PROCESS FOR THE PREPARATION OF alpha -METHYLENE LACTONES

Abstract: This invention concerns a process for the addition of formaldehyde to the alpha carbon atom of lactones for the production of alpha -methylenelactones, and specifically alpha -methylene- gamma -butyrolactone.

Description: TITLE PROCESS FOR THE PREPARATION OF α-METHYLENE LACTONES This application claims the benefit of U.S. Provisional Application No. 60/126,883 filed March 30, 1999 and U.S. Provisional Application No. 60/126,884, filed March 30, 1999. FIELD OF THE INVENTION This invention concerns a process for the addition of formaldehyde to the α carbon atom of lactones to produce α-methylenelactones, and specifically α-methylene-γ-butyrolactone. TECHNICAL BACKGROUND α-Methylene-γ-butyrolactone is useful as a monomer in the preparation of both homopolymers and copolymers. An early synthesis of α-methylene-γ-butyrolactone involved two steps (Watts et al., J. Chem. Soc. Chem. Comm. 27 (1970)). The first is carboxylation of γ-butyrolactone with methyl methoxymagnesium carbonate (Stiles' reagent) to produce the acid. Next, the acid is briefly treated with a mixture of aqueous formaldehyde and diethylamine, followed by a separate treatment of the crude product with sodium acetate in acetic acid. The first step requires 6-7 hours and affords almost quantitative yields, whereas the second step can be accomplished in less than 30 minutes but with yields of only 50%. A. W. Murray et al. Synthesis, January 1985, p 35-38 report the development of a two-step route to α-methylene-γ-butyrolactone that consists of the reaction of γ-butyrolactone with ethyl formate in the presence of sodium hydride base followed by the isolation of the resulting formyl derivative as its sodium salt and subsequent reaction with an aldehyde. B. S. Orlek et al., U.S. Patent No. 5,166,357, use this same route specifying the use of formaldehyde as the aldehyde. Although the above methods for the production of α-methylene lactones are useful, they are time consuming and are multipart processes. The instant invention represents an advance in the art as it is a single step process that produces the desired product in high yields and good selectivity. SUMMARY OF THE INVENTION The invention provides a process for preparing α-methylenelactones of Formula II comprising heating lactones of Formula I and formaldehyde in the vapor phase at a temperature of above 200°C in the presence of a basic catalyst: Formula I wherein, «=1-11 ; R 1 , R 2 , R 3 , and R 4 taken independently are hydrogen, hydrocarbyl or substituted hydrocarbyl, C j -Ci g unsubstituted or substituted alkyl, unsubstituted or substituted alkenyl, unsubstituted or substituted cycloalkyl, unsubstituted or substituted cycloalkyl containing at least one heteroatom, unsubstituted or substituted aromatic ring, and unsubstituted or substituted aromatic ring containing at least one heteroatom. In a specific embodiment the lactone of Formula I is γ-butyrolactone and the α-methylenelactone of Formula II is α-methylene-γ-butyrolactone. Catalysts suitable in the present invention may be selected from the group consisting of metal oxides, metal hydroxides, and metal carbonates and may be supported or unsupported and may make use of catalyst promoters. Additionally the invention provides a process for preparing α-methylenelactones of Formula II comprising: (a) heating lactones of Formula I and formaldehyde in the vapor phase at a temperature of above 200°C in the presence of a basic catalyst for a time sufficient for the α-methylenelactones of Formula II to be formed; wherein, «=1-11; R 1 , R 2 , R 3 , and R 4 taken independently are hydrogen, hydrocarbyl or substituted hydrocarbyl, Ci-Ci g unsubstituted or substituted alkyl, unsubstituted or substituted alkenyl, unsubstituted or substituted cycloalkyl, unsubstituted or substituted cycloalkyl containing at least one heteroatom, unsubstituted or substituted aromatic ring, and unsubstituted or substituted aromatic ring containing at least one heteroatom; (b) separating the lactones of Formula I from the basic catalyst; (c) contacting the basic catalyst with oxygen for a time sufficient to permit catalyst regeneration; and (d) repeating steps (a) through (c). Additionally the invention provides process for preparing α- methylenelactones of Formula II comprising: (a) heating lactones of Formula I and formaldehyde in the vapor phase at a temperature of above 200°C in the presence of a basic catalyst for a time sufficient for the α-methylenelactones of Formula II to be formed in a reactor effluent; Formula II wherein, n=l-l l ; R 1 , R 2 , R 3 and R 4 taken independently are hydrogen, hydrocarbyl or substituted hydrocarbyl, Cj-Cjg unsubstituted or substituted alkyl, unsubstituted or substituted alkenyl, unsubstituted or substituted cycloalkyl, unsubstituted or substituted cycloalkyl containing at least one heteroatom, unsubstituted or substituted aromatic ring, and unsubstituted or substituted aromatic ring containing at least one heteroatom, (b) collecting the reactor effluent of step (a); and (c) contacting the collected effluent with the base catalyst at a temperature of above 200°C. DETAILED DESCRIPTION OF THE INVENTION The process of the present invention concerns an efficient methenylation of lactones to yield α-methylenelactones of which α-methylene-γ-butyrolactone is a preferred member. The reaction proceeds according to the general scheme: Formula II wherein, w=l-l l ; R 1 , R 2 , R 3 , and R 4 taken independently are hydrogen, hydrocarbyl or substituted hydrocarbyl, Ci-Ci g unsubstituted or substituted alkyl, unsubstituted or substituted alkenyl, unsubstituted or substituted cycloalkyl, unsubstituted or substituted cycloalkyl containing at least one heteroatom, unsubstituted or substituted aromatic ring, and unsubstituted or substituted aromatic ring containing at least one heteroatom. In a specific embodiment the lactone of Formula I is γ-butyrolactone and the α-methylenelactone of Formula II is α-methylene-γ-butyrolactone. R 1 , R 2 ,R 3 , and R 4 may join to form members of a ring structure selected from the group consisting of, unsubstituted or substituted cycloalkyl, unsubstituted or substituted cycloalkyl containing at least one heteroatom in the ring, unsubstituted or substituted aromatic ring, and unsubstituted or substituted aromatic ring containing at least one heteroatom in the ring. Most preferred compounds are where the lactone of Formula I is γ-butyrolactone and the α-methylenelactone of Formula II is α-methylene-γ- butyrolactone. In the context of this disclosure, a number of terms and abbreviations shall be utilized. The following definitions are provided. When a group contains a substituent which can be hydrogen, for example R 1 , R 2 , R 3 , and R 4 , then, when this substituent is taken as hydrogen, it is recognized that this is equivalent to said group being unsubstituted. The term "alkyl" includes straight-chain or branched alkyl, such as, methyl, ethyl, n-propyl, z ' -propyl, or the different butyl, pentyl and hexyl isomers. Also included are all isomers up to and including octadecane. A "hydrocarbyl group" is a univalent group containing only carbon and hydrogen. If not otherwise stated, it is preferred that hydrocarbyl groups herein contain 1 to about 30 carbon atoms. By "substituted hydrocarbyl" herein is meant a hydrocarbyl group which contains one or more substituent groups which are inert under the process conditions to which the compound containing these groups is subjected. The substituent groups also do not substantially interfere with the process. If not otherwise stated, it is preferred that substituted hydrocarbyl groups herein contain 1 to about 30 carbon atoms. Included in the meaning of "substituted" are heteroaromatic rings. One of skill in the art will know where and how to obtain the α-methylene lactones reactant of the present invention. For example γ-butyrolactone is readily available from commercial sources such as Aldrich Chemical Company (Millwaukee, WI). The process of the present invention is carried out in the vapor state, at temperatures greater than 200°C, over highly basic catalysts. Although any temperature above 200°C is useful, temperature in the range of about 250°C to about 400°C are preferred where ranges of about 300°C to about 340°C are most preferred. In one preferred embodiment the lactone and formaldehyde of the present invention are in the vapor phase. The basic catalysts are selected from the metal oxides, hydroxides, and carbonates. The oxides, hydroxides and carbonates employed herein may be used as powders, granules, or other particulate forms, or may be supported on an essentially inert support as is common in the art of catalysis. Representative catalysts include but are not limited to of magnesium oxide, barium oxide, barium hydroxide, lanthanum oxide potassium hydroxide, cadmium oxide, rubidium oxide, lithium hydroxide, strontium hydroxide, sodium hydroxide, calcium hydroxide, barium carbonate and mixtures thereof. Preferred catalysts are barium hydroxide and lanthanum oxide, where barium hydroxide is most preferred. In some cases reaction conditions may result in decreased catalytic efficiency. In these situations it may be useful to modify the reaction process to allow for catalyst regeneration. For example, contacting the present catalysts with 0 2 at elevated temperatures has the effect of reactivating the catalyst. Contact temperatures with O2 may range from about 300°C to about 500°C where temperatures of about 400°C to about 425°C are preferred. The metal oxide, hydroxide and carbonate catalysts of the present invention may further comprise catalyst additives and promoters which will enhance the efficiency of the catalyst. Use of theses materials are common and well known in the art (see for example, Kirk-Othmer Encyclopedia of Chemical Technology, Howe-Grant Ed., Vol. 5, pp 326-346, (1993), John Wiley & Sons, New York and Ullmann's Encyclopedia of Industrial Chemistry, Vol. A5, Gerhartz et al., Eds., pp. 337-346, (1986), VCH Publishers, New York, both hereby incorporated by reference.) Particularly useful in the present invention is gold used as a promoter with BA(OH) 2 . Basic catalysts of the present invention may be supported or unsupported. Where a support is desired suitable supports include but are not limited to silica, titania, zirconia, alumina, carbon, various zeolites and mixtures thereof. Particularly suitable catalyst - support combinations include barium hydroxide and lanthanum oxide supported on Siθ2- Preferred catalysts of the present invention have been effective in producing product at good selectivities. Selectivities of greater than 50% are typical where selectivities of greater than 95% are common. It will be appreciated that the selectivities and yields of product may be enhanced by additional contact with the catalyst. For example, yields and selectivities may be increase where the reactor effluent containing a mixture of reactant and product may be passed one or more times over the catalyst under the reaction conditions to enhance the conversion of reactant to product. One component of the invention is formaldehyde. Formaldehyde may be supplied in a variety of forms including as a solution or in the form of a formaldehyde polymer. Polymers of formaldehyde are more generally denominated polyacetals and include or are characterized by a linear polymer chain containing recurring -(CH2O)- units or ggroups. A convenient form of formaldehyde was formalin, (37% aqueous formaldehyde). The desired products, including α-methylene-γ-butyrolactone, are recovered using techniques common to the art. For example, when allowed to cool the α-methylene-γ-butyrolactone reaction mixture forms a viscous, clear mass. Alternatively, when heated under vacuum, the α-methylene-γ- butyrolactone/γ-butyrolactone mixture can be distilled directly from the reaction mixture. Additionally, the reaction mixture can be dissolved in water, adjusted to pH ■= 4 with 6N HC1, then distilled. Similarly, the separation of α-methylene-γ- butyrolactone from γ-butyrolactone can be accomplished using vacuum distillation with a spinning band column. Another method to recover the desired product is to polymerize α-methylene-γ-butyrolactone in the γ-butyrolactone solution using standard free-radical polymerization, isolate the polymer by precipitation from methanol, then thermally depolymerize back to α-methylene-γ-butyrolactone by heating under vacuum. Finally, α-methylene-γ-butyrolactone may also be separated from -γ-butyrolactone by melt crystallization. Table 1 summarizes the results of Examples 1-29. Of the catalysts tested Ca(OH) 2 /SiO 2 , NaOH/SiO 2 , LiOH/SiO 2 , Sr(OH) 2 /SiO 2 , KOH/SiO 2 and Ba(OH) 2 /SiO 2 gave yields exceeding 5%. The best overall catalyst was 8 wt % Ba(OH) 2 /SiO 2 which gave an 11% yield of α-methylene-γ-butyrolactone at 37% conversion of the γ-butyrolactone (37% product selectivity) at 340 °C. No significant amounts of other volatile compounds were noted. As seen from Table 1, the base oxides or hydroxides of Mg, Ca, Sr and Ba (Group IIA) are active catalysts. Similarly, the base oxides or hydroxides of Na, K and Rb(in combination with Mg) (Group IA) are active catalysts. These Groups include the most basic metal oxides known. Most of these materials were tested as deposited on an oxide support. The support material need not have a special character except that it should be stable to the reaction conditions. Metal oxides of Groups IVB and higher, up to Group rVA, are preferable. Rare earth oxides are also acceptable. It is believed that a support is preferred in order to maintain high catalyst surface areas. Table 2 shows examples (30-34) wherein feed ratios are varied. The most significant improvement in the % selectivities to α-methylene-γ-butyrolactone came from variations in the reactant feed ratio. When the feed ratio was increased from 1 :1 to 1 :8 (lactone:formaldehyde) the average % yield increased as the ratio of formaldehyde increased. Table 3 shows results with the varied catalysts and conditions. Example 37 identifies LiOH/Silicon as an especially useful catalysts/support combination. Table 4 shows the formation of α-methylene-γ-butyrolactone and γ-mefhylene-γ- butyrolactone using preferred catalyst (LaO/SiO ) under varied conditions. Example 46 (Table 5) shows the ability to regenerate the catalyst Ba(OH) 2 /SiO 2 with air. Example 47 (Table 6) illustrates that there is enhanced conversion of γ-butyrolactone to α-methylene butyrolactone if the reactor effluent is recycled across the catalyst a second time, indicating that a recycled procedure improves product yield. EXAMPLES The present invention is further defined in the following Examples, in which all parts and percentages are by weight and degrees are Celsius, unless otherwise stated. It should be understood that these Examples, while indicating preferred embodiments of the invention, are given by way of illustration only. From the above discussion and these Examples, one skilled in the art can ascertain the essential characteristics of this invention, and without departing from the spirit and scope thereof, can make various changes and modifications of the invention to adapt it to various usage and conditions. Common reagents were purchased from Sigma- Aldrich and solvents from VWR Scientific. The meaning of abbreviations is as follows: "μL" means microliter, "mL" means milliliter(s), "L" means liter(s), "mM" means millimolar, "M" means molar, "mmol" means millimole(s) and "ng" means nanogram(s). REACTION OF γ-BUTYROLACTONE WITH FORMALDEHYDE Solutions containing γ-butyrolactone in formalin (37% aqueous formaldehyde) at various feed ratios, was fed to a vaporizer (held at 200°C) followed by the introduction of a gas (N 2 ) to carry the vapor through a !Λ inch tubular reactor containing a catalyst heated to the appropriate reaction temperature. A series of basic materials (1-2 g samples) was examined for catalytic activity by exposing these materials to the test conditions for about 0.25 to about 6 hr periods. In all cases, ca. 25% to 75% extents of conversion of the γ-butyrolactone were found, depending upon the catalyst employed. The Tables 1-6 contains the examples and show catalyst, nature and amount, feed ratio of γ-butyrolactone to formalin, temperature, flow rate, observed conversion and yield or selectivity. Below are listed the preparations of the catalysts listed in the table. KOH/SiO 2 5 g of granular, sol-gel derived silica (+8 mesh; 300 m g-**) was slurried into a solution of 1 g KOH in 10 mL distilled water. The slurry was stirred for 10 minutes and then evaporated to dryness. The recovered solid was dried in a gold boat under flowing (100 mL/min) nitrogen at 550°C for 2 hours and then collected under nitrogen as a granular white solid. Ba(OH) 2 /SiO 2 5 g of granular, sol-gel derived silica (+8 mesh; 300 m 2 g _1 ) was slurried into a solution of 1 g Ba(OH) 2 octahydrate in 10 mL distilled water. The slurry was stirred for 10 minutes and then evaporated to dryness. The recovered solid was dried in a gold boat under flowing (100 mL/min) nitrogen at 550°C for 2 hours and then collected under nitrogen as a granular white solid. CdO/SiO 2 5 g of granular, sol-gel derived silica (+8 mesh; 300 m 2 g" 1 ) was slurried into a solution of 1 g Cd(NU3) 2 tetrahydrate in 10 mL distilled water. The slurry was stirred for 10 minutes and then evaporated to dryness. The recovered solid was dried in a gold boat under flowing (100 mL/min) nitrogen at 550 °C for 2 hours and then collected under nitrogen as a granular brown solid. 8% Ba(OH) 2 /SiO 2 50 g of granular, sol-gel derived silica (+8 mesh; 300 m 2 g' 1 ) was slurried into a solution of 10 g Ba(OH) 2 octahydrate in 100 mL distilled water. The slurry was stirred for 10 minutes and then evaporated to dryness. The recovered solid was dried in a gold boat under flowing (100 mL/min) nitrogen at 550 °C for 2 hours and then collected under nitrogen as a granular white solid. l% Ba(OH) 2 /SiO 2 10 g of granular, sol-gel derived silica (+8 mesh; 300 m 2 g' 1 ) was slurried into a solution of 0.2 g Ba(OH) 2 octahydrate in 20 mL distilled water. The slurry was stirred for 10 minutes and then evaporated to dryness. The recovered solid was dried in a gold boat under flowing (100 mL/min) nitrogen at 550 °C for 2 hours and then collected under nitrogen as a granular white solid. 10% Ba(OH) 2 /γ-Al 2 O 3 10 g of γ-alumina powder (150 m g- 1 ) was slurried into a solution of 2 g Ba(OH) 2 octahydrate in 20 mL distilled water. The slurry was stirred for 10 minutes and then evaporated to dryness. The recovered solid was dried in a gold boat under flowing (100 mL/min) nitrogen at 550 °C for 2 hours and then collected under nitrogen as a granular white solid. Ba(OH) 2 /TiO 2 10 g of titania (anatase) powder (-30 m g _1 ) was slurried into a solution of 2 g Ba(OH) 2 octahydrate in 20 mL distilled water. The slurry was stirred for 10 minutes and then evaporated to dryness. The recovered solid was dried in a gold boat under flowing (100 mL/min) nitrogen at 550 °C for 2 hours and then collected under nitrogen as a granular white solid. 10% Ba(OH) 2 /MgO 10 g of magnesia powder (-10 m 2 g" 1 ) was slurried into a solution of 2 g Ba(OH) 2 octahydrate in 20 mL distilled water. The slurry was stirred for 10 minutes and then evaporated to dryness. The recovered solid was dried in a gold boat under flowing (100 mL/min) nitrogen at 550 °C for 2 hours and then collected under nitrogen as a granular white solid. 10% Ba(OH) 2 /ZrO 2 10 g of zirconia powder (-25 m 2 g _1 ) was slurried into a solution of 2 g Ba(OH) 2 octahydrate in 20 mL distilled water. The slurry was stirred for 10 minutes and then evaporated to dryness. The recovered solid was dried in a gold boat under flowing (100 mL/min) nitrogen at 550°C for 2 hours and then collected under nitrogen as a granular white solid. 10% Ba(OH) 2 /SiO 2 /Al 2 O 3 10 g of silica-alumina powder (-150 m g _1 ) was slurried into a solution of 2 g Ba(OH) octahydrate in 20mL distilled water. The slurry was stirred for 10 minutes and then evaporated to dryness. The recovered solid was dried in a gold boat under flowing (100 mL/min) nitrogen at 550°C for 2 hours and then collected under nitrogen as a granular white solid. Ca(OH) 2 /SiO 2 10 g of silica granules (-300 m 2 g _1 ) was slurried into a solution of 0.25 g Ca(OH) 2 in 100 mL distilled water. The slurry was stirred for 10 minutes and then evaporated to dryness. The recovered solid was dried in a gold boat under flowing (100 mL/min) nitrogen at 550°C for 2 hours and then collected under nitrogen as a granular white solid. ICP revealed 1.15 wt % Ca in this sample. Sr(OH) 2 /SiO 2 10 g of silica granules (-300 m g _1 ) was slurried into a solution of 0.25 g Sr(OH) 2 octahydrate in 100 mL distilled water. The slurry was stirred for 10 minutes and then evaporated to dryness. The recovered solid was dried in a gold boat under flowing (100 mL/min) nitrogen at 550°C for 2 hours and then collected under nitrogen as a granular white solid. ICP revealed 0.60 wt % Sr in this sample. NaOH/SiO 2 10 g of silica granules (-300 m 2 g _1 ) was slurried into a solution of 0.25 g NaOH in 20 mL distilled water. The slurry was stirred for 10 minutes and then evaporated to dryness. The recovered solid was dried in a gold boat under flowing (100 mL/min) nitrogen at 550°C for 2 hours and then collected under nitrogen as a granular white solid. ICP revealed 1.45 wt % Na in this sample. LiOH/SiO 2 10 g of silica granules (-300 m g" 1 ) was slurried into a solution of 0.25 g LiOH in 20 mL distilled water. The slurry was stirred for 10 minutes and then evaporated to dryness. The recovered solid was dried in a gold boat under flowing (100 mL/min) nitrogen at 550°C for 2 hours and then collected under nitrogen as a granular white solid. ICP revealed 0.42 wt % Li in this sample. 10% Ba(OH) 2 /SiO 2 In a 100 ml round bottom flask, 25 ml of a solution of 1.86 wt % Ba (as the hydroxide) in H 2 O were combined with 5.0 grams of silica gel (Grace Davison, grade 57, 10-20 mesh). The slurry was stirred at room temperature for 10 minutes. The H 2 O was then removed by rotovac. The solid was calcined at 550°C for 2 hours in flowing nitrogen. 10% Ba(OH) 2 /l%Au/SiO 2 In a 100 ml round bottom flask, 25 ml of a solution of 1.86% Ba (as the hydroxide) in H 2 O were combined with 1.18 grams of 0.3 molar gold chloride in H 2 O and 5.0 grams of silica gel. The slurry was stirred at room temperature for 10 minutes. The H 2 O was then rotovac removed. The solid was calcined at 550°C for 2 hours in flowing nitrogen. TABLE 1 Effects of Basic Catalysts on Condensation of γ-Butyrolactone with Formaldehyde Feed Catalyst Wt. % % Example No. Catalyst (R ats) wt, g Ratio 3 T, °C Conditions Conv b Yield c 1 MgO 2.0 1:1 380 12cc/minN 2 24 1.4 0.5 cc/h liq feed 6 h runtime 2 MgO 2.0 :1 380 12cc/minN 2 19 1.5 0.5 cc/h liq feed 6 h runtime 3 MgO 2.0 :1 340 12cc/minN 2 31 2.1 0.5 cc/h liq feed 6 h runtime 4 MgO 2.0 :1 340 12cc/minN 2 30 2.1 0.5 cc/h liq feed 6 h runtime 5 Ba(OH) 2 /SiO 2 1.0 :1 340 12cc/minN 2 36 14 0.5 cc/h liq feed 6 h runtime 6 Ba(OH) 2 /SiO 2 1.0 :1 370 12cc/minN 2 36 14 0.5 cc/h liq feed 6 h runtime 7 KOH/SiO 2 0.80 1:1 340 12cc/minN 2 37 5.8 0.5 cc/h liq feed 6 h runtime Feed Catalyst Wt. o //o % Example No. Catalyst (Repeats) Ratio 3 T, °C Conditions Conv b Yield c 8 CdO/SiOn 1.0 1 :1 340 12 cc/min N 2 34 3.0 0.5 cc/h liq feed 6 h runtime RbO 0 .oι MgOo . 99 1.0 1 :1 340 12 cc/min N 2 1 1 0.12 0.5 cc/h liq feed 6 h runtime 10 LYCOS2-NaZ 1.0 1 :1 340 12 cc/min N 2 46 0.01 0.5 cc/h liq feed 6 h runtime 1 1 RbO 0.05 MgO 0. 9 5 0.89 1 :1 340 12 cc/min N 2 32 1.7 0.5 cc/h liq feed 6 h runtime 12 H-Beta 1.0 1 :1 340 12 cc/min N 2 25 0.21 0.5 cc/h liq feed 6 h runtime 13 LZ-20 2.0 1 :1 340 12 cc/min N 2 69 1.1 0.5 cc/h liq feed 6 h runtime 14 Mg-ZSM-5 2.0 1 :1 340 12 cc/min N 2 70 1.9 0.5 cc/h liq feed 6 h runtime Feed Catalyst Wt. Example No. Catalyst (Repeats) wt, g Ratio 3 T, °C Conditions Conv b Yield c 15 LiOH/SiO 2 1.0 1:1 340 12 cc/min N 2 37 14 0.5 cc/h liq feed 6 h runtime 16 SrOH/SiO 2 1.0 1:1 340 12 cc/min N 2 21 10 0.5 cc/h liq feed 6 h runtime 17 NaOH/SiO 2 1.0 1 :1 340 12 cc/min N 2 24 9 0.5 cc/h liq feed 6 h runtime 18 Ca(OH) 2 /SiO 2 1.0 1 :1 340 12 cc/min N 2 32 11 0.5 cc/h liq feed 6 h runtime 19 8% Ba(OH) 2 /SiO 2 (l) § 1.0 1 : 1 340 12 cc/min N 2 64 6.0 0.5 cc/h liq feed 6 h runtime 19a 8% Ba(OH) 2 /SiO 2 (2) § 1.0 1 :1 340 12 cc/min N 2 63 6.0 0.5 cc/h liq feed 6 h runtime 19b 8% Ba(OH) 2 /SiO 2 (3) § 1.0 1 :1 340 12 cc/min N 2 48 7.4 0.5 cc/h liq feed 6 h runtime Feed Catalyst Wt. % % Example No. Catalyst (Repeats) wt, g Ratio 3 T, °C Conditions Conv b Yield c 19c 8% Ba(OH) 2 /SiO 2 (4) § 1.0 1 :1 340 12 cc/min N 2 35 7.6 0.5 cc/h liq feed 6 h runtime 19d 8% Ba(OH) 2 /SiO 2 (5) § 1.0 1 :1 340 12 cc/min N 2 65 4.5 0.5 cc/h liq feed 6 h runtime 20 8% Ba(OH) 2 /SiO 2 1.0 1 :1 340 5 cc/min N 2 48 9.9 0.5 cc/h liq feed 6 h runtime 21 8% Ba(OH) 2 /SiO 2 1.0 1 :2 340 12 cc/min N 2 41 17 0.5 cc/h liq feed 6 h runtime 21a 8% Ba(OH) 2 /SiO 2 (2) § 1.0 1 :2 340 12 cc/min N 2 48 14 0.5 cc/h liq feed 6 h runtime 22 8% Ba(OH) 2 /SiO 2 1.0 1 :2 340 12 cc/min N 2 48 16 0.5 cc/h liq feed 6 h runtime 23 Ba(OH) 2 /SiO 2 /Al 2 O 3 1.0 1 :2 340 12 cc/min N 2 35 6.6 0.5 cc/h liq feed 6 h runtime Feed Catalyst Wt. o //o % Example No. Catalyst (Repeats) wt, g Ratio 3 τ, °c Conditions Conv b Yield c 24 Ba(OH) 2 /TiO 2 2.0 1 :1 340 12 cc/min N 2 25 2.5 0.5 cc/h liq feed 6 h runtime 25 10% Ba(OH) 2 /ZrO 2 3.0 1 :1 340 12 cc/min N 2 20 2.1 0.5 cc/h liq feed 6 h runtime 26 10% Ba(OH) 2 /γ-Al 2 O 3 1.5 1 :1 340 12 cc/min N 2 32 4.5 0.5 cc/h liq feed 6 h runtime 27 10% Ba(OH) 2 /MgO 1.5 1 : 1 340 12 cc/min N 2 25 1.5 0.5 cc/h liq feed 6 h runtime 28 1 % Ba(OH) 2 /SiO 2 1.0 1 : 1 340 12 cc/min N 2 44 10.4 0.5 cc/h liq feed 6 h runtime 29 Ba(OH) 2 /SiO 2 1.0 1 :4 340 12 cc/min N 2 38 22 0.5 cc/h liq feed 6 h runtime a Feed wt. Ratio = Wt ofγ-butyrolactone:Wt. of formalin (37%) (1 : 1 wt ratio = 0.945 mole ratio) " % Conversion = ( Moles of γ-butyrolactone converted moles of γ-butyrolactone fed)*100 c % Yield = (Moles of α-methylene butyrolactone formed/Moles of γ-butyrolactone converted)* 100 § Parenthetical numbers indicate duplicate (repeats) runs TABLE 2 Effects of Changes in Reactant Ratios on Condensation of γ-Butyrolactone with Formaldehyde (4.0 g of Ba(OH) 2 /SiO 2 ) Example No. Feed Wt. Ratio T, °C Conditions % Conv b % Yield 0 30 1 :1 340 24 cc/min N 2 36 15 1.0 cc/h liq feed 6 h runtime 31 1:2 340 24 cc/min N 2 34 18 1.0 cc/h liq feed 6 h runtime 32 1 :4 340 24 cc/min N 2 44 19 1.0 cc/h liq feed 6 h runtime 33 1 :4 340 24 cc/min N 2 41 20 1.0 cc/h liq feed 6 h runtime 34 1 :8 340 24 cc/min N 2 35 30 1.0 cc/h liq feed 6 h runtime a Feed wt. Ratio = Wt of γ-butyrolactone: Wt. of formalin (37%) (1 : 1 wt ratio = 0.945 mole ratio) " % Conversion = ( Moles of γ-butyrolactone converted/moles of γ-butyrolactone fed)* 100 c % Yield = (Moles of α-methylene butyrolactone formed/Moles of γ-butyrolactone converted)* 100 Table 3 tion Variations on Conversion and Selectivity Feed Molar Ratio Catalyst (Formaldehyde: % /o Example No. Catalyst (Repeats) wt, g GBL) T, °C Conditions Conv b Selectivity 35 10% LaO/SiO, 1 8 320 24 cc/min N 2 16.0 >95 1 cc/h liq feed 0.25 h runtime 36 10% LaA/SiO 2 8 380 24 cc/min N 2 36.7 >95 1 cc/h liq feed 0.25 h runtime 37 0.42% LiOH/SiO*. 8 24 cc/min N 2 53.3 >95 1 cc/h liq feed 0.25 h runtime 38 10%Ba(OH) 2 /Subunit Carbon 8 340 24 cc/min N 2 9.73 >95 1 cc/h liq feed 0.25 h runtime 39 10%Ba(OH) 2 /l %Au/SiO 2 8 250 24 cc/min N 18.8 >95 1 cc/h liq feed 0.25 h runtime Feed Molar Ratio Catalyst (Formaldehyde: % % Example No. Catalyst (Repeats) wt, g GBL) τ, °c Conditions Conv b Selectivity 40 10%Ba(OH) 2 /l %Au/SiO 2 1 8 280 24 cc/min N 2 53.5 >95 1 cc/h liq feed 0.25 h runtime 41 10%Ba(OH) 2 /l %Au/SiO 2 320 24 cc/min N 2 36.9 >95 1 cc/h liq feed 0.25 h runtime a Molar Feed Ratio= Moles of formaldehyde: moles of γ-butyrolactone (Formaldehyde used as 37 wt% aqueous solution " % Conversion = ( Moles of γ-butyrolactone converted/moles of γ-butyrolactone fed)* 100 Ό Table 4 Conversion of γ-methyl-γ-Butyrolactone to α-methylene-α-methyl-γ-butyrolactone over 10% LaO/SiO 2 Feed Molar Ratio % Catalyst (Formaldehyde: o o Selectivity to Example No. Catalyst wt, g Me-GBL) τ> ° Conditions Conv b Me-MBL 42 10% LaO/SiO 340 48 cc/min N 2 40.1 >95% 1 cc/h liq feed 0.25 h runtime 43 10% LaO/SiO 2 340 48 cc/min N 2 23 >95% 1 cc/h liq feed 1 h runtime 44 10% LaO/SiO^ 300 48 cc/min N 2 33.9 >95% 1 cc/h liq feed 1 h runtime to o 45 10% LaO/SiO 7 340 24 cc/min N 2 57.7 >95% 1 cc/h liq feed 0.25 h runtime a Molar Feed Ratio= Moles of formaldehyde:moles of γ-butyrolactone (Formaldehyde used as 37 wt% aqueous solution) " % Conversion = ( Moles of γ-butyrolactone converted moles of γ-butyrolactone fed)*100 Table 5 Example 46 Reaction Of Formalin With Butyrolactone, Showing Effect Of Cyclic Regeneration With Air Under Varied Conditions Feed Molar Ratio Regeneration 5 Catalyst (Formaldehyde: 0 o o Cycle Catalyst wt, g GBL ) T, °C Conditions Conv b Selectivity 1 10%Ba(OH) 2 /SiO 2 1 8 340 48 cc/min N 2 36.0 >95 1 cc/h liq feed 0.25 h runtime 10%Ba(OH) 2 /SiO 2 340 48 cc/min N 2 23.4 >95 1 cc/h liq feed 1 h runtime 10%Ba(OH) 2 /SiO 2 340 48 cc/min N 2 34.9 >95 1 cc/h liq feed 0.25 h runtime 10%Ba(OH) 2 /SiO 2 340 48 cc/min N 2 25.00 >95 1 cc/h liq feed 1 h runtime 10%Ba(OH) 2 /SiO 2 340 48 cc/min N 2 35.8 >95 1 cc/h liq feed 0.25 h runtime 10%Ba(OH) 2 /SiO 2 340 48 cc/min N 2 22.6 >95 1 cc/h liq feed 1 h runtime Feed Molar Ratio Regeneration 5 Catalyst (Formaldehyde: 0/ o/ /o /o Cycle Catalyst wt, g GBL) T, °C Conditions Conv b Selectivity 10%Ba(OH) 2 /SiO 2 1 8 340 48 cc/min N 2 34.0 >95 1 cc/h liq feed 0.25 h runtime 10%Ba(OH) 2 /SiO 2 340 48 cc/min N 2 21.9 >95 1 cc/h liq feed 1 h runtime a Molar Feed Ratio= Moles of formaldehyde:moles of γ-butyrolactone (Formaldehyde used as 37 wt% aqueous solution b % Conversion = ( Moles of γ-butyrolactone converted moles of γ-butyrolactone fed)* 100 c After each reaction cycle reactant feed was stopped. Reactor was heated to 450°C with air feed for 15 min. Reactor / catalyst temperature was then returned to 340°C, air was stopped and reactant feed reinitiated. Table 6 Example 47 Demonstration of Enhanced Conversion of GBL to MBL after recycling Cat Feed Rctr GBL/MBL Vol Molar Feed N2 CT TOS Temp Molar Ratio Norm Catalyst (cc) Ratio cc/hr ccm (s) (h) (C) after Rx % GBL conv BaO/l%Au/SiO 7 2 8:1 2 48 1.5 0.25 340 0.55 28.6 Example 47 illustrates that the conversion of γ-butyrolactone (GBL) to α-methylene butyrolactone (MBL) is enhanced if the reactor effluent is recyceld a second time through the reactor containing the catalyst. As is seen in the table above, the molar ratio of GBL/MBL drops from 1 to 0.55 after a second exposure to the catalyst under reaction conditions, indicating further conversion of GBL to MBL.

Claims: CLAIMS What is claimed is: 1. A process for preparing α-methylenelactones of Formula II comprising heating lactones of Formula I and formaldehyde in the vapor phase at a temperature of above 200°C in the presence of a basic catalyst: Formula I Formula II wherein, w=l-l l ; R 1 , R 2 , R 3 and R 4 taken independently are hydrogen, hydrocarbyl or substituted hydrocarbyl, C j -C j g unsubstituted or substituted alkyl, unsubstituted or substituted alkenyl, unsubstituted or substituted cycloalkyl, unsubstituted or substituted cycloalkyl containing at least one heteroatom unsubstituted or substituted aromatic ring, and unsubstituted or substituted aromatic ring containing at least one heteroatom. 2. A process according to Claim 1 wherein R 1 , R 2 , R 3 and, R 4 are joined to form members of a ring structure selected from the group consisting of unsubstituted or substituted cycloalkyl, unsubstituted or substituted cycloalkyl containing at least one heteroatom in the ring unsubstituted or substituted aromatic ring, and unsubstituted or substituted aromatic ring containing at least one heteroatom in the ring. 3. The process of Claims 1 or 2 wherein the lactone of Formula I is γ-butyrolactone and the α-methylenelactone of Formula II is α-methylene-γ- butyrolactone. 4. The process of Claim 1 or 2 wherein R 3 is CH3. 5. A process according to Claim 1 wherein the temperature is from about 250°C to about 400°C. 6. A process according to Claim 5 wherein the temperature is from about 300°C to about 340°C. 7. A process according to Claim 1 wherein the base catalyst is selected from the group consisting of metal oxides, metal hydroxides, and metal carbonates. 8. A process according to Claim 7 wherein the base catalyst is selected from the group consisting of magnesium oxide, barium hydroxide, barium oxide, lanthanum oxide potassium hydroxide, cadmium oxide, rubidium oxide, lithium hydroxide, strontium hydroxide, sodium hydroxide, calcium hydroxide, barium carbonate and mixtures thereof. 9. A process according to Claim 7wherein the base catalyst is optionally supported on a suitable support. 10. A process according to Claim 7wherein the base catalyst optionally comprises a catalyst promoter. 11. A process according to Claim 10 wherein said catalyst promoter is gold. 12. A process according to Claim 9 wherein the suitable support is selected from the group consisting of silica, titania, zirconia, alumina, carbon, zeolites and mixtures thereof. 13. A process according to Claim 9 wherein the base catalyst is selected from the group consisting of magnesium oxide, barium hydroxide, barium oxide, lanthanum oxide, potassium hydroxide, cadmium oxide, rubidium oxide, lithium hydroxide, strontium hydroxide, sodium hydroxide, barium carbonate, calcium hydroxide , and wherein the suitable support is SiO 2 . 14. A process according to Claim 8 wherein the α-methylenelactone is produced at a selectivity of at least 50%. 15. A process according to Claim 14 wherein the α-methylenelactone is produced at a selectivity of at least 95%. 16. A process according to Claim 13 wherein the supported catalyst is Ba(OH) 2 /SiO 2 . 17. A process according to Claim 13 wherein the supported catalyst is La(OH) 2 /SiO 2 . 18. A process according to Claim 12 wherein the supported catalyst is Ba(OH) 2 /Carbon. 19. A process according to Claim 1 1 wherein the supported catalyst is Ba(OH) 2 /Au/SiO 2 . 20. A process according to Claim 1 wherein the formaldehyde is in the form of formalin. 21. A process according to Claim 1 wherein the formaldehyde is in the form of formaldehyde polymer. 22. A process for preparing α-methylenelactones of Formula II comprising: (a) heating lactones of Formula I and formaldehyde in the vapor phase at a temperature of above 200°C in the presence of a basic catalyst for a time sufficient for the α-methylenelactones of Formula II to be formed; Formula I Formula II wherein, w=l-l l; R 1 , R 2 , R 3 and R 4 taken independently are hydrogen, hydrocarbyl or substituted hydrocarbyl, Ci-Cig unsubstituted or substituted alkyl, unsubstituted or substituted alkenyl, unsubstituted or substituted cycloalkyl, unsubstituted or substituted cycloalkyl containing at least one heteroatom, unsubstituted or substituted aromatic ring, and unsubstituted or substituted aromatic ring containing at least one heteroatom, (b) separating the lactones of Formula I from the basic catalyst; (c) contacting the basic catalyst with oxygen for a time sufficient to permit catalyst regeneration; and (d) repeating steps (a) through (c). 23. A process according to Claim 22 wherein the contacting of the basic catalyst with oxygen of step (c) is for a time of about 5 min to about 60 min. 24. A process according to Claim 22 wherein the contacting of the basic catalyst with oxygen of step (c) is at a temperature of about 300°C to about 500°C. 25. A process according to Claim 24 wherein the contacting of the basic catalyst with oxygen of step (c) is at a temperature of about 400°C to about 425°C. 26. A process for preparing α-methylenelactones of Formula II comprising: (a) heating lactones of Formula I and formaldehyde in the vapor phase at a temperature of above 200°C in the presence of a basic catalyst for a time sufficient for the α-methylenelactones of Formula II to be formed in a reactor effluent; wherein, w=l-l l; R 1 , R 2 , R 3 and R 4 taken independently are hydrogen, hydrocarbyl or substituted hydrocarbyl, Cj-Cjg unsubstituted or substituted alkyl, unsubstituted or substituted alkenyl, unsubstituted or substituted cycloalkyl, unsubstituted or substituted cycloalkyl containing at least one heteroatom, unsubstituted or substituted aromatic ring, and unsubstituted or substituted aromatic ring containing at least one heteroatom, (b) collecting the reactor effluent of step (a); and (c) contacting the collected effluent with the base catalyst at a temperature of above 200°C. 27. The process of Claim 26 wherein steps (b) and (c) are repeated from about 1 to about 10 times.

Inventors: COULSON DALE ROBERT, MANZER LEO E, COULSON, DALE, ROBERT, MANZER, LEO, E.
Applicants: COULSON DALE ROBERT, DU PONT, MANZER LEO E, COULSON, DALE, ROBERT, E.I. DU PONT DE NEMOURS AND COMPANY, MANZER, LEO, E.
Application year: 2000
Main classification: C07D307
IPC codes: C07B61, C07D307