an affinity towards the monomer are used. The stabilizer places itself at the interface between organic phase and aqueous phase, and forms a protective film which hinders the polymeric particle agglomeration.
At the end of the polymerization the suspending agent is removed from the polymer particle surface by washing with water.
See for example EP 457,356, herein incorporated by re-ference, wherein, as suspending and stabilizing agents of the aqueous suspension, polymers selected from the homopolymers of compounds having the formula CH2 = CRa - CO - A - CRbR~ -CHZ - S03 M ( I ) are used, wherein: Ra = H, CH3; Rb and R~, equal to or diffe-rent, are H, C1-C8 alkyls and M - alkaline, alkaline-earth metal or ammonium, A - NH, O or NCH3, or the copolymers of said compounds with acrylic monomers in amounts in the range 0-40~ by weight.
As continuous phase instead of water the polymerization aqueous phase, totally or partially formed by the mother liquors obtained after the acrylic polymer separation, can be used, said mother liquors containing an organic phase compri-sing said suspending agent and other products obtained in polymerization, optionally added with an additional amount of said suspending agent so as to have a suspending medium containing at least 0.05% by weight and up to about 1~ by weight of said suspending agent and at least 0.05 by weight, the maximum extent being up to about 5~ by weight, of the above mentioned other products obtained in polymerization, preferably 0.1-0.5~ by weight of the suspending agent and 0.1 lg by weight of the other products obtained in polymerization.
This process is described in EP 683, 182 in the name of the Applicant herein incorporated by reference.
As suspending agents which can be used in the suspension polymerization besides the suspending agents of formula (I), those known used in this kind of polymerization, such as polyvinylic alcohol, poly(meth)acrylic acid, etc., can be mentioned.
The acrylic polymer is separated from the mother liquors, for instance by centrifugation or filtration. The process can be carried out using the modalities known for the aqueous suspension polymerizations, that is, by operating with ratios between the aqueous phase and the acrylic monomers generally in the range 1:1-3:1, in the presence of suspending agents and of a radical polymerization initiator at temperatures at which the initiator decomposition occurs, generally in the range 50°C-120°C. The aqueous phase is totally (1000 or partially formed, also in the range 30-50~ by weight, by the mother liquors obtained by a previous polymerization provided that the above mentioned limits are observed. It is possible to recycle from 30 to 100 by weight of said mother liquors, if necessary by integrating with further amounts of water optionally containing fresh suspending agent.
The acrylic monomers which can be polymerized according to the process of the present invention are C1-Cg alkylacryla tes or methacrylates such as, for example, methyl (meth) acryla te, ethyl (meth) acrylate, propyl (meth) acrylate, isopropyl (met-h)acrylate, butylacrylate, sec-butylmethacrylate, terbu-tylmethacrylate. Said acrylic monomers can be used singly or in admixture each other, optionally in the presence of other monomers, in amounts of at most 50~ by weight, containing double bonds, such as, for example, styrene, alpha-methyls-tyrene, (meth)acrylonitrile, alkyl-, cycloalkyl- or aryl-maleimides, butadiene, (meth)acrylic acid, (meth)acrylamide.
As radicalic initiators peroxides such as for example t-butylperoxy-2-ethylhexanoate, dibenzoylperoxide, t-butylpe-roxydiethylacetate or unstable azocompounds such as, for example, azodiisobutyronitrile, can be used.
Examples for illustrative but not limitative purposes of the present ivention are given hereinafter.
EXAMPLE 1 (suspendant preparation) In a reactor 120 parts of a 40% by weight NaOH solution and 630 parts of deionized water are introduced. 250 parts of 2-acrylamido-2-methylpropansulphonic (AMPS) acid are slowly fed, then the pH is adjusted in the range 7-8 with small additions of soda or AMPS. After the solution has been fluxed with nitrogen to eliminate oxygen and heated to 50°C, 0.075 parts of potassium persulphate and 0.025 parts of sodium methabisulphite are added. The polymerization is completed in about 60 minutes. Then it is diluted with 4,000 parts of deionized water obtaining a solution with a dry residue at 160°C of 5.5°s by weight and a Brookfield viscosity of 4 Pas, determined at 25°C.
EXAMPLE 2 (comparative) The methylmethacrylate and methylacrylate suspension polymerization is carried out, using as suspending agent the sodic salt homopolymer of the 2-acrylamido-2-methylpropansul-phonic acid obtained in Example 1.
In a stirred, jacketed and pressure-resistant reactor, 193 parts of deionized water and 7 parts of the solution obtained in Example 1, corresponding to 0.385 parts of dry product, are introduced. The oxygen is elimianted by nitrogen flow and the solution is heated to 80°C. Then 100.67 parts of a mixture, it too deoxygenated, formed by: methylmethacrylate 98 parts, methylacrylate 2 parts, benzoyl peroxide 0.5 parts, n-butanthiol 0.17 parts, are fed.
The reactor is hermetically sealed, pressurized at 100 KPa and under continuous stirring the mixture is gradually heated up to 110°C in 120'. The reactor is allowed to stay at 110°C for 15 minutes, then it is cooled.
The polymer, in the form of beads, is separated from the mother liquors by centrifugation, washed with deionized water and dried in stove at 80°C.
The mother liquors, with a dry residue at 160°C of about 0.6% by weight, partly formed by the suspending agent (0.2% by weight) and for the remaining fraction by acrylic polymer in the form of particles in emulsion, are collected in order to be used in the subsequent polymerization tests.
EXAMPLE 3 ! comparat ive ) In the same reactor already used in Example 2 and with the general operating modalities described in said Example, the methylmethacrylate and methylacrylate suspension polymeri-zation is carried out, using as suspending solution the mother liquors coming from the polymerization described in Example 2, without further addition of the suspending agent.
200 parts of mother liquors of Example 2 are then intro-duced in the reactor. The solution is heated to 80°C and then 100.67 parts of a mixture, formed by: methylmethacrylate 98 parts, methylacrylate 2 parts, benzoyl peroxide 0.5 parts, n-butanthiol 0.17 parts, are fed.
The polymerization is carried out according to the 10 procedures already described in Example 2. The reactor is allowed to stay at 110°C for 15 minutes, then it is cooled.
The polymer, in the form of beads, is separated from the mother liquors by centrifugation, washed with deionized water and dried in stove at 80°C.
The mother liquors show a dry residue at 160°C of about 0.7% by weight, partly formed by the suspending agent (0.2% by weight? and for the remaining fraction by acrylic polymer in the form of particles in emulsion.
The methylmethacrylate and methylacrylate suspension polymerization is carried out, using as suspending agent the sodic salt homopolymer of the 2-acrylamido-2-methylpropansul-phonic acid obtained in Example 1.
In a stirred, jacketed and pressure-resistant reactor, 193 parts of deionized water and 7 parts of the solution obtained in Example 1, corresponding to 0.385 parts of dry product, are introduced. The oxygen is eliminated by nitrogen flow and the solution is heated to 80°C. Then 103.67 parts of a mixture, it too deoxygenated, formed by: methylmethacrylate 98 parts, methylacrylate 2 parts, antistatic agent of formula (1) 3 parts, benzoyl peroxide 0.5 parts, n-butanthiol 0.17 parts, are fed.
The reactor is hermetically sealed, pressurized at 100 KPa and under continuous stirring the mixture is gradually heated up to 110°C in 120'. The reactor is allowed to stay at 110°C for 15 minutes, then it is cooled.
The polymer, in the form of beads, is separated from the mother liquors by centrifugation, washed with deionized water and dried in stove at 80°C.
The mother liquors show a dry residue at 160°C of about 0.6% by weight, partly formed by the suspending agent (0.2~ by weight) and for the remaining fraction by acrylic polymer in the form of particles in emulsion.
The obtained polymer beads are dissolved in CHC13 and then reprecipitated in hexane.
The FT-IR analysis of the fraction soluble in hexane of the so obtained beads shows the presence of the additive. This confirms that the additive is wholly englobed in the beads themselves.
In the same reactor already used in Example 2 and with the general operating procedures described in said Example, the methylmethacrylate and methylacrylate suspension polyme-rization is carried out, using as suspending solution the mother liquors coming from the polymerization described in Example 2, without further addition of the suspending agent.
200 parts of mother liquors of Example 2 are then intro-duced in the reactor. The solution is heated to 80°C and then 103.67 parts of a mixture, formed by: methylmethacrylate 98 parts, methylacrylate 2 parts, antistatic agent of formula (1) 3 parts, benzoyl peroxide 0.5 parts, n-butanthiol 0.17 parts, are fed.
The polymerization is carried out according to the procedures already described in Example 2. The reactor is allowed to stay at 110°C for 15 minutes, then it is cooled.
The polymer, in the form of beads, is separated from the mother liquors by centrifugation, washed with deionized water and dried in stove at 80°C.
The mother liquors show a dry residue at 160°C of about 0.7~s by weight, partly formed by the suspending agent (0.2a by weight) and for the remaining fraction by acrylic polymer in the form of particles in emulsion.
The obtained polymer beads are dissolved in CHC13 and then reprecipitated in hexane.
The FT-IR analysis of the fraction soluble in hexane of the so obtained beads shows the presence of the additive. This confirms that the additive is wholly englobed in the beads themselves.
In the same reactor already used in Example 2 and with the general operating procedures described in said Example, the methylmethacrylate and methylacrylate suspension polymeri-zation is carried out, using as suspending solution the mother liquors coming from the polymerization described in Example 2, without further addition of the suspending agent.
200 parts of mother liquors of Example 2 are then intro-duced in the reactor. The solution is heated to 80°C and then 105.67 parts of a mixture, formed by: methylmethacrylate 98 parts, methylacrylate 2 parts, antistatic agent of formula (3) 5 parts, benzoyl peroxide 0.5 parts, n-butanthiol 0.17 parts, are fed.
The polymerization is carried out according to the procedures already described in Example 2. The reactor is allowed to stay at 110°C for 15 minutes, then it is cooled.
The polymer, in the form of beads, is separated from the mother liquors by centrifugation, washed with deionized water and dried in stove at 80°C.
The mother liquors show a dry residue at 160°C of about 0.7~ by weight, partly formed by the suspending agent (0.2~ by weight) and for the remaining fraction by acrylic polymer in the form of particles in emulsion.
The obtained polymer beads are dissolved in CHC1, and then reprecipitated in hexane.
The FT-IR analysis of the fraction soluble in hexane of the so obtained beads shows the additive presence. This confirms that the additive is wholly englobed in the beads themselves.
In a stirred, jacketed and pressure-resistant reactor, 297 parts of deionized water and 3 parts of polyvinylic alcohol having a viscosity in the range 5-20 cPS at a 5~ by weight concentration, are introduced. The oxygen is eliminated by nitrogen flow and the solution is heated to 80°C. Then 103.67 parts of a mixture, it too deoxygenated, formed by:
methylmethacrylate 98 parts, methylacrylate 2 parts, anti-static agent of formula (2) 3 parts, benzoyl peroxide 0.5 parts, n-butanthiol 0.17 parts, are fed.
The polymerization is carried out according to the procedures already described in Example 2. The reactor is allowed to stay at 110°C for 15 minutes, then it is cooled.
The polymer, in the form of beads, is separated from the mother liquors by centrifugation, washed with deionized water and dried in stove at 80°C.
The mother liquors show a dry residue at 160°C of about 0.6~ by weight, partly formed by the suspending agent (0.2~s by weight) and for the remaining fraction by acrylic polymer in the form of particles in emulsion.
The obtained polymer beads are dissolved in CHC13 and then reprecipitated in hexane.
10 The FT-IR analysis of the fraction soluble in hexane of the so obtained beads shows the additive presence. This confirms that the additive is wholly englobed in the beads themselves.
The beads obtained according to the methods described in Examples 2-5 were granulated by monoscrew extruder according to the usual methods for PMMA. The beads arP lnar3ar3 ;n a feedbox from which they are introduced in the extruder. A
Bandera TR30 monoscrew extruder is used, having the following characteristis:
Length/diameter (L/D) - 25 Flow-rate (Kg/h) _ 5 Extruder temperature (°C) lAt zone (15 cm from feeding) - 210 2nd zone (29 cm from feeding) - 230 3rd zone (59 cm from feeding) - 230 4"' zone (75 cm from feeding) - 220.
The Melt Flow Rate (M.f.r.) of the so obtained granules was measured, see Table 1.
The so obtained granules were injection molded so as to obtain specimen suitable to the determination of the thermal, optical and antistatic properties according to the methods indicated in Table 1.
For the thermal properties (Vicat) and antistatic (surface resistivity) the specimen are disks having 66 mm diameter and 3.2 mm thickness for the Vicat and 66 mm diameter and 1.6 mm thickness for the antistatic properties.
As to the optical properties (Transmittance Ts, Haze, Yellow Index Y.I.) the specimen are rectangular plates having 90 x 60 mm sizes and a 4 mm thickness.
The results are shown in Table 1.
EXAMPLE 9 (comparative) Example 8 was repeated using the polymer beads of Example 3 to which 3 phr of additive of formula (1) of Example 5 were added by extrusion.
The results are shown in Table 1.
The comparison of the results of Example 5, beads obtained with the antistatic agent directly in the polymeriza-tion process, and of Example 9, beads charged with the antistatic agent in extruder, reported in Table 1 shows that the antistatic properties are clearly better in Example 5 (lower resistivity value) compared with those of Example 9.
Moreover it is noted that the very good resistivity values of Example 5 are combined with clearly superior optical proper-ties, Haze and Y.I..
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Claims (10)
1. A process for preparing antistatic acrylic polymers wherein the acrylic monomers are polymerized in suspension, said acrylic monomers contain dissolved the antistatic additives selected from the following ones:
(1) C n H2n+1CO-N(CH2CH2OH)2 wherein n is an intger ranging from 9 to 13, preferably n=11;
(2) C n' H2n'+1N(CH2CH2OH)2 wherein n' is an integer ranging from 8 to 14, preferably n'=12;
(3) CH2(OR1)CH(OR2)CH2(OR3) or C(CH2OR1)(CH2OR2)(CH2OR3)(CH2OR4) wherein R1, R2, R3, R4 equal to or different from each other, are H or R, wherein R is a saturated or unsaturated C12-C18 alkylcarboxylate, preferably saturated or monounsaturated C18, in class (3) monoesters are the preferred compounds; or their mixtures; the amount of total antistatic agent being in the range 0.2-15 phr (for 100 parts of monomers), preferably 1-5 phr.
(1) C n H2n+1CO-N(CH2CH2OH)2 wherein n is an intger ranging from 9 to 13, preferably n=11;
(2) C n' H2n'+1N(CH2CH2OH)2 wherein n' is an integer ranging from 8 to 14, preferably n'=12;
(3) CH2(OR1)CH(OR2)CH2(OR3) or C(CH2OR1)(CH2OR2)(CH2OR3)(CH2OR4) wherein R1, R2, R3, R4 equal to or different from each other, are H or R, wherein R is a saturated or unsaturated C12-C18 alkylcarboxylate, preferably saturated or monounsaturated C18, in class (3) monoesters are the preferred compounds; or their mixtures; the amount of total antistatic agent being in the range 0.2-15 phr (for 100 parts of monomers), preferably 1-5 phr.
2. A process according to claim 1 wherein the product obtained under the foam of beads, with granulometry in the range 50-1,000 micron, is subsequently transformed into granules by extrusion.
3. A process according to claims 1-2 wherein the process is carried out in aqueous suspension.
4 . A process according to claim 3 , wherein the aqueous phase is totally or partially formed by the mother liquors obtained by a previous polymerization.
5. A process according to claim 4, wherein said mother liquors, optionally charged with an additionl amount of the suspending agent, contain at least 0.05% by weight of said suspending agent, preferably 0.1-0.5%.
6. A process according to claims 1-5 wherein as suspension stabilizers hydrosoluble macromolecular compounds having an affinity towards the monomer, which hinder the polymeric particles agglomeration, are used.
7. A process according to claim 6 wherein as suspending and stabilizing agents of the aqueous suspension, polymers selected from the homopolymers of compounds having the formula CH2 = CR a - CO - A - CR b R c -CH2 - SO3 M (I) are used, wherein: Ra = H, CH3; Rb and Rc, equal to or differnt, are H, C1-C8 alkyls anal M = alkaline, alkaline-earth metal or ammonium, A, = NH, O or NCH3, or the copolymers of said compounds with acrylic monomers in amounts in the range 0-40% by weight.
8. A process according to claim 6 wherein as suspending agents the polyvinylic alcohol or the poly (meth) acrylic acid are used.
9. A process according to claims 1-8 whereien the acrylic monomers are selected from C1-C8 alkyl acrylates or methacrylates such as, methyl(meth)acrylate, ethyl(meth) acrylate, propyl(meth)acrylate, isopropyl(meth)acrylate, butylacrylate, sec-butylmethacrylate, terbutylmethacrylate.
10. A process according to claim 9 wherein said acrylic monomers ar used singly or in admixture with each other, optionally in the presence of other monomers, in amounts of at most 50% by weight, containing double bonds such as styrene, alpha-methylstyrene, (meth)acrylonitrile, alkyl-cycloalkyl- or aryl-maleimides, butadiene, (meth)acrylic acid, (meth)acrylamide.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| ITMI98A001702 | 1998-07-23 | ||
| IT1998MI001702A IT1301847B1 (en) | 1998-07-23 | 1998-07-23 | SUSPENSION POLYMERIZATION PROCESS OF ACRYLIC MONOMERS |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2278115A1 true CA2278115A1 (en) | 2000-01-23 |
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ID=11380499
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002278115A Abandoned CA2278115A1 (en) | 1998-07-23 | 1999-07-21 | Suspension polymerization process of acrylic monomers |
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| Country | Link |
|---|---|
| KR (1) | KR20000011898A (en) |
| CA (1) | CA2278115A1 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| KR101707612B1 (en) * | 2015-07-24 | 2017-02-16 | 윤경화 | Lightweight radiant engine |
-
1999
- 1999-07-21 CA CA002278115A patent/CA2278115A1/en not_active Abandoned
- 1999-07-22 KR KR1019990029772A patent/KR20000011898A/en not_active Application Discontinuation
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| KR20000011898A (en) | 2000-02-25 |
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