PROCESS FOR THE PREPARATION OF A PURIFIED ACRYLAMIDO SULFONIC ACID MONOMER DERIVATIVE

Abstract: A process for the preparation of a purified monomer is disclosed which comprises the steps of reacting an impure monomer (A) wherein R<1> and R<2> are independently hydrogen or alkyl groups containing from 1 to about 6 carbon atoms, with (B) a substantially aqueous solution of an oxide or hydroxide of the structure MO or MOH wherein M is a Group IA or Group IIA metal, or an amine of the structure NR<3>R<4>R<5> wherein R<3>, R<4> and R<5> are independently hydrogen or alkyl, alkanol or alkoxy groups containing from 1 to about 12 carbon atoms, wherein the molar ratio of (A):(B) is from about 1:1-2 for Group IA metals, 2:1-2 for Group IIA metals or ratio of moles of (A) to nitrogens of (B) is from about 1:1-2 nitrogens to form a salt, and recovering a purified salt by crystallization by subjecting the aqueous solution to changes in temperature and/or pressure and/or concentration.

Description: TITLE: PROCESS FOR THE PREPARATION OF A PURIFIED ACRYLAMIDO SULFONIC ACID MONOMER DERIVATIVE FIELD OF THE INVENTION This invention relates to a process for preparing a purified sulfonic acid monomer salt. The purification is accomplished by a crystallization of a derivative of the monomer from an aqueous solution. BACKGROUND OF THE INVENTION Previously purified derivatives of acrylamido sulfonic acid monomers are prepared utilizing the already purified sulfonic acid. U.S. Patent 4,337-,215 (Doi et al, June 29, 1982) relates to a purification process for the efficient preparation of high-purity 2-acrylamido-2-methyl- propanesulfonic acid (hereinafter referred to simply as AMPS, a registered trademark of The Lubrizol Corpora¬ tion). In this process, the starting material is crude AMPS crystals which have been obtained by washing precipitates from the reaction mixture obtained by any of the conventional reaction methods. The crude crystals are dissolved in hydrous acetic acid containing 5 to 40% water. The quantity of the hydrous acetic acid required to completely dissolve the desired amount of AMPS at 90°C depends on the water content. When the hydrous acetic acid has a water content of 10%, it is used in an amount about 4 to 5 times the weight of crude crystals. The purified crystals are collected by filtration of this solution after the solution is cooled to about 10 to 20'C. U.S. Patent 4,701,283 (Itoh et al, October 20, 1987) relates to a process for preparing amidoalkanesulfonic acids and derivatives, such as salts thereof, as well as copolymer-coated solid materials, copolymer emulsions and pigment dispersants in which the copolymer is obtained by copolymerizing such an amidoalkanesulfonic acid derivative with another monomer. U.S. Patent 4,650,614 (Jevne et al, March 17, 1987) provides - a method for purifying reaction grade 2-acrylamido-2-methylpropanesulfonic acid, as obtained commercially, by a. short duration, mild heating of the acid in a slurry with a volatile liquid monohydric alcohol followed by acid recovery via decantation or other form of separation and subsequent drying of the wet solid acid. SUMMARY OF THE INVENTION The present invention is a process for the preparation of a purified monomer comprising the steps of reacting an impure monomer 1 2 wherein R and R are independently hydrogen or alkyl groups containing from 1 to about 6 carbon atoms, with (B) a substantially aqueous solution of an oxide or hydroxide of the structure MO or MOH wherein M is a Group IA or Group IIA metal, or an amine of the structure 3 4 5 . 3 4 5 NR R R wherein R , R and R are independently hydrogen or alkyl, alkanol or alkoxy groups containing from 1 to about 12 carbon atoms, wherein the molar ratio of (A) : (B) is from about 1:1-2 for Group IA metals, 2:1-2 for Group IIA metals or ratio of moles of (A) to nitrogens of (B) is from about 1:1-2 nitrogens to form a salt, and recovering a purified salt by crystallization by subjecting the aqueous solution to changes in temperature and/or pressure and/or concentration. DESCRIPTION OF THE DRAWINGS Fig. 1 is a chromatograph of impure AMPS. Fig. 2 is a chromatograph of a purified sodium salt of AMPS. .. DETAILED DESCRIPTION OF THE INVENTION Generally this invention provides a process for purifying a monomer of a sulfonic acid derivative. A commercially obtained (A) monomer of a sulfonic acid is reacted with (B) a substantially aqueous solution of an oxide, hydroxide or an amine. The reaction of (A) and (B) forms a salt. The invention lies in being able to obtain a salt of high purity. This high purity salt has utility as a monomer to produce ultra high molecular weight copolymers or ho opolymer of said monomer. The prepared polymers function on flocculants, fluid loss and cementing polymers. .Al The Monomer of a Sulfonic Acid The sulfonic acid wherein R 1 and R2 are as defined above can be prepared by several different schemes. One method involves reacting acrylonitrile with a β-hydroxyalkanesulfonic acid CH =CHC≡N + H0-C- UCHl. -SW0,H > (A) i 3 12 ~ R Another method involves reacting acrylonitrile with an olefin such as propylene or a butylene in the presence of fuming sulfuric acid. CH 2 -CHC=N + olefin + acid > (A) In any event, the (A) component is a starting material - or this invention and as such is commercially readily available. The preferred (A) is one wherein R 2 and R are both methyl groups to give 2-acrylamido-2-methylpropanesulfonic acid. (B) The Oxide. Hydroxide or Amine Component (B) is a substantially aqueous solution of a metal oxide, MO; a metal hydroxide, MOH; or an amine. As a metal oxide or hydroxide, preferred are the Group IA and Group IIA metals as identified in the Periodic Table of the Elements published by Johnson Mattey, 1989. Specifically, these metals are lithium, sodium, potassium, magnesium and calcium. The most preferred Group IA metal is sodium and the most preferred Group IIA metal is magnesium. Of the metal oxide or hydroxide, it is preferred to employ a metal hydroxide, specifically sodium hydroxide. Component (B) may also be a substantially aqueous solution of an amine NR R R wherein R , R and are independently hydrogen or alkyl, alkanol or alkoxy groups containing from 1 to about 12 carbon atoms, preferably from 1 to about 8 carbon atoms and most preferably from 1 to about 4 carbon atoms. It is most desirable to employ an aqueous solution of ammonia wherein R 3=R4=R5=hydrogen. In an alternative embodiment, component (B) may be a substantially aqueous solution of an amine of the structure R 3R4NR6NR7 wherein R3 and R4 are as defined above, R is an alkylene group containing from 1 to about 6 carbon atoms and R 7 i.s R3R4 or -CH^CH-XCH-CH-- wherein X is nitrogen or oxygen. The term "substantially aqueous solution" means that water is the predominant solvent. Water comprises at least about 90%, preferably at least about 95%, and most preferably at least about 99% by weight of the solvent. Other solvents that may be present are alcohols, aldehydes, ketones, esters and ethers of 4 carbon atoms, or less, -amides such as dimethyl formamide or sulfoxides such as dimethyl sulfoxide. When R 3, R4. and R5 are alkyl groups, an illustrative but non-exhaustive list is methyl, ethyl, n-propyl, isopropyl, n-butyl, 2-methylpropyl, n-pentyl, 2-methylbutyl, 3-methylbutyl, neopentyl, n-hexyl, 2- ethylpenty1, 3-methylpentyl, 4-methylpentyl, 2-ethylbuty1, 3-ethylbuty1, 2,3-dimethylbuty1, 2,2-dimethylbutyl, 3,3-dimethylbuty1 and the isomeric heptyls, octyls, nonyls, decyls, undecyls and dodecyls. As alkanols, R 3 , R 4 and R 5 are -CH 2 OH, -CH 2 CH 2 OH, -CH-CH-CH-OH, -CH_CHCH_, -CH_ CH_ CH_ CH_ OH , -CH- CH_ CHCH_ , 2 2 2 2| 3' 2 2 2 2 2 2- 3 OH OH OH I -CH 2 CHCH 2 CH 3 , -CH 2 CHCH 2 OH, -CH 2 CCH 3 , -CH 2 CH 2 CH 2 CH 2 CH 2 OH, OH CH 3 CH 3 -CH2-CH2-CH2-C|HCH3-,' -CH2_CH2_C|HCH2-CH-3, -CH2_C|HCH2-CH2-CH_3, OH OH OH -CH 2 CH-CHCH 3 , -CH 2 CH-CHCH 3 , -CH^CCH^ OH CH 3 CH 3 OH OH -CH_ C CH-CH-, the isomeric hexanols, heptanols, OH octanols, nonanols, decanols, undecanols and dodecanols. As alkoxy groups, R 3, R4 and R5 are -OCH_, -OCH-CH-, -OCH-CH-CH-, -OCHCH,, -OCH- CH- CH_ CH_ , -OCH- CHCH- , 2 2 3 i 3' 2 2 2 3 2 | 3 CH 3 CH 3 -OC-CH 3 , -OCH 2 CH 2 CH 2 CH 2 CH 3 , -OCH 2 CH 2 CH CH 3 , CH 3 CH 3 -OCH 2 CHCH 2 CH 3 , -OCHCH 2 CH 2 CH 2 CH 3 , -OCH 2 CCH 3 , CH ^ CH„ CH„ -OCH 2-CiHCH3-,' -OCiH-CiHCH3,,' CH 2 CH 3 CH 3 CH, the isomeric hexoxys, heptoxys, octoxys, nonoxys, decoxys, undecoxys and dodecoxys. When the amine is R 3R4NR6NR7, R3 and R4 are as earlier defined and R is an alkylene group containing from 1 to about 6 carbon atoms, preferably from 1 to about 3 carbon atoms. R may be methylene, ethylene, or isomers of propylene, butylene, pentylene or hexylene. Most preferably, R is ethylene. R is R R or -CH 2 XH 2 XCH 2 CH 2 - wherein X is oxygen or nitrogen. Some of the preferred amines of the formula R 3 R 4 NR 6 NR 7 are H 2 NCH 2 CH 2 NH 2 , H 2 NCH 2 CH 2 CH 2 NH 2 , CH,NHCH * 2CH2NH2,' , / CH3-NH CH2-CH2-CH2-CH2-Nv i0 . No attempt is made to purify component (A) prior to salt formation. Component (B) is typically prepared in an aqueous solution. ' Component (A) may be in aqueous solution or substantially aqueous free. By substantially aqueous free it is meant that free water is present at no more than about 2%, and preferably, no more than about 1% on a weight basis. The reaction of component (A) with component (B) produces a salt. There is no criticality in employing an extremely large excess of (B) . From as little as 1 mole percent excess up to about 20 mole percent excess is envisaged. Component (B) is an aqueous solutions having a percent weight of water of from about 15 to about 95, preferably from about 25 to about 95 and most preferably from about 50 to about 90. To effect salt formation, component (A) may be added to component (B) or vice-versa. In practice, component (A) is usually added to component (B) . Salt formation is exothermic and the exotherm is utilized to solubilize the maximum amount of salt in water. After the salt is formed in an aqueous medium, it is filtered to remove any solid impurities. The aqueous salt is then cooled and the solid salt is obtained as a purified product by crystallization. The reaction of (A) and (B) to form a salt occurs at a temperature of from about -20 'C up to about the decomposition of any reactant or product. Preferably, the salt formation is conducted at a temperature of from about 20*C up to about 75*C and most preferably from about 30 β C up to about 75*C. The molar ratio of (A) : (B) to effect salt formation is dependent on the nature of (B) . When (B) is a Group IA metal, the molar ratio of (A) : (B) is from about 1:1-2, preferably 1:1-1.10 and most preferably from about 1:1-1.05. When (B) is a Group IIA metal, the. molar ratio of (A) : (B) is from about 2:1-2, preferably 2:1-1.10 and most preferably from about 2:1-1.05. When B is an amine of the formula NR R R , the ratio of moles of (A) to nitrogens of (B) is from about 1:1-2, preferably 1:1-1.10 and most preferably from about 1:1-1.05. When B is an amine of the formula R R NR NR the ratio of moles of (A) to nitrogens of (B) is from about 2:2-3, preferably 2:2-2.1 and most preferably from about 2:2-2.05. However, when R 7 is -CH CH NCH.CH -, then the H ratio of moles of (A) to nitrogens of (B) is from about 3:3-4, preferably 3:3-3.1 and most preferably from about 3:3-3.05. The salt so formed is in aqueous solution. The aqueous solution is filtered to remove solid impurities, and the salt is recovered by subjecting the aqueous solution to changes in temperature and/or pressure and/or concentration. By increasing the temperature, water is removed which increases the amount of salt present relative to the remaining water. Removal of water at an increased temperature may be facilitated by decreasing the pressure. However, water may also be removed by decreasing the pressure even at ambient temperature. By decreasing the temperature, the salt is removed due to a shift in the solubility of salt relative to temperature. At any rate, the salt is recovered by effecting supersaturation. The two methods for providing supersaturation are the thermal swing and evaporative crystallization. In the thermal swing, a saturated solution is cooled to reduce the solubility of the desired salt. As the solubility is decreased, the salt is crystallized out of solution. In the evaporative crystallization, water is removed from the aqueous solution either through heating or reduced pressure or a combination of heating and reduced pressure. Less water present to effect solution causes the desired salt to crystallize. The thermal swing and evaporative crystallization may be carried out batchwise or continuously. Component (A) is ' a known monomer in the polymer field. The salt of (A) and (B) also has utility as a monomer. As such, it becomes necessary to ensure that the salt does not undergo polymerization or any other undesired reaction. It is necessary that the aqueous solution be maintained at a temperature of between about -20°C to about 75"C. Temperatures above about 77°C lead to rapid formation of by-products by the addition of water across the double bond in component (A) . Temperatures above about 77 " C also leads to some salt polymer formation. Temperatures below about -20°C cause the formation of ice crystals which cause problems during separation of the salt from the aqueous solution. The pH of the aqueous salt solution is to be maintained at between about 7 to about 12.5 A pH of less than 7 causes rapid polymerization and a pH of greater than 12.5 causes rapid by-product formation at temperatures above 75*C. In order to prevent polymerization, it is necessary to maintain both temperature and pH, as discussed above. It is also helpful to utilize a polymerization inhibitor. Many polymerization inhibitors are available. An especially preferred polymerization inhibitor is hydroquinone monomethyl ether. This inhibitor requires the presence of dissolved oxygen in the aqueous solution in order to be effective. During the evaporative crystallization water is distilled away under reduced pressure in order to lower the distillation temperature and minimize by-product formation. A constant purge of air or any other oxygen bearing gas stream to the distillation vessel must be maintained or polymerization will occur. The following examples illustrate preparation of the salt. Example 1 In a 2-liter flask is prepared a solution of 87.2 parts (2.18 moles) sodium hydroxide in 461 parts water and purged with compressed air at 0.5 cubic feet per hour. To this solution is slowly added 452 parts (2.18 moles) AMPS monomer and 0.07 part hydroquinone monomethyl ether in 400 parts water while stirring and maintaining the air purge. The temperature is maintained at between about 24-40'C. The contents are then filtered to remove insolubles prior to crystallization. Example 2 Charged to a 5-liter flask is a solution of 124 parts (3.1 moles) sodium hydroxide and 0.13 parts hydroquinone monomethyl ether in 400 parts water. This is followed by the addition of 100 parts of an aqueous solution of impure AMPS prepared by reacting propylene and acrylonitrile in the presence of fuming sulfuric acid. This solution contains 3.05 moles AMPS based on a neutralization number to phenolphthalein of 275. In the chromatograph of Fig. 1, AMPS is identified at 1. The impurities of this AMPS are identified at 2-13. The amount of impurity is a function of the area under 2-13 relative to the area under 1. Air is bubbled below the surface at 0.5 cubic feet per hour while maintaining the temperature at between 30-50 β C. The contents are filtered to remove insolubles prior to crystallization. Table I outlines Examples 3-8 wherein 1000 parts of an impure aqueous solution of AMPS as defined in Example 2 is reacted with various metal oxides or metal hydroxides as component (B) to form the salt. These procedures are according to Example 2. TABLE I Table II outlines Examples 9-17 wherein 1000 parts of an impure aqueous solution of AMPS as defined in Example 2 is reacted with various amines of the structure NR3R4R5 to form the salt. These procedures are according to Example 2. - ι: f-l i-. rq i-I r. t-. .- * .-. ^j* ^sj* ^J* ^J* '■^' ^J* 'SJ' "^* ^J* o o o o o o o o o •^j* *^j* ^π* ^r ^Γ ^3^ ^* * « ^T ^3^ Table III outlines Examples 18-25 wherein 1000 parts of an impure aqueous solution of AMPS as defined in Example 2 is reacted with various amines of the structure R R NR NR to form the salt. These procedures are according to Example 2. The temperature range is from about 40-65*C. TABLE III Moles R 3 R 4 NR 6 NR 7 Example Moles AMPS in 400 parts water R R" R ^ R' 19 4.0 2.05 20 4.0 2.05 21 4.0 2.05 22 4.0 2.05 23 4.0 2.05 24 4.0 2.05 25 4.0 1.37 H The following examples illustrate purification of the salt by crystallization by both the thermal swing and evaporation crystallization methods. Example 26 - Thermal Swing The filtered contents of Example 2 are added to a 5-liter flask immersed in a bath set up with coils for cooling. Air is blown below the surface at 0.25 cubic feet per hour and stirring is begun. The contents of the flask are cooled to -10*C by pumping brine through the cooling coils. The temperature is maintained at -10"C for 8 hours. The contents are filtered through paper and the product is obtained as a solid having the following analyses: % Sodium 9.91, % sulfur 13.92, % nitrogen 6.05. In the chromatograph of Fig. 2, the sodium salt of AMPS is identified at 20. The impurities are identified at 21-24. In comparing Fig. 2, the purified salt of Example 26, with Fig. 1, the impure starting material, it is readily apparent that the impurities 21-24 residing with the purified salt are both less in number and in relative concentration to the starting material impurities 2-13. Example 27 - Evaporative Crystallization The filtered contents of Example 2 are added to a 3-liter flask equipped for distillation and containing an air purge tube. The contents are heated and stirred while air is blown below the surface at 0.5 cubic feet per hour. The contents are heated to 50°C while under a vacuum of 700 millimeters of mercury. As water is removed, more and more solids appear in the flask. Water is removed until that point where stirring becomes difficult. The contents are then transferred to a centrifuge where the solid product is obtained having the following analyses: % sodium 9.94, % sulfur 13.89, % nitrogen 6.03. While the invention has been explained in relation to its preferred embodiments, it is to be understood that various modifications thereof will become apparent to those skilled in the art upon reading the specification. Therefore, it is to be understood that the invention disclosed herein is intended to cover such modifications as fall within the scope of the appended claims.

Claims: What is claimed is: 1. A process for the preparation of a purified monomer comprising the steps of reacting an impure monomer (A) wherein 1 and R2 are independently hydrogen or alkyl groups containing from 1 to about 6 carbon atoms, with (B) a substantially aqueous solution of an oxide or hydroxide of the structure MO or MOH wherein M is a Group IA or Group IIA metal, or an amine of the structure NR 3R4R5 wherei.n R3, R4 and R5 are independently hydrogen or alkyl, alkanol or alkoxy groups containing from 1 to about 12 carbon atoms, wherein the molar ratio of (A) : (B) is from about 1:1-2 for Group IA metals, 2:1-2 for Group IIA metals or ratio of moles of (A) to nitrogens of (B) is from about 1:1-2 nitrogens to form a salt, and recovering a purified salt by crystallization by subjecting the aqueous solution to changes in temperature and/or pressure and/or concentration. 2. The process according to claim 1 wherein the Group I metals are lithium, sodium or potassium. 3. The process according to claim 1 wherein the Group II metals are magnesium or calcium. .4. The process according to claim 1 wherein the molar ratio of (A) : (B) is from about 1:1-1.05 for Group IA metals to form a salt. ι 5. The process according to claim 1 wherein R and R 2 are independently methyl, ethyl or propyl. 6. The process according to claim 1 wherein R , R and R are independently hydrogen or alkyl, alkanol or alkoxy groups containing from 1 to about 12 carbon atoms. 7. The process according to claim 1 wherein the purified•• salt is recovered by subjecting the aqueous solution to changes in temperature. 8. The process according to claim 1 wherein the Group IA metal is sodium. 9. The process according to claim 1 wherein the Group IIA metal is magnesium. 10. The process according to claim 1 wherein the purified salt is recovered by subjecting the aqueous solution to changes in pressure. 11. The process according to claim 6 wherein R 3, R4 and R 5 are independently hydrogen or alkyl, alkanol or alkoxy groups containing from 1 to about 8 carbon atoms. 12. The process according to claim 4 wherein R 1 and 2 R are methyl. 13. The process according to claim 1 wherein the molar ratio of (A) : (B) is from about 2:1-1.05 for Group II metals to form a salt. 14. The process according to claim 11 wherein R3, R and R are independently hydrogen or alkyl, alkanol or alkoxy groups containing from 1 to about 4 carbon atoms. 15. The process according to claim 1 wherein the ratio of moles of (A) to nitrogens of (B) is from about 1:1-1.05 to form a salt. 16. The process according to claim 1 wherein the purified salt is recovered by subjecting the aqueous solution to changes in concentration. 17. • The process according to claim 14 wherein R 3 , . R 4 and R5 are hydrogen. • 1 18. The process according to claim 1 wherein R and R 2 are methyl, (B) is NaOH and the molar ratio of (A) : (B) is from about 1:1-1.05. 19. A process for the preparation of a purified monomer comprising the steps of reacting an impure monomer O R 1 Ii I (A) CH =CHCN-C-CH_SO_H H R^ wherein R 1 and R2 are independently hydrogen or alkyl groups containing from 1 to about 6 carbon atoms, with (B) a substantially aqueous solution of an amine of 3 4 6 7 . 3 4 the structure R R NR NR wherein R and R are independently hydrogen or alkyl, alkanol or alkoxy groups containing from 1 to about 12 carbon atoms, R is an alkylene group containing from 1 to about 6 carbon atoms 7 3 4 and R is R R or -CH 2 CH 2 XCH CH 2 ~ wherein X is nitrogen or oxygen. wherein the ratio of moles of (A) to nitrogens of (B) is from about 2:2-3 to form a salt, with the proviso that when X is nitrogen, the (A) : (B) ratio is from about 3:3-4, and recovering a purified salt by crystallization by subjecting the aqueous solution to changes in temperature and/or pressure and/or concentration. 20. The process according to claim 19 wherein R 2 and R are independently methyl, ethyl or propyl. 21. The process according to claim 19 wherein the purified • salt is recovered by subjecting the aqueous solution to changes in temperature. 22. The process according to claim 19 wherein the purified salt is recovered by subjecting the aqueous solution to changes in pressure. 23. The process according to claim 20 wherein Rl 2 and R are methyl. 24. The process according to claim 19 wherein the ratio of moles of (A) to nitrogens of (B) is from about 2:2-2.05 to form a salt. 25. The process according to claim 19 wherein the purified salt is recovered by subjecting the aqueous solution to changes in concentration. 26. The process according to claim 19 wherein R 7 is R R comprising hydrogen or alkyl, alkanol or alkoxy groups containing from 1 to about 4 carbon atoms. 27.. The process according to claim 19 wherein R is an alkylene group containing from 1 to about 3 carbon atoms. 28. The process according to claim 19 wherein R7 is R 3R4 comprising hydrogen. 29. The process according to claim 19 wherein R 7 is -CH 2 CH 2 CH 2 CH 2 - wherein X is oxygen. AMENDED CLAIMS [received by the International Bureau on 29 October 1992 (29.10.92) ; original claims 1-29 replaced by amended claims 1-18 (3 pages)] 1. A process for the preparation of a purified monomer comprising the steps of reacting an impure monomer wherein R, and R j are independently hydrogen or alkyl groups containing from 1 to about 6 carbon atoms, with (B) a substantially aqueous solution of an oxide or hydroxide of the structure MO or MOH wherein M is a Group IA or Group IIA metal, or an amine of the structure NR 3 R 4 R 5 wherein R 3 , R 4 and R 5 are independently hydrogen or alkyl, alkanol or alkoxy groups containing from 1 to about 12 carbon atoms, wherein the molar ratio of (A) : (B) is from about 1:1-2 for Group IA metals comprising lithium, sodium or potassium, 2:1-2 for Group IIA metals comprising magnesium or calcium or ratio of moles of (A) to nitrogens of (B) is from about 1:1-2 nitrogens to form a salt, and recovering a purified salt by crystallization by subjecting the aqueous solution to changes in temperature and/or pressure and/or concentration. 2. The process according to claim l wherein the purified salt is recovered by subjecting the aqueous solution to changes in temperature. 3. The process according to claim 1 wherein the Group IA metal is sodium. 4. The process according to claim 1 wherein the Group IIA metal is magnesium. 5. The process according to claim 1 wherein the purified salt is recovered by subjecting the aqueous solution to changes in pressure. 6. The process according to claim 1 wherein R 1 and R 2 are methyl. 7. The process according to claim 1 wherein the purified salt is recovered by subjecting the aqueous solution to changes in concentration. 8. The process according to claim 1 wherein R 3 , R 4 and R 5 are hydrogen. 9. The process according to claim 1 wherein R 1 and R 2 are methyl, (B) is NaOH and the molar ratio of (A) : (B) is from about 1:1-1.05. 10. A process for the preparation of a purified monomer comprising the steps of reacting an impure monomer wherein R 1 and R 2 are independently hydrogen or alkyl groups containing from 1 to about 6 carbon atoms, with (B) a substantially aqueous solution of an amine of the structure R 3 RNR 6 NR 7 wherein R 3 and R 4 are independently hydrogen or alkyl, alkanol or alkoxy groups containing from 1 to about 12 carbon atoms, R 6 is an alkylene group containing from 1 to about 6 carbon atoms and R 7 is R 3 R 4 or -CH g CH- j XCH g CH.,- wherein X is nitrogen or oxygen, wherein the ratio of moles of (A) to nitrogens of (B) is from about 2:2-3 to form a salt, with the proviso that when X is nitrogen, the (A) : (B) ratio is from about 3:3-4, and recovering a purified salt by crystallization by subjecting the aqueous solution to changes in temperature and/or pressure and/or concentration. 11. The process according to claim 10 wherein the purified salt is recovered by subjecting the aqueous solution to changes in temperature. 12. The process according to claim 10 wherein the purified salt is recovered by subjecting the aqueous solution to changes in pressure. 13. The process according to claim 10 wherein R 1 and R 2 are methyl. 14. The process according to claim 10 wherein the purified salt is recovered by subjecting the aqueous solution to changes in concentration. 15. The process according to claim 10 wherein R 7 is R 3 R 4 comprising hydrogen or alkyl, alkanol or alkoxy groups containing from 1 to about 4 carbon atoms. 16. The process according to claim 10 wherein R 6 is an alkylene group containing from 1 to about 3 carbon atoms. 17. The process according to claim 10 wherein R 7 is R 3 R 4 comprising hydrogen. 18. The process according to claim 10 wherein R 7 is - CH 2 CH 2 XCH 2 CH 2 - wherein X is oxygen.

Inventors: BURK W MICHAEL, GOODLIVE STEVEN A, HENRY WILLIAM S, QUINN ROBERT E, BURK, W., MICHAEL, GOODLIVE, STEVEN, A., HENRY, WILLIAM, S., QUINN, ROBERT, E.
Applicants: LUBRIZOL CORP, THE LUBRIZOL CORPORATION
Application year: 1992
Main classification: C07C309
IPC codes: C07C303, C07C309