PROCESS FOR THE PREPARATION OF A SUBSTITUTED PYRONE

Abstract: There is provided a process for the preparation of 4-hy­ droxy-6-methyl-2-pyrone which comprises reacting dehydro­ actate acid (DHAA) with aqueous H₂SO₄ containing 90-99% by weight of H₂SO₄ at a temperature from 60°C to 140°C and un­ der a pressure of 10 millimetres of mercury gauge to 388 cen­ timetres of mercury gauge, wherein (A) the H₂SO₄ plus H₂O: DHAA weight ratio is from 0.8 to 3:1 and (B) the DHAA is initially reacted with from 91 to 99% H₂SO₄ followed by one or more staged H₂O additions during the reaction whereby the to­ tal weight of H₂O added and initially present in the H₂SO₄ charged is 10% or less of the weight of H₂SO₄ (100% basis) in­ itially charged, said staged H₂O addition(s) being optional when 93-96% H₂SO₄ is initially charged.

Description: PROCESS FOR THE PREPARATION OF A SUBSTITUTED PYRONE This invention concerns a process for the preparation of a substitute pyrone namely 4-hydroxy-6-methyl-2-ryone. The compound 4-hydroxy-6-methyl-2-pyrone (HMEP) has been used, inter alia, as an intermediate for the preparation of l-(4-chlorophenyl)-1,4-dihydro-6-methyl-4-oxo-3pyridazine carboxylates and related plant growth regulating agents (see West German Offenlegungsschrift No. 2,808,795). HMEP has been prepared, inter alia, by deacetylation of dehydroacetic acid (DHAA) in hot 90% sulfuric acid, see W. Borsche and B.K. Blount, Berichte der Deutschen Chemischen Gesellschaft, 65, 827 (1932), J.N. Collie, J. Chem. Soc., 59, 607-609 (1891) and U.S. Patent No. 3,657,426. The acidic deacetylation conditions using H2S04 are critical since heating DHAA in 85% sulfuric acid produces primarily the rearrangement product 2,6-dimethyl-4-pyrone3-carboxylic acid; see J.N. Collie and T.P. Hilditch, J. Chem. Soc., 91, 787 (1907). The preparation of HMEP from DHAA in sulfuric acid as disclosed by J.N. Collie, is described in more detail by Borsche and Blount. This Collie-Borsche-Blount procedure is not suitable for batch production of HMEP because of the enormous rates of heat transfer that would be required. It or any other procedure requiring such large ratios of H2S04 (3 to 1) and quench water (4 to 1) to DHAA suffers from problems of HMEP losses in the quench mixture, large volumes of acidic waste to be treated or recycled, and low kettle productivity. Moreover, the procedures are run under conditins (ca. two minutes at 130 C. or an unspecified time at 120 C.) that cannot readily be duplicated or controlled on a commercial scale. This invention provides a process for the preparation of HMEP which is more advantageous than the known procedures for deacetylating DHAA using sulfuric acid. The process of the invention comprises reacting dehydroacetic acid (DHAA) with aqueous H2 504 containing 90-99% by weight of H2SO4 at a temperature from 60 C. 40 140 C. under a pressure of 10 millimetres of mercury gauge to 388 centimetres of mercury gauge, wherein (A) the H2S04 plus H20 : DHAA weight ratio is from 0.8 to 3:1 and (B) the DHAA is initially reacted with from 91% to 99% H2S04 followed by one or more staged H20 additions during the reaction whereby the total weight of H20 added and initially present in the H2 504 charged is 10% or less of the weight of H2S04 (100% basis) initially charged, said staged H20 additicn(s) being optional when 93-96% H2S04 is initially charged. Preferably 94-99% H2S04 is initially charged. A preferred process of this invention involves initially charging 94 to 99% sulfuric acid followed by one or more staged water additions. A preferred temperature range for the process of this invention is from about 800 to about 1200C. The process of the present invention can be carried out either as a batch process or as a continuous process. A more preferred process of the present invention involves initially charging 94 to 99% sulfuric acid followed by one or more staged additions of water whereby the total weight of water added in staged increments and present initially in the H2S04 is from 4% to 7% of the weight of the sulfuric acid (100% basis) initially charged. Preferred reaction times are from 10 minutes to 15 hours. The preferred reaction pressure is 760 millimetres of mercury. The advantage of the process of the invention over the prior art is that in the process of the present invention the water content of the sulfuric acid utilized in the HMEP preparation is controlled so that the initial sulfuric acid concentration is between 91% and 99%, preferably about 94-96%, more preferably 96-98 Ï H2 504 with about- 2-38 by weight of water added in staged increments. The advantages obtainable by the process include: 1. The possibility of using lower minimum H2SO4/DHAA charge ratios resulting in reduced waste volumes and higher productivity. Using staged water additions and an initial charge of 1.4-2.2 parts by weight of 96.9-97.5% H2S04 per part by weight of DHAA, the process can provide isolated HMEP yields of 71-80% after 2.1-2.5 hours at 1O00C. The charge ratios can represent 47%-73% of the sulfuric acid charge utilized in the Collie-Borsche-Blount procedure. This improvement further permits 25%-38% reductions in the weight of quench water utilized as well. The overall result is a large reduction in the volume of acidic waste produced and a large increase in kettle productivities. 2. Increased yield and selectivity over those obtained with 90% sulfuric acid initially charged, especially at sulfuric acid/DHAA weight ratios of 2.5 to 1.0 or less. The isolated HMEP yields of 71-80% discussed above with staged water additions and an isolated HMEP yield of 75% obtained using 94% H2S04 and DHAA in a 2.0 to 1.0 weight ratio are higher than most of the yields reported using the Collie-Borsche-Blount procedure. In addition, they are much higher than the isolated HNEP yields obtained using 90% sulfuric acid at 100 C. with lower sulfuric acid/DHAA weight ratios. For example, use of 90% sulfuric acid at a 2.37:1-aqueous-H2S04/DHAA ratio gave only a 60.5% isolated A.I. yield of HNIEP while at a 1.75:1 weight ratio, the isolated HMEP yield was only 31.8%. Hence the use of the drier sulfuric acid and/or staged water additicn(s) in the process of the invention greatly improves the yield and selectivity of HMEP production at sulfuric acid/DHAA weight ratios of 2.5 or less to 1.0. 3. Ready applicability to batch or continuous processing. The lower reaction temperature and improved control of the water content of the sulfuric acid in thins invention gives a process which is applicable to batch or continuous processing.- Several 300-gallon (scale) batches of HMEP have been conducted using a preferred version of the invention (see Example 10 appearing later). The present invention consists of controlling the water content of the sulfuric acid so that the initial sulfuric acid concentration is between 91% and 99%, preferably about 94%-96%, more preferably 96-98% when 2-3% of water is added in staged increments as the reaction proceeds. It further consists of reductions in the reaction temperature.and lengthening of heating and cooling cycles to permit a more readily controlled deacetylation. The invention is based upon the discovery that keeping the acid initially charged drier than the 90% sulfuric acid utilized in the prior art permits a more selective, practical preparation of HMEP to occur at lower DHAA/sulfuric acid ratios. The preparation is especially selective if the reaction is initiated with relatively dry (ca. 97% or more) sulfuric acid and small incremental portions of water are added during the deacetylation to bring the total water content up to the equivalent of starting with 93-95% sulfuric acid.. If, however, the acid is too dry (e.g., 97%-99% sulfuric acid) with no incremental water additions), the deacetylation stalls and much DHAA remains uncoverted, especially when the H2S04/DHAA weight ratio is less than about 2.5 to 1.0. On the other hand, when the acid initially charged is too wet (e.g., the 90% sulfuric acid utilized in the prior art), the yield of the by-products 2,6-dimethyl-4pyrone-3-carboxylic acid (D.NSCA) and 2,6-dimethyl-4-pyrone (DMP) increases, especially if the H2S04/DHAA weight ratio is less than about 2.5 to 1.0. The following examples 1-7 and 10 are provided to illustrate the process of the present invention. Examples 8 and 9 are presented by way of comparison. All experiments except Examples 1, 2 and 10 were conducted in the laboratory using a stoppered 300 ml. three-neck, round-bottom flask equipped with a mechanical paddle stirrer and a thermometer. The flask was heated by a heating mantle controlled by an Instruments for Research and Industry Therm-o-Watch controller. Examples 1 and 10 were run in 38 litre (10 U.S. gallons) and 1135 litre (300 U.S. gallons) glass-lined kettles, respectively, and heated with steam or hot water. In all cases except Examples 1 and 10, the dehydroacetic acid was charged before the sulfuric acid, but the order of addition is immaterial to the invention. @ Quenches of the reaction mixtures were conducted using 1.39 or 1.77 parts by weight of quench; water per part weight of sulfuric acid (100% basis) used. - The decrease in isolated yields using the lower quench ratio was only 0.6%. The chemical yields of DHAA, HMEP, DMPCA and DMP in the unquenched reaction mixtures were determined by NMR spectroscopy of the (ring) vinyl peaks at g5.5-7.5. EXAMPLE 1 6.67 Kg (14.7 lbs) of dehydroacetic acid and 13.24 Kg (29.2 lbs) of 96.9% sulfuric acid were charged to an unpressurized glass-lined 38 1 (10 U.S. gallon) kettle and heated with stirring over 65 minutes to 98 C. Then the mixture was held for 2.5 hours at 96-98 C. Two 14.2g (five-ounce) tap water charges were added. after 30 ar;d 60 minutes of the hold period had elapsed; during the hold period, the color of the reaction mixture changed from a golden brown to a reddish brown. 28G (one-ounce) samples were taken for NMR analysis after one hour and two hours of the hold period had elapsed. After the 2.5 hour hold, the agitated reaction mixture was cooled to 22 C. over 65 minutes. Then 22.8 Kg (50.2 1bs) of tap water were added to the reaction mixture over 105 minutes at 22-46 C.; a finely divided white slurry of HMEP precipitated. The HMEP slurry was cooled to 10 C and filtered onto a chock filter equipped with a cheesecloth. The wet cake was washed with two 10 Kg (22.0 lbs) portions of tap water and sucked dry to give 7.58 Kg (16.7 lbs) of of 49.7% solids-wet HMEP. The crude isolated yield of HMEP was 3.76 Kg (8.3 lbs) or 75.6%; the purity of a sample of the HMEP was 98-1008 (four determinations) by TLC densitometry. NMR analysis of the two-hour sample indicated a 78.5% reaction yield of HMEP and a 14.5% yield of DMPCA with 7.0% uncoverted DHAA. EXAMPLE 2 111.3 G of DHAA and 220.4 G of 96.9% H2S04 were charged to a 1,000-ml., 4-necked round bottomed flask equipped with an addition funnel,.paddle stirrer and thermometer. The stirred mixture was rapidly heated to 1100C. and held for 5 hours at 109-1120C. After 3 hours, a 1.807 g water charge was added, after 4.27 hours, a second 1.800 g water charge was added. Four NMR samples removed during the hold period gave the following analysis: Time ' %-DHAA % HMEP % DMPCA 45 min. 34.5 54.5 11.0 2.5 hr. 26.9 57.2 15.9 3.75 hr. 7.5 74.8 17.7 5.0 hr. 2.7 79.5 18.8 At the end of the hold period, the mixture was cooled and quenched with 380 g of tap water at 20.0-52.5 C. over 28 minutes. The resulting white HMEP slurry was cooled to 0-50C., held for one hour and suction filtered to give a HMEP wet cake. The HMEP was washed twice with 165 g portions of tap water and vacuum dried to give 62.4 g of 95.4% pure dry HMEP. The corrected HMEP yield was 72%. Examples 3-6 and 10 in Table 1 give further documentation of the use of staged water additions and low H2S04/DHAA ratios under the claims of this invention. Example 7 in Table 1 illustrates the preparation of HMEP under this invention using a 2.0/1.0 94% H2S04/DHAA weight ratio. Comparative examples 8 and 9 in Table 1 illustrate the preparation of HMEP at lower temperatures and lower sulfuric acid ratios using the 90% sulfuric acid specified by the prior art. The yields of BMEP are clearly lower than those obtained using similar H2S04/DHAA ratios under the drier conditions and/or staged water addition(s) used in the process of this invention. Example 10 illustrates the large scale preparation of HMEP-using one of the preferred sets of conditions of this invention. The results of these experiments are presented in Table II below. In Table II a dash indicates "not determined". Table 1 - Preparations of HMEP By Deacetylation of DHAA Reaction Conditins Weight of Weight Init. Cone. Water Charges Example Time Temp. C. Aqueous DHAA of H2SO4 and Times after Start H2SO4 of Hold Period 1 2.5 hr. 96 - 98 13.24 Kg 6.67Kg 96.9% 142g., 30 min. 142g., 60 min. 2 5.0 hr. 109-112 220.4 g 111.3 g. 96.9 1.81 g., 3 hr. 1.80 g., 4.27 hr. 3 1.0 hr. 98 - 105 110.5 g. 50.4 g. 97.1 1.01 g., 30 min. 4 2.0 hr. 98 - 105 81.5 g.a 50.43 g. 97.5 0.94 g., 30 min. 0.95 g., 60 min. 5 2.5 hr. 96 - 103 71.1 g. 50.4 g 96.9% 0.96 g., 21 min. 0.77 g., 60 min. 0.81 g., 105 min. 6 3.1 hr. 98 - 103 52.9 g.a 50.45 g 99.1 0.72 g., 30 min. 0.68 g., 62 min. 0.29 g., 122 min. 7 2.1 hr. 99 - 106 103.0 g.a 50.4 g 94.0 none 8 2.0 hr. 99 - 105 119.2 g.a 50.4 g 90.0 none 9 2.0 hr. 99 - 105 97.9 g. a 55.95 g. 90.0 none 10 3.65 hr. 98 - 111 446 Kga 225 Kg 97.1 6.12Kg. 30 min. 6.12Kg. 60 min. B Aetual charges were as follows: Example 4, 76.7 g., 97.1% H2SO4 and 4.80 g., 104.1% H2SO4: Example 6, 37.85 g. of 97.1% H2SO4 and 15.05 g. of 104.1% H2SO4; Example 7, 100.8 g. of 96.0% H2SO4 and 2.2 g. of water; Example 8, 111.8 g. of 96.0% H2SO4 and 7.4 of water; Example 9. 98.8 g. of 96.0% H2SO4 and 6.1 g. of water; and Example 10, 227 Kg. of 99.1% of H2SO4 216 Kg. of 96.6% H2SO4 and 3.54 Kg. of water. TABLE II - Distribution OF Reaction Mixture Components Mole % of Reaction Mixture Componentsa Analysis of Isolated Products soleted Example No. HMEP DHAA DMPCA DMP Crude Yield % HMEP Yield 1 78.5 7.0 19.5 - 3.76Kg. 75.6% 98 74.0% 2 79.5 2.7 18.8 - 62.4 g. 75.5% 95.4 72.0% 3 91.1 0.0 8.9 - 30.4 g., 80.4% - 4 81.0 4.3 14.7 - 28.4 g., 75.0% 75.0 5 83.9 8.0 16.1 - 27.8 g., 73.7% 96.8 71.0 6 20.5 g., 54.2% 54.2 7 74.9 9.1 12.8 3.3 28.4 g., 75.1% 101.5 75.1 8 69.3 0.6 25.8 4.4 23.0 g., 61.0% 99.2 60.5 9 43.9 0.0 43.5 12.6 14.3 g., 34.1% 93.3 31.8 10 88.6 4.1 9.35 - 134.3Kg. 79.5% 100 79.5 a Mole % of reaction mixture components determined by nmr analysis, b DMPCA is 2,6-dimethyl-4-pyrone-3-carboxylic acid and DMP is 2,6-dimethyl-4-pyrone.

Claims: Claims: 1. A process for the preparation of 4-hydroxy-6-methyl 2-pyrone which comprises reacting dehydroacetic acid (DHAA) with aqueous H2 SO4 containing 90-99% by weight to of H2 SO4 at a temperature from 60 and under a pressure of 10 millimetres of mercury gauge to 388 centimetres of mercury gauge, wherein (A) the H2S04 plus H2O: DHAA weight ratio is from 0.8 to 3:1 and (B) the DHAA is initially reacted with from 91% to 99% H2S04 followed by one or more staged H20 additions during the reaction whereby the total weight of H20 added and initially present in the H2 SO4 charged is 10% or less of the weight of H2S04 (100% basis) initially charged, said staged H20 addition(s) being optional when 93-96% H2S04 is initially charged. 2. A process as claimed in Claim 1, wherein 94%-99% H2SO4 -is initially charged. 3. A process as claimed in Claim 1, wherein 94% to 99% H2 504 is initially charged followed by one or more of said staged H20 additions. 4. A process as claimed in Claim 3, wherein the reacticn temperature is from 800C to 12O0C. 5. A process as claimed in Claim 4, wherein the total weight of H20 added and initially present in the H2 504 charged is from 4-7% of the weight -of H2S04(100% basis) initially charged. 6. A process as claimed in Claim 5, wherein the reaction time is from 10 minutes to 15 hours an the reaction pressure 760 millimetres of mercury.

Inventors: OPIE, THOMAS RANSON
Applicants: ROHM AND HAAS COMPANY
Application year: 1982
Main classification: C07D309
IPC codes: C07D309