PROCESS FOR RECOVERY OF METHACRYLIC ACID

Abstract: Process for treating the reaction product of propionic acid and formaldehyde to recover methacrylic acid from an acqueous effluent wherein said effluent contains methacrylic acid, unreacted formaldehyde, unreacted propionic acid, water and by-products.

Description: PROCESS FOR RECOVERY OF METHACRYLIC ACID Field Of The Invention In general, the field of this invention relates to a method of distilling the reaction product stream from reaction of a saturated aliphatic monocarboxylic acid compound and formaldehyde, said reaction product stream comprising saturated aliphatic monocarboxylic acid com¬ pound, an alpha, beta-ethylenically unsaturated aliphatic monocarboxylic acid compound of one more carbon atom than the starting saturated aliphatic monocarboxylic acid com¬ pound, water and formaldehyde wherein unreacted saturated aliphatic monocarboxylic acid compound and unreacted for¬ maldehyde are removed from the product stream and can be recycled back to the reactor. In more specific terms, the field of this invention relates to a process for recovery of methacrylic acid from an aqueous effluent obtained by the vapor phase aldol-type condensation of propionic acid and formal- dehyde wherein the effluent contains methacrylic acid, unreacted propionic acid, unreacted formaldehyde, water and by-products. The unreacted propionic acid and unreacted formaldehyde are removed from the aqueous effluent and can be recycled. Background Of The Invention Unsaturated acids, such as methacrylic and acrylic acids, acrylonitrile, and the esters of such acids, such as methyl methacrylate, are widely used for the produc¬ tion of corresponding polymers, resins and the like. Various processes and catalysts have been proposed for the conversion of alkanoic acids, such as acetic acid or propionic acid, and formaldehyde to the corresponding unsaturated monocarboxylic acids, e.g., methacrylic acid, by an aldol-type reaction. Generally, the reaction of acid and formaldehyde takes place in the vapor or gas phase while in the presence of a basic or acidic cata¬ lyst. The literature is replete with disclosures of the reaction of aliphatic carboxylic acid compounds with for- " aldehyde to produce alpha, beta-ethylenically unsatu¬ rated aliphatic monocarboxylic acid compounds of one more carbon atom than in the saturated carboxylic acid. For every molecule of alpha, beta-ethylenically unsaturated aliphatic monocarboxylic acid produced there is one molecule of water by-product. It is necessary to sepa¬ rate the alpha, beta-ethylenically unsaturated carboxylic acid compound, formaldehyde and the starting unsaturated carboxylic acid. In the case of methacrylic acid, this means that the methacrylic acid must be separated from propionic acid, formaldehyde and water. This separation presents several problems since each of the components are water soluble and because propionic acid and methacrylic acid have boiling points that are so close that it is difficult to fractionate one from the other. Further, the separation is complicated by the fact that mefhacrylic acid has a tendency to homopolymerize and formaldehyde, if water is removed from the system, also has a tendency to homopoly¬ merize. Of the various alpha, beta-ethylenically unsatu¬ rated compounds, it is generally recognized that methacrylic acid has one of the greatest tendencies to polymerize and it is extremely difficult to handle at elevated temperatures. In this regard, we have found that the presence of certain reaction by-products greatly increase the propensity of methacrylic acid to homopoly¬ merize. Specifically, alpha-, beta- unsaturated ketones, i.e., ethylisopropenyl ketone and 2,5-dimethylcyclopenten-l-one, have been shown to greatly increase the degree of methacrylic acid homopolymeriza- tion. Additionally, methacrylic acid, propionic acid and formaldehyde individually form binary azeotropes with water. The boiling points of the three binary azeotropes are within 1°F of each other and are thus exceedingly difficult to separate. The following table lists boiling points and weight percentages of binary azeotropes of water and methacrylic acid, propionic acid and formal¬ dehyde at 760 mm Hg. t Wt % B.P. % H. °F .—O Methacrylic acid 23.1 76.9 210.7 Propionic acid 17.8 82.2 210.4 Formaldehyde 18.25-21. .0 79.0-81. .75 210.4 In somewhat greater detail, the invention relates to a process for an aldol-type condensation of a saturated aliphatic monocarboxylic acid compound and an aldehyde wherein said monocarboxylic acid is propionic acid and said aldehyde is formaldehyde. As is well-known, an aldol-type condensation can be base-catalyzed and is sub¬ ject to ready dehydration if the β-hydroxyl group is adjacent to an α-hydrogen atom. The product is an α, β-unsaturated acid of one more carbon atom than the ori- ginal unsaturated aliphatic monocarboxylic acid, when the reacting aldehyde is formaldehyde. The reaction using propionic acid and formaldehyde is: CH 3 CH 2 COOH + HCHO ÷ CH = C(CH 3 )COOH + H 2 0 In the prior art a number of methods have been taught to overcome the aforementioned problems. A method for recovery of methacrylic acid from an aqueous effluent obtained by vapor phase condensation of formaldehyde and propionic acid, where the effluent contains unreacted formaldehyde and unreacted propionic acid, is taught in U.S. Patent 4,040,913, wherein the recovery steps include extracting the effluent with an organic solvent capable of azeotroping with propionic acid to obtain an organic phase and an aqueous raffinate; distilling the organic phase to remove 50-100% of the unreacted propionic acid and leaving as bottoms remaining propionic acid and methacrylic acid; distilling the bottoms to obtain methacrylic acid as bottoms; and distilling the aqueous raffinate with an entrainer to obtain dilute aqueous for¬ maldehyde overhead which is further concentrated by dis- tillation. The aqueous raffinate and organic phase are separated by decantation. Use of selective solvents for recovering unsaturated acids such as acrylic acid and methacrylic acid from aqueous mixtures is taught in the prior art. For example, U.S. Patent 3,414,485 teaches a method of removing water from methacrylic acid in a two-stage pro¬ cess. In the first stage, methacrylic acid is extracted with an organic solvent which forms a minimum-boiling azeotrope with water. Suitable organic solvents include o-, m- and p_-xylene, toluene, n.-octane, monochloroben- zene, methylamylketone, ligroin and methyl methacrylate monomer. U.S. Patent 3,478,093 teaches use of a lactam having 4 to 7 ring members and a hydrocarbon radical sub- stituent on the nitrogen atom as an extraction solvent to separate methacrylic acid from aqueous mixtures. U.S. Patent 3,781,332 teaches use of a dual mixture containing methyl or ethyl methacrylate and not more than 50% of xylene, ethyl benzene or a mixture thereof. U.S. 4,142,058 teaches use of a mixed solution of methyl methacrylate and toluene to separate methacrylic acid from an aqueous solution containing acetic acid. U.S. 4,147,721 teaches use of methyl n-propyl ketone. Initially, it was believed by workers in this labo¬ ratory that it would be possible to separate methacrylic acid from propionic acid, formaldehyde and water by extraction and fractional distillation using a suitable solvent, such as an aliphatic hydrocarbon of from about 6 to 12 carbon atoms, as is taught in U.S. Patent 4,409,128 or G.B. Patent 2,001,315B. Unfortunately, attempts to implement the separation led to solid paraformaldehyde formation in the column between the feed location and the top of the column resulting in plugging of the column. The separation of these products is, of course, complicated by the fact that the unreacted saturated ali¬ phatic carboxylic acid and formaldehyde must be recovered and returned to the main reactor in order to have an eco- nomically attractive process. Accordingly, the formation of solid paraformaldehyde in the column must be manage¬ able from both an operational point of view and an economic point of view. Likewise, it is desirable to minimize the amount of unreacted formaldehyde that must be processed before returning same to the reactor. The general object of this invention is to provide an improved method of treating the reaction product stream comprising the alpha, beta-ethylenically unsatu¬ rated aliphatic monocarboxylic acid compound of one more carbon atom than the starting saturated monocarboxylic acid compound, the saturated monocarboxylic acid com¬ pound, water, formaldehyde and by-products. A more spe¬ cific object of this invention is an improved method of separating methacrylic acid, propionic acid, water, for- maldehyde and by-products. The objects of this invention can be attained by distilling the reaction product of a saturated aliphatic monocarboxylic acid compound and a formaldehyde compound comprising an alpha, beta-ethylenically unsaturated ali- phatic monocarboxylic acid compound of one more carbon atom than the starting saturated aliphatic monocarboxylic acid compound, water and by-products, which comprises fractionally distilling said reaction products whereby a sidestream is removed from a location above the location of the feed stream input to the distillation column. In those cases where a distillation column is not in direct contact with a vessel or a reactor containing catalyst and is downstream from the reactor, the location of the sidedraw is typically located such that at least 10 (wt)% of the unreacted formaldehyde, and at least 10 (wt)% of the unreacted propionic acid in the column feed is removed from the column in the sidestream. The side- stream is composed of no more than 50 (wt)% water plus methacrylic acid. In a preferred method, the reaction products are distilled together with a substantially non-reactive compound capable of acting as a water-en- trainer and of breaking a water azeotrope of said satu¬ rated aliphatic carboxylic acid compound under conditions whereby (1) a major proportion of the ethylenically unsaturated monocarboxylic acid compound remains in the bottom of the column, (2) a major portion of the water, a portion of the formaldehyde compound and a major portion of the compound capable of acting as a water-entrainer and of breaking or preventing the formation of said azeo¬ trope are removed overhead and (3) a sidestream is removed below the top of the distillation column comprising water, a major portion of formaldehyde and a substantial proportion of saturated aliphatic carboxylic acid. In the case of the separation of the reaction prod¬ ucts of methacrylic acid, propionic acid, formaldehyde and water, we have found that by removing a sidestream below the top of the distillation column, it is possible to recycle a substantial portion of the unreacted formal¬ dehyde and propionic acid to the reactor and avoid the polymerization and plugging of the distillation column by polymerized formaldehyde. In addition, a major advantage of using a side draw stream and directly recycling this stream to the metha¬ crylic acid synthesis reactor is the reduced costs in the overall process which accrue because unreacted propionic acid and formaldehyde do not have to be separated and individually purified. In a preferred method of operation, the unreacted propionic acid and formaldehyde are recycled to the inlet ports of the reactor and employed to produce methacrylic acid. Summary Of The Invention A method is disclosed of distilling the reaction products of a saturated aliphatic monocarboxylic acid compound and formaldehyde compound, said reaction prod¬ ucts comprising saturated aliphatic monocarboxylic acid compound, alpha, beta-ethylenically unsaturated aliphatic monocarboxylic acid compound of one more carbon atom than the starting saturated aliphatic monocarboxylic acid com¬ pound, water, formaldehyde and by-product which comprises fractionally distilling said reaction product whereby a sidestream is removed below the top of the distillation column comprising water, a major portion of unreacted formaldehyde and a substantial proportion of unreacted saturated aliphatic monocarboxylic acid. Description And Preferred Embodiments Of The Invention The process of this invention will be understood from the following description and examples. The process of this invention is a process for the separation of alpha-, beta-ethylenically unsaturated monocarboxylic compounds of one more carbon atom than the starting saturated aliphatic monocarboxylic acid compound from the effluent stream. Particularly it is a process for the separation of methacrylic acid from the reactor effluent comprising methacrylic acid, propionic acid, formaldehyde, water and by-products. The success of this method of separation of metha¬ crylic acid from the reactor effluent stream is due pri¬ marily to the use of particular process conditions and process equipment, specifically a distillation tower with a side-draw means of separating a sidestream rich in for¬ maldehyde and propionic acid. This sidestream typically contains 60-95 (wt)% of the unreacted formaldehyde and 10-70 (wt)% of the unreacted propionic acid entering the distillation column. Typically this sidestream also con- tains a sufficient amount of water to prevent polymeri¬ zation of formaldehyde and/or methacrylic acid with attendant plugging of the side-draw means. Water content of the side-draw stream can be within the range of from about 0.5 (wt)% to about 50 (wt)% of the side-draw stream. Water content will depend upon ratio of reac- tants in reactor feed, reaction temperature, and other process conditions. The sidestream is suitable for direct recycle to the methacrylic acid synthesis reactor. The recycle of large percentages of unreacted formaldehyde and unreacted pro¬ pionic acid directly back to the synthesis reactor reduces need for separation and purification of formal¬ dehyde and propionic acid downstream and downsizes recovery equipment. Immediate recovery and immediate recycle of unreacted formaldehyde and unreacted propionic acid back to the synthesis reactor is an economic advantage. Reaction products of methacrylic acid and water are removed as bottoms and overhead respectively. Location of the side-draw on the effluent distilla¬ tion column can be within a wide range over the column's height, from a low which is about 10% of the column theoretical trays to a high of about 90% of the column theoretical trays, preferably 30-85% of the column theor¬ etical trays. Actual location of the side-draw can be determined by experiment, as location of the side-draw will be determined by reaction conditions, including com- position of the reactor feed and effluent as well as con¬ ditions of the distillation unit operation, such as optional use of an entrainer. A large number of catalysts, both water-tolerant and water-intolerant types, exhibit activity in the aldol- type condensation reaction of this invention. Specific catalyst materials that are useful in the process include synthetic alkali metal aluminosilicates, natural alkali metal aluminosilicates, synthetic alkaline earth metal aluminosilicates, natural alkaline earth metal aluminosilicates, alkali metal hydroxides on synthetic aluminosilicates, alkali metal hydroxides on natural alu¬ minosilicates, alkaline earth metal hydroxides on syn- thetic aluminosilicates, alkali metal hydroxides on silica gel, alkaline earth metal hydroxides on silica gel, sodium silicate on silica gel, potassium silicate on silica gel, molybdenum oxide on silica gel, silica gel, synthetic manganese aluminosilicate, natural manganese aluminosilicate, synthetic cobalt aluminosilicate, natural cobalt aluminosilicate, synthetic zinc aluminosi¬ licate, and natural zinc aluminosilicate. Catalyst compositions found to be especially useful in the reaction to form methacrylic acid from propionic acid and formaldehyde are the subject of applications numbered S.N. 624,040 and S.N. 624,041 filed on even date in the names of Hagen, et al., and Kakuk, et al., respec¬ tively, which are hereby incorporated by reference. The synthesis reactor feed stock can be composed of propionic acid, formaldehyde, and some water. The mole ratio of propionic acid to formaldehyde is preferably maintained within the range from about 25/1 to about 1/25; with a more preferred range of about 2/1 to 1/2. The feed stock or feed mixture can be obtained by adding the required amounts of propionic acid and formaldehyde to the recycle mixture of propionic acid and formal¬ dehyde, to maintain the desired proportions. The reaction takes place over a wide temperature range; temperatures in the range of about 280°C to about 500°C are satisfactory. Desirable and advantageous results are obtained by operating with temperatures in the range of about 280°C to about 350°C. The process is normally run at atmospheric pressure, although higher or lower pressures can be used. The space velocity of the vaporized feed mixture over the catalyst can be varied over wide limits. Space velocity figures in this specification are based on the total number of moles of materials entering the catalyst zone. Total moles are multiplied by the volume of a mole of an ideal gas at 0°C and one atmosphere (22.4 liters/mole), to obtain the total volume under standard conditions. A space velocity in the range from about 100 liters per hour of the feed per liter of reactor volume to about 1000 liters per hour of the feed per liter of reactor volume is preferred. Any of the various formaldehyde containing materials can be used with the catalyst of the process, such as formalin, methanolic formaldehyde solution, paraformal¬ dehyde, and trioxane. Preferably, the formaldehyde com¬ pound is from about 99 (wt)% to about 70 (wt)% formal- dehyde. The reactor effluent stream contains water of reac¬ tion, one male of water for each mole of methacrylic acid produced. Distillation with use of a side-draw separates unreacted propionic acid and unreacted formaldehyde with some percentage of water, from the reactor effluent. Methacrylic acid and remaining water are removed as bot¬ toms and overhead, respectively. Alternatively, to sepa¬ rate the water from the propionic acid and methacrylic acid, a substantially non-reactive compound capable of acting as a water-entrainer and of breaking or preventing the formation of a water azeotrope of propionic acid can be introduced into the reactor effluent to break the water-propionic acid azeotrope upon distillation. The non-reactive compound alternatively can also be intro- duced into the reactor. Because the product stream contains amounts of unreacted propionic acid and unreacted formaldehyde, as well as water, selection of a suitable hydrocarbon in a preferred method of operation wherein reactor effluent is distilled to separate the components is determined by the boiling points of azeotropes of propionic acid and metha¬ crylic acid. Both propionic acid and methacrylic acid form water azeotropes which boil at approximately 99°C. Separation by distillation of the C g to C.- hydrocarbon in the presence of water requires that the water:hydrocarbon azeotrope which forms have a boiling point below the boiling points of the propionic acid and f I methacrylic acid:water azeotropes. Preferably, the boiling point of the water:hydrocarbon azeotrope be no more than 95°C. Boiling points of typical hydrocarbon: ater azeo- tropes are: Hydrocarbon % Water B . P . °C n-Hexane 5 — n-Heptane 13 79 n-Octane 23 90 n-Nonane 40 95 Branched C β to C,- saturated aliphatic hydrocarbons, aromatic hydrocarbons of 6 to 12 carbon atoms, cycloal- kanes of 6 to 12 carbon atoms and mixtures thereof which form water:hydrocarbon azeotropes with boiling points of no more than 95°C can be also used. We have found that introduction of a suitable hydro¬ carbon non-reactive compound into the reactor can result in an increase in yield, based on propionic acid, of about 3% without any loss of reactants due to formation of additional by-products. Suitable hydrocarbon compounds found to be useful in increasing the yield of methacrylic acid from propionic acid and formaldehyde are the subject of S.N. 624,050 filed an even date in the names of Hagen, et al, which is hereby incorporated by reference. The hydrocarbon compound can be any hydrocarbon capable of azeotroping with water and not forming a mul- ticomponent azeotrope with acid, as one of the compo¬ nents. Suitable entrainers include aliphatic saturated hydrocarbons of 6 to 12 carbon atoms such as hexane, hep¬ tane and octane, including isomers, as well as benzene, o-, m-, or £- xylenes, toluene and mixtures thereof. n-Heptane is preferred. An essential process element of the process of the instant invention is distillation of the reactor effluent stream under process conditions utilizing a side-draw whereby, typically, 60-90(wt)% of the unreacted formaldehyde and 10-70(wt)% of unreacted propionic acid entering the distillation column are removed for recycle to the synthesis reactor. If an entrainer is used, the distillation column overhead consists of water, the entrainer, a small amount of formaldehyde and a trace of propionic acid. The distillation column bottoms contain methacrylic acid, propionic acid and the heavy by-prod- ucts of the methacrylic acid synthesis reaction. These bottoms are further processed to recover the methacrylic acid and the propionic acid. The overhead is sent to a formaldehyde recovery and dehydration section to remove the water. There, aqueous formaldehyde is reacted with an alcohol selected from the group consisting of 2-ethylhexanol, cyclohexanol and other commercially available heavy alcohols. A hemiacetal is formed with an alcohol, such as 2-ethyl-l-hexanol (2-EH) to form 2-ethylhexyl hemiformal, which is then dried. The dry hemiformal is subsequently thermally cracked, liberating dry formaldehyde for the reaction section. The waste water is sent to waste treatment. In a specific embodiment, the synthesis reaction section in the instant process produces methacrylic acid and water via the base-catalyzed aldol-type condensation of propionic acid and formaldehyde. Typically, conver¬ sions of propionic acid in the reactor range from 15 to 40%. Catalyst performance, irrespective of whether the catalyst is relatively water-tolerant or relatively water-intolerant, can be adversely affected over a long time period by the presence of significant quantities of water in the reactor feed. It has been learned that long-term water concentrations of greater than 2-4 (wt)% in the reactor feed can have a deleterious effect on long-time catalyst performance. High selectivities have been obtained from propionic acid and formaldehyde with typical catalysts, 80-95% and 75-90%, respectively. Major liquid reaction by-products have been identified as ethyl isopropenyl ketone, 3-pentanone, 2,5-dimethyl- cyclopen-ten-1-one, 2,2,4-trimethylbutyrolactone, and isobutyric acid. Carbon dioxide is also a by-product. Reactor effluent is necessarily processed to recover unreacted propionic acid, unreacted formaldehyde and methacrylic acid. In a preferred embodiment, introduction of an entrainer into the reactor or into the reactor effluent in the effluent distillation tower serves to break the binary azeotropes which form. n-Heptane, as an example of an entrainer, is introduced into the reactor or into the reactor effluent to break the propionic acid-water azeotrope (BP 210°F) with a lower boiling rv-heptane-water azeotrope (BP 174.6°F). With no n-heptane present, pro¬ pionic acid would be carried overhead from the effluent distillation column in substantial amounts. The pro¬ pionic acid-water azeotrope is 17.8 (wt)% propionic acid. In a typical example of the method of operation, the effluent distillation tower consisted of a 40-tray two- inch vacuum jacket Oldershaw column equipped with a forced convection reboiler and a downflow condenser. Thermowells and sample taps were provided on every fifth tray of which several sample taps functioned as feed or product removal taps. Surprisingly, it was found that at temperatures of from approximately 160°F to 315°F (at one atmosphere) over the length of the distillation column, high concen¬ trations of unreacted propionic acid and unreacted for- maldehyde occurred within the column at certain tray levels, permitting removal of the unreacted propionic acid and unreacted formaldehyde from the distillation column. The sidestream so removed from the distillation column typically can contain as much as 60-95 (wt)% of the unreacted formaldehyde and 10-70 (wt)% of the unreacted propionic acid contained in the synthesis reactor effluent. The sidestream typically can contain from about 0.5 (wt)% to about 10 (wt)% water and as much as 2-4 (wt)% methacrylic acid. The resultant concentration ratio of water to for¬ maldehyde in the sidestream is dependent upon synthesis reactor operating conditions, in particular, the propionic acid/formaldehyde mole feed ratio to the reactor, the formaldehyde conversion, the resulting water make in the reactor and the water concentration in the reactor feed. Surprisingly, it has been found that if an entrainer is used, control of the water content of the sidestream can be obtained by control of the ratio of entrainer to water in the feed to the column. Since a completely anhydrous sidestream containing formaldehyde results in solids formation in the sidedraw, the sidestream water content is preferably at least 0.5 (wt)%. The formaldehyde species withdrawn in the side¬ stream are polyoxymethylene glycols whose average mole¬ cular weights increase with increasing formaldehyde/water mole ratios. The formation of solids (paraformaldehyde) in the sidedraw is aggravated by use of high vacuum which reduces operating temperatures. Accordingly, limits of temperature and pressure in the effluent distillation column are dependent upon the formaldehyde/water mole ratios in the column and side-draw temperature, typi- cally, formation of solids occurring in the side-draw at about 175°F and a formaldehyde:water mole ratio of 15:1 or more. In a specific embodiment, concentration of unreacted formaldehyde and unreacted propionic acid within the effluent distillation column is dependent upon tempera¬ ture, pressure and sidedraw formaldehyde/water weight ratios. Polymerization of methacrylic acid in the effluent distillation column is conveniently prevented by addition of a suitable inhibitor which can be selected from the group consisting of p_-benzoquinone, t-butylcate- chol, and phenothiazine, as well as other well-known inhibitors (including oxygen) for the prevention of methacrylic acid polymerization. The following table gives typical operating conditions of the effluent distillation column: Number of Trays 40 Column Temperatures Overhead °F 160°-175° Sidedraw °F 210°-250° Bottoms °F 285°-315° Column Pressure, At . 1 Sidedraw Formaldehyde/ Water (Weight % Ratios) 20.3/2.09 to 41.2/3.5 Water content in the feed to the effluent distilla¬ tion column is composed of water produced in the reactor and water content of the reactor feed. The following table gives suitable operating conditions of the metha- crylic acid synthesis reactor. Water Concentration In Feed (wt)% l%-2% Propionic Acid/Formaldehyde Mole Ratio 3:2 to 1:1 Methacrylic Acid Yield (Based on Propionic Acid) 28-33 (wt)% Water Concentration In Reactor Effluent (wt)% 4%-8% In summary, the instant invention relates to a pro¬ cess for distilling the reaction product stream from a reactor of propionic acid, and a formaldehyde compound, the reaction product stream comprising propionic acid, formaldehyde, methacrylic acid and by-products which com¬ prises fractionally distilling said reaction product stream whereby a sidestream is removed from the central I 6 part comprising from 10% to 90% of the theoretical trays of said distillation column. The location of the side¬ draw is such that at least 10 (wt)% of the unreacted for¬ maldehyde and at least 10 (wt)% of the unreacted pro- pionic acid is removed from the column in the sidestream. The sidestream comprises not more than a total of 50 (wt)% water plus methacrylic acid. The invention also comprises a method of distilling the reaction product stream of a saturated aliphatic monocarboxylic acid compound and a formaldehyde compound, said reaction product stream comprising said saturated aliphatic monocarboxylic acid compound, an alpha, beta- ethylenically unsaturated aliphatic monocarboxylic acid compound of one more acid compound, water, said formaldehyde compound and byproducts which comprises fractionally distilling said reaction product together with a substantially non-reactive compound capable of acting as a water-entrainer and of breaking or preventing the formation of a water azeotrope of said saturated ali- phatic monocarboxylic acid compound under conditions whereby (1) a major proportion of ethylenically unsatu¬ rated monocarboxylic acid compound is in the bottom of the distillation column, (2) a major portion of the water, a portion of the formaldehyde compound and a major portion of the compound capable of breaking or preventing the formation of said azeotrope are removed overhead and (3) a sidestream is removed below the top of the distil¬ lation column comprising water, a major portion of said formaldehyde compound and a substantial portion of said saturated aliphatic monocarboxylic acid. The sidestream • can be recycled back to the reactor. Specifically, the invention comprises a method of treating the reaction products of propionic acid and for¬ maldehyde which comprise methacrylic acid and water wherein the reaction products are fractionally distilled and unreacted propionic acid and unreacted formaldehyde are removed in a side-draw stream from the distillation column. Alternatively, the reaction products are distilled with an entrainer wherein the greater portion of water present is removed overhead, the substantial portion of unreacted propionic acid and major portion of unreacted formaldehyde are removed in a sidedraw stream and methacrylic acid and propionic acid are removed as bottoms. Embodiments of the process of the present invention can be found in the following examples. These embodi- ents and examples are presented for purposes of illus¬ tration only and are not intended to limit the scope of the invention. EXAMPLE I Into a 2 inch vacuum jacketed Oldershaw distillation column containing 30 trays and 22 inches of 0.16 inch Pro Pack 316 stainless steel packing at the top, equivalent to about 10 to 20 theoretical trays, 1212.9 g/hr was fed at Tray No. 8 of simulated methacrylic acid (MA) reactor effluent having the following composition of formaldehyde (FA), water (H-O), propionic acid (PA) and n-heptane (C ? ), FA H_0_ PA MA = (wt)%'s 9.11 3.69 40.37 16.05 30.51 Also incorporated into the feed to prevent MA poly¬ merization in the tower bottoms was 1000 ppm p_-benzoqui- none and 500 ppm phenothiazine. In addition 4500-5000 ppm oxygen (as 50 vol.% with nitrogen) was sparged into the reboiler of the column. All levels are based on MA in the feed. As a control, actual pilot-plant reactor effluent containing small amounts of the by-products was fed to the reactor effluent column under nearly identical condi- tion. Additional inhibitor was required to keep the system MA polymer free. The pilot plant reactor effluent had the composition of by-products described below; ( t)% 3-Pentanone 0.034 Isobutyric Acid 0.05 2,5-Dimethylcyclopenten-l-one 0.013 2,2,4-Trimethylbutyrolactone 0.003 An inhibitor package of 1100 ppm p_-benzoquinone, 1100 ppm t-butylcatechol and 550 ppm phenothiazine together with an oxygen addition rate of 10,000 ppm oxygen (all based on MA fed to the column) allowed operation with no visible evidence of MA polymers. The column was operated at atmospheric pressure with the temperature at various locations in the column as follows: Column Feed Sidedraw Column Bottoms Tray No. 8 Tray No. 18 Overhead 296°F 264°F 220°F 169°F The compositions and takeoff rates for the column bottoms, sidedraw (Tray No. 18) and overhead are given below. Rate < Zomposition Analysis Location (<3/HR) (wt)% Overhead Aqueous 59.9 25.69 72.60 1.71 - ~0 Organic 373.8 - - - - -100 Sidedraw 238.3 41.22 3.50 52.12 2.36 0.8 Bottoms 553.6 <0.01 0.07 65.23 34.69 ~0 1225.6g (101.0% Theory) The (wt)% of FA (unreacted FA) and PA (unreacted PA) in the sidedraw stream correspond to 88.9% of the FA fed to the column and 25.4% the PA fed to the column. EXAMPLE II When the column and condition as described in Example I were used to distill a feed as described in Example I without removing a sidedraw stream the forma- tion of solid paraformaldehyde in the column between Tray No. 20-30 caused column plugging and the resultant failure of the system to operate. EXAMPLE III In the procedure of Example I, the same composition of formaldehyde and propionic acid was fed to the distillation column. Excess water, in the amount to make the H-O/FA ratio in the column 3/1 or greater, was added. The dilution of the formaldehyde was below the level at which solids formation occurred. However, it was deter- mined that separation of the water component in the tower overhead would entail a heavy energy penalty. EXAMPLE IV In the procedure of Example I, the same composition of formaldehyde, propionic acid and water was fed to the distillation column. Excess heptane, in the amount to azeotrope all the water in the feed, was added above the feed point of the column so that only heptane was used as the reflux to the column. All the water and excess for¬ maldehyde was removed overhead. The overhead with the high formaldehyde content condensed as paraformaldehyde in the condenser, plugging the condenser tubes. In addi¬ tion propionic acid loss in this overhead stream was excessive.

Claims: WHAT IS CLAIMED IS: Claim 1. A process of distilling the reaction product stream from a reactor of a saturated monocarbox¬ ylic acid compound and a formaldehyde compound, said reaction product stream comprising said saturated ali¬ phatic monocarboxylic acid compound, an alpha, beta-ethy¬ lenically unsaturated aliphatic monocarboxylic acid compound of one more carbon atom than the starting saturated aliphatic monocarboxylic acid compound, water, said formaldehyde compound and by-products which-com¬ prises fractionally distilling said reaction product stream whereby a sidestream is removed from the central part comprising from 10% to 90% of the theoretical trays of the distillation column. Claim 2. The process of Claim 1 wherein said side¬ stream is removed at a location wherein said sidestream comprises at least 10 (wt)% of the unreacted formaldehyde and at least 10 (wt)% of the unreacted propionic acid in said column, and total (wt)% water plus said alpha-, beta- ethylenically unsaturated alipahtic monocarboxylic acid compound in said sidestream is not more than 50 (wt)%. Claim 3. The process of Claim 1 wherein said satu¬ rated aliphatic monocarboxylic acid compound is propionic acid and said alpha-,beta-ethylenically unsaturated ali¬ phatic monocarboxylic acid compound is methacrylic acid. Claim 4. The process of Claim 1 where ' in said for¬ maldehyde compound is selected from the group consisting of formalin, methanolic formaldehyde solution, parafor- maldehyde and trioxane. Claim 5. The process of Claim 1 wherein said for¬ maldehyde compound is from about 99 (wt)% to about 70 (wt)% formaldehyde. Claim 6. The process of Claim 1 wherein said reac- tion product is distilled in said column at conditions of: Column Temperatures o Overhead °F 160-175 Sidedraw °F 210°-250° Bottoms °F 285°-315° Column Pressure, Atm. 1 Claim 7. The process of Claim 1 wherein said side¬ stream comprises up to 95 (wt)% of unreacted formaldehyde compound and up to 70 (wt)% of unreacted saturated mono- carboxylic acid compound in said reaction product stream. Claim 8. The process of Claim 1 which comprises fractionally distilling said reaction product stream together with a substantially non-reactive compound capable of acting as a water-entrainer and of breaking or preventing the formation of a water azeotrope of said saturated aliphatic monocarboxylic acid compound under conditions whereby (1) a major proportion of said ethy- lenically unsaturated monocarboxylic acid compound is in the bottom of said distillation column, (2) a major por- tion of the water, a portion of said formaldehyde com¬ pound and a major portion of said compound capable of breaking or preventing the formation of said azeotrope are removed overhead and (3) said sidestream is removed from said central part of said distillation column. Claim 9. The process of Claim 8 wherein said non- reaction compound is a hydrocarbon of from 6 to 12 carbon atoms. Claim 10. The process of Claim 8 wherein said non- reactive compound is selected from the group consisting of n-hexane, n-heptane, n-octane and their isomers, ben¬ zene, o-, m-, or j-xylene, toluene and mixtures thereof. Claim 11. The process of Claim 8 wherein said non- reactive compound is n-heptane. Claim 12. The process of Claim 8 wherein said non- reactive compound is introduced into the reactor producing said reaction product. Claim 13. The process of Claim 8 wherein said non- reactive compound forms a water-azeotrope. Claim 14. The process of Claim 1 wherein said side¬ stream is recycled to said reactor.

Inventors: BALEIKO MARC O, RADER EDWARD F, BALEIKO, MARC, O., RADER, EDWARD, F.
Applicants: AMOCO CORP, AMOCO CORPORATION
Application year: 1985
Main classification: B01D3
IPC codes: B01D3, C07C45, C07C51, C07C57