Mixed metal phosphorus oxide catalysts for the oxidative dehydrogenation of carboxylic acids

Abstract

A process is provided for the oxydehydrogenation of saturated carboxylic acids with oxygen in the presence of iron phosphorus oxide catalysts containing promoters selected from the group Ag, Al, B, Cd, Co, Cr, Cu, Ga, Ge, In, Mn, Ni, Te, Th, Ti, Tl, U, V, Zn, Zr, rare earths and mixtures thereof.

Description

BACKGROUND OF THE INVENTION

This invention relates to the catalytic, oxidative dehydrogenation of saturated carboxylic acids to their corresponding unsaturated acids. More particularly, it is directed to the production of unsaturated carboxylic acids such as methacrylic acid from saturated carboxylic acids such as isobutyric acid utilizing promoted iron phosphorus oxide catalysts.

The production of unsaturated carboxylic acids from their corresponding saturated acids using iron phosphorus oxide catalysts, with or without various promoters, is disclosed in the art.

U.S. Pat. No. 3,948,959 discloses the preparation of unsaturated acids by oxidation of the corresponding saturated acid using iron phosphorus oxide catalysts promoted with Li, Na, K, Rb, Cs, Mg, Ca, Sr and Ba. U.S. Pat. Nos. 3,634,494; 3,652,654; 3,855,279; 3,917,673 and 4,029,695 disclose the preparation of unsaturated acids and esters from saturated acids and esters using iron phosphorus oxide catalysts, containing bismuth and/or lead promoters, optionally with other promoter elements, including Mn, U, Pr, Ca, Sr, and Cr. Prior art catalysts characteristically have exhibited short life and thermal instability.

It is therefore an object of the present invention to provide a process for the production of unsaturated acids from their corresponding saturated acids.

It is a further object of the invention to provide catalysts for said process having improved catalyst life and thermal stability.

It is a further object of the invention to provide catalysts for said process having improved activity and selectivity.

SUMMARY OF THE INVENTION

We have found that unsaturated acids, particularly methacrylic acid, can be produced from their corresponding saturated acids, such as isobutyric acid, using iron phosphorus oxide catalysts promoted with particular elements, in increased yields corresponding to an increase of catalyst activity and/or selectivity over prior art catalysts. The catalysts of the present invention exhibit increased life and thermal stability with respect to the prior art catalysts.

Although promoters such as Mn, U, Cr, were disclosed as being suitable promoters in an iron lead mixed phosphate system if present in low amounts, and promoters such as Co, Ni, Cu, Zn, Cd and Ce were disclosed for that system as less than suitable promoters, we have found that these elements exhibit excellent promotional activity in the iron phosphorus oxide system for the oxydehydrogenation of saturated carboxylic acids wherein the iron phosphorus oxide is free of lead phosphate or oxide.

In general, the process of the present invention includes the preparation of unsaturated acids by contacting their corresponding saturated acids with molecular oxygen or an oxygen-containing gas in the vapor phase, at a reaction temperature of about 250.degree. C. to 600.degree. C. in the presence of a catalyst having the empirical formula

A.sub.a Fe.sub.b P.sub.c D.sub.d O.sub.x wherein A is selected from the group Al, B, Be, Cd, Co, Cr, Ga, Ge, In, Ni, Te, Th, Ti, Tl, U, V, Zn, Zr, rare earths and mixtures thereof, wherein D is selected from the group Ag, Cu, Mn and mixtures thereof, and wherein a=0-1.0 b=0.75-1.5 c=1.0-2.0 d=0-2.0 a+d is greater than zero, and x is the number of oxygens needed to satisfy the valence requirements of the remaining elements.

Preferably a equals 0.15-0.5 and d equals 0.2-1.5.

The present invention further provides oxydehydrogenation catalysts having the empirical formula:

A.sub.a Fe.sub.b P.sub.c D.sub.d O.sub.x wherein A is selected from the group Cd, Cr, Ge, Te, Th, Ti, U, V, Zr, rare earths and mixtures thereof; wherein D is selected from the group Ag, Cu, Mn and mixtures thereof, and wherein a=0-1.0 b=0.75-1.5 c=1.0-2.0 d=0-2.0 a+d is greater than zero, and x is the number of oxygens needed to satisfy the valence requirements of the remaining elements.

Preferably a equals 0.15-0.5 and d equals 0.2-1.5. Preferred rare earth metal promoters are La, Ce, Nd, Sm, Eu, Dy, Ho, Tm, Yb and Lu.

DETAILED DESCRIPTION OF THE INVENTION

Saturated carboxylic acids are oxidatively dehydrogenated according to the process of the present invention in the vapor phase, in the presence of promoted iron phosphorus oxide catalysts to form the corresponding unsaturated acid. The saturated acids preferably correspond to the formula ##STR1## wherein R.sub.1, R.sub.2, and R.sub.3 are each independently selected from the group consisting of hydrogen and alkyl groups containing 1 to 4 carbon atoms. The acids may contain other functional groups such as aryl or nitrile, provided the functional groups do not interfere with the dehydrogenation reaction, under the reaction conditions required. The dehydrogenation occurs essentially in the alpha, beta position.

The process of the present invention is highly suitable for the oxidative dehydrogenation of isobutyric acid to methacrylic acid.

The promoted iron phosphorus oxide catalysts of the present invention are represented by the formula set forth above. These catalysts may be prepared according to methods known in the art.

One method of preparing the catalysts of the present invention includes introducing a compound of iron, and a compound containing the promoter element into water and contacting with a phosphorus compound, or the iron and promoter containing compound are introduced into an aqueous solution of phosphoric acid. Preferably, the compounds used containing iron and the promoter elements are soluble in water, and may include salts such as nitrates, halides, sulfates, acetates, carbonates, formates and the like. The resulting solution or slurry is evaporated to dryness, and the resulting solid is calcined at from about 300.degree. to 700.degree. C. Alternatively, the catalyst may be prepared in an organic liquid medium. Alternatively, the aqueous solution or slurry can be adjusted to a pH of about 5-6 before drying.

The catalyst may be formed into tablets, pellets and the like, and may be prepared for use in either fixed or fluid beds. The catalyst may be combined with inert diluents such as silica. Alternately, the catalyst may be coated upon inert supports, such as silica, alumina, alumina-silica, silicon carbide, titania, zirconia, zeolites and clays such as kieselguhr. Techniques of coating are included in U.S. Pat. No. 4,077,912, The inert supports preferably are of at least about 20 microns in diameter.

The promoted iron phosphorus oxide catalysts of the present invention exhibit enhanced activity and selectivity for the oxydehydrogenation of saturated carboxylic acids, particularly isobutyric acid. The catalysts also exhibit long life and thermal stablity.

The saturated acids are contacted with the catalyst in the vapor phase, together with molecular oxygen. The molecular oxygen is most conveniently added as air, but synthetic streams containing oxygen are also suitable. In addition to the carboxylic acid feed and molecular oxygen, other gases may be added to the reactant feed. For example, steam is preferably added to the reactant feed to aid in the reaction, although the mechanism by which it does so is not certain. Inert diluents such as nitrogen, carbon monoxide, carbon dioxide and argon may also be added.

The molar ratio of the reactants may vary widely and are not critical. The ratios of carboxylic acid:air:steam are in the range of 1:2.5-50:0-50 and are preferably 1:3-10:10-30. Diluents may be present in the range of 0-40 moles per mole of carboxylic acid.

The reaction temperature may vary widely and is dependent upon the particular carboxylic acid and catalyst employed. Normally, temperatures of about 250.degree. to 600.degree. C. are employed with temperatures of 325.degree.-450.degree. C. being preferred.

The contact time may vary from a fraction of a second to about 50 seconds. In fixed bed reactions the contact time is preferably about 0.5 seconds to about 10 seconds, for fluid bed, preferably from about 2 seconds to about 20 seconds. The reaction may be conducted at atmospheric, superatmospheric or subatmospheric pressure, preferably from about 1 psia to about 100 psia, most preferably between about 10 to about 30 psia.

In the production of methacrylic acid from isobutyric acid, the major by-product is acetone (generally about 5-15% yield) which may be removed from the product by conventional methods.

SPECIFIC EMBODIMENTS OF THE INVENTION

Catalysts tested in the below examples were prepared according to the following procedure.

Fe(NO.sub.3).sub.3 .multidot.9H.sub.2 O, the appropriate promoter metal nitrate and H.sub.3 PO.sub.4 (85%) were added to water in the amounts necessary to provide the molar ratios set forth in the tables below, for each of the particular catalysts reported. The solution of the components was evaporated to a dry paste with heating and stirring. The paste was dried for about 16 hours at 110.degree. C., and the resulting solid was calcined for about 2 hours at 540.degree. C. The solid was crushed and screened to 14-30 mesh (0.595-1.41 mm).

The catalyst particles were processed according to the examples below, and were tested for the oxydehydrogenation of isobutyric acid to methacrylic acid in a 20 cc fixed bed reactor. The reactor consisted of a length of stainless steel tubing having an outer diameter of about 1.3 cm, and containing a full length 0.31 cm diameter axial thermowell. The reactor was heated with a split stainless steel block furnace.

The isobutyric acid was fed to the reactor by passing air through a saturator filled with isobutyric acid and maintained at a temperature of 108.degree. C. Water was fed by means of a tubing pump and vaporized in a compartment maintained at about 154.degree. C. before entering the reactor. Liquid products were analyzed on a Hewlett Packard 5710 A F.I.D. gas chromatograph. Gaseous products were analyzed on a conventional split column system.

The test reactions were run a atmospheric pressure, unless otherwise noted. Reaction conditions such as temperature, feed ratios, contact time and catalyst working rate (WWH=weight of isobutyric acid/weight of catalyst/hour) are listed in the tables below. Results of the tests reported in the tables below are reported in terms as follows: ##EQU1##

100% Active Catalysts

Examples 1-13

Iron phosphorus oxide catalysts promoted with manganese (added as manganese nitrate) in varying molar ratios were prepared according to the procedure set forth above. The crushed and screened catalysts were charged to the reactor. The results of the tests, together with the amount of manganese in the catalysts are reported in Table I.

Examples 14-39

Iron phosphorus oxide catalysts promoted with silver (added as silver nitrate) in varying amounts were prepared according to the procedure set forth above. The crushed and screened catalysts were charged to the reactor. The results of the tests, together with the amount of silver in the catalysts are reported in Table II.

Examples 40-50

Iron phosphorus oxide catalysts promoted with copper (added as copper nitrate) in varying amounts were prepared according to the procedure set forth above. The crushed and screened catalysts were charged to the reactor. The results of the tests, together with the amount of copper in the catalysts are reported in Table III.

Examples 51-62

Catalysts of the formula TH.sub.0.2 Fe.sub.1 P.sub.1.84 O.sub.x were prepared from iron and thorium nitrates according to the procedure set forth above. The crushed and screened catalysts were charged to the reactor. The results of the tests are reported in Table IV.

Examples 63-118

Catalysts having the formula A.sub.a Fe.sub.1 P.sub.1.84 O.sub.x were prepared with the designated promoter metal nitrates as set forth in the procedure above, The crushed and screened catalysts were charged to the reactor. The results of the tests and the amount and identity of the promoter metal are reported in Table V.

Examples 119-124

Catalysts having the formula A.sub.a Fe.sub.1 P.sub.1.84 D.sub.d O.sub.x containing two promoter elements were prepared as set forth in the procedure above. The crushed and screened catalysts were charged to the reactor. The results of the tests and the amounts and identities of the promoters are reported in Table VI.

Diluent-containing catalysts

Examples 125-132

Catalysts having the formula Ag.sub.0.8 Fe.sub.1 P.sub.1.84 O.sub.x were prepared according to the procedure set forth above, with the addition of various amounts of silica to the catalyst during preparation by slurrying in water. The crushed and screened catalysts were charged to the reactor. The results of the tests and the weight percents of active material and silica are reported in Table VII.

Coated Catalysts

Examples 133-140

Catalysts of the formula A.sub.a Fe.sub.1.0 P.sub.1.84 O.sub.x were prepared according to the procedure set forth above. The crushed and screened catalysts were ground to a fine powder, and coated upon Alundum SA 5209 spheres (trade designation of Norton Company) according to the method set forth in U.S. Pat. No. 4,077,912, with water as the wetting agent. The results of the tests, the catalyst used and the weight percent of catalyst loading (based upon total weight) are reported in Table VIII.

Examples 141-150

Catalysts of the formula A.sub.0.6 Fe.sub.1.0 P.sub.1.8 O.sub.x were prepared according to the procedure set forth above, except that the pH of the aqueous solution was adjusted to about 6 by addition of concentrated NH.sub.4 OH solution. The dried catalysts were ground to a fine powder and coated on Alundum which had been ground to 10-20 mesh, using the method set forth in U.S. Pat. No. 4,077,912 with absolute ethanol as a wetting agent. The coated particles were dried at 175.degree. C. for 30 minutes and calcined for 2 hours at 540.degree. C. The catalyst loading was about 17 weight percent.

The catalysts were tested in a 5 cc reactor consisting of a 61/2" (16.5 cm) stainless steel tube of 5/16" (0.8 cm) inner diameter immersed in a molten salt bath. Feed ratios were 1 IBA/5 AIR/25 H.sub.2 O at a contact time of about 2 seconds. Reaction temperature was 415.degree. C. Run time was about one hour. Results of the tests and the identity of the promoter elements contained in the catalysts are listed in Table IX.

We have found that the iron phosphorus oxide catalysts, promoted according to the present invention, are not particularly suited to the oxydehydrogenation of saturated carboxylic acid esters, due to the hydrolysis of the ester by water formed as a by-product of the reaction even if steam is not co-fed. The oxydehydrogenation of the ester with these catalysts generally results either primarily in the formation of the unsaturated acid, or in low conversions to both acid and ester.

A catalyst of the formula Th.sub.0.2 Fe.sub.1.0 P.sub.1.84 O.sub.x was prepared according to the procedure of examples 51-62. Methyl isobutyrate was oxydehydrogenated over this catalyst in the 20 cc reactor described above at 444.degree. C. with a feed ratio of MlBA/AIR/H.sub.2 O/N.sub.2 equals 1/4.5/18/7.8 and a contact time of 1.6 seconds. Total conversion was 95.6%, but yield of methyl methacrylate was only 11.6% with a yield of methacrylic acid of 38.6%. With no steam being co-fed, (replaced by nitrogen), yield of methyl methacrylate increased to 23%, but total conversion decreased to 47.8%.

As is demonstrated by the test results reported in Tables I through IX, promoted iron phosphorus oxide catalysts according to the present invention exhibit high activity and selectivity in the oxydehydrogenation of saturated carboxylic acids, particularly isobutyric acid, to the corresponding unsaturated acid. The catalysts of the invention additionally exhibit long life and thermal stability, as is demonstrated by the test results reported in the tables.

Thus it should be apparent to those skilled in the art that the subject invention accomplishes the objects set forth above. It is to be understood that the subject invention is not to be limited by the examples set forth herein. These have been provided merely to demonstrate operability, and the selection of iron and phosphorus-containing compounds, promoter element-containing compounds, preparation techniques, reaction feedstocks and reaction conditions can be determined from the total specification disclosure provided without departing from the spirit of the invention herein disclosed and described, the scope of the invention including modifications and variations that fall within the scope of the attached claims.

TABLE I__________________________________________________________________________OXYDEHYDROGENATION OF ISOBUTYRIC ACID TO METHACRYLIC ACID OVER Mn.sub.aFe.sub.1.0 P.sub.1.84 O.sub.x CATALYSTS HoursExample Molar Feed Ratio Temperature Contact Methacrylic Acid % OnNo. Ratio-Mn (a) 1BA/Air/H.sub.2 O .degree.C. Time (Sec.) WWH % Yield % Selectivity Conversion Stream__________________________________________________________________________1 0.33 1/4.8/24.7 429 0.9 0.3 58.7 64.1 91.6 222 0.33 1/4.8/24.7 447 0.9 0.3 54.9 57.0 96.4 413 0.33 1/4.1/24.7 410 1.0 0.34 76.1 76.9 98.9 22.54 0.33 1/4.1/24.7 410 1.0 0.34 74.6 75.4 98.8 475 0.5 1/4.4/24.7 393 1.0 0.34 76.2 77.6 98.3 366 0.5 1/3.4/24.7 390 1.0 0.34 76.7 81.8 93.8 58.57 0.5 1/3.7/24.7 419 1.0 0.34 79.3 81.5 97.3 114.58 0.7 1/4.1/24.7 368 1.0 0.51 77.8 79.7 97.5 24.59 0.7 1/3.3/24.7 397 1.0 0.51 77.8 81.5 95.4 50.510 0.7 1/3.7/24.7 409 1.0 0.51 74.9 79.1 94.7 73.511 1.0 1/4.7/32.3 399 0.7 0.40 67.9 70.8 95.9 2212 1.0 1/4.7/37.3 389 0.7 0.40 68.2 69.7 93.5 4513 1.0 1/4.7/25.3 413 0.9 0.40 63.8 69.1 92.4 54__________________________________________________________________________ TABLE II__________________________________________________________________________OXYDEHYDROGENATION OF ISOBUTYRIC ACID TO METHACRYLIC ACID OVER Ag.sub.aFe.sub.1.0 P.sub.1.84 O.sub.x CATALYSTS HoursExample Molar Feed Ratio Temperature Contact Methacrylic Acid % OnNo. Ratio-Ag (a) 1BA/Air/H.sub.2 O .degree.C. Time (Sec.) WWH % Yield % Selectivity Conversion Stream__________________________________________________________________________14 0.33 1/4.7/24.7 385 1.0 0.23 67.7 75.3 89.9 24.415 0.33 1/4.8/24.7 382 1.0 0.23 69.0 70.2 98.3 52.516 0.33 1/4.8/24.7 378 1.0 0.23 66.8 69.2 96.6 73.617 0.66 1/4.9/25.3 406 0.9 0.27 71.9 71.9 100 24.618 0.66 1/4.4/25.3 382 1.0 0.27 74.3 76.1 97.5 50.919 0.70 1/4.5/25.3 387 1.0 0.18 73.8 76.1 96.9 45.920 0.75 1/4.8/24.7 368 1.0 0.20 74.9 80.8 92.7 2421 0.75 1/5/24.7 388 1.0 0.20 80.0 81.1 98.7 3622 0.75 1/5.5/25.6 391 0.9 0.20 80.2 82.1 97.6 10823 0.75 1/5/17.3 407 1.2 0.20 70.6 72.9 96.8 19824 0.75 1/5/30.5 390 0.8 0.20 75.1 76.8 97.8 24325 0.8 1/4.5/24.7 388 1.0 0.19 78.4 79.6 98.5 46.526 0.8 1/3.6/24.7 395 1.0 0.19 80.4 82.2 97.8 8327 0.8 1/4.7/24.7 406 1.0 0.19 73.1 73.1 100 15628 0.8 1/4.8/24.7 383 1.0 0.19 73.1 75.1 97.3 24429 0.8 1/4.8/17.5 390 1.3 0.19 70.9 74.4 95.3 25030 0.85 1/5.5/24.7 368 1.0 0.18 73.6 76.7 95.9 54.531 0.85 1/4.8/24.7 368 1.0 0.18 81.4 84.5 96.3 8432 0.85 1/4.5/24.7 370 1.1 0.18 77.6 80.7 96.2 127 33* 0.8 1/5/26.2 376 0.9 0.26 74.7 76.3 99.2 24 34* 0.8 1/4.1/26.2 373 0.9 0.26 76.3 78.4 97.3 48.5 35* 0.8 1/3.6/32.9 376 0.8 0.26 79.9 81.9 97.6 59.536 1.0 1/4.7/24.7 386 1.0 0.22 73.7 76.1 96.9 26.537 1.0 1/4.7/24.7 389 1.0 0.22 71.0 78.2 90.8 5238 1.0 1/4.8/24.7 360 1.1 0.14 70.4 72.7 97.0 2439 1.5 1/5/24.7 366 1.0 0.13 69.4 71.2 97.4 25.8__________________________________________________________________________ *Molar ratio Fe = 1.2 TABLE III__________________________________________________________________________OXYDEHYDROGENATION OF ISOBUTYRIC ACID TO METHACRYLIC ACID OVER Cu.sub.aFe.sub.1.0 P.sub.1.84 O.sub.x CATALYSTS HoursExample Molar Feed Ratio Temperature Contact Methacrylic Acid % OnNo. Ratio-Cu (a) IBA/Air/H.sub.2 O .degree.C. Time (Sec.) WWH % Yield % Selectivity Conversion Stream__________________________________________________________________________40 0.2 1/4.8/24.7 405 1.0 0.27 68.1 72.1 94.4 2441 0.2 1/4.8/24.7 387 1.0 0.27 70.0 72.1 97.1 4642 0.33 1/4.8/24.7 396 1.0 0.28 66.2 66.3 99.9 2743 0.33 1/4.9/24.7 386 1.0 0.28 67.1 71.2 94.3 72 44* 0.33 1/4.3/22.0 374 1.7 0.32 65.7 69.9 94.0 10745 0.66 1/4.8/24.7 368 1.0 0.26 70.9 72.9 97.3 2546 0.66 1/4.8/24.7 368 1.0 0.26 71.4 74.0 96.6 49 47* 0.66 1/4.8/13.0 410 0.9 0.77 61.9 67.0 92.4 60 48* 0.66 1/4.2/22.6 386 0.9 0.52 68.1 72.6 93.8 67 49* 0.66 1/4.7/12.9 430 0.9 0.77 63.1 68.1 92.8 7650 1.0 1/4.9/24.7 429 0.9 0.27 49.5 55.9 88.5 24__________________________________________________________________________ *Run at reactor outlet pressure 12 PSIG. TABLE IV__________________________________________________________________________OXYDEHYDROGENATION OF ISOBUTYRIC ACID TO METHACRYLIC ACID OVERTh.sub.0.2 Fe.sub.1.0 P.sub.1.84 O.sub.x CATALYSTSExample Feed Ratio Temperature Contact Methacrylic Acid %No. IBA/Air/H.sub.2 O .degree.C. Time (Sec.) WWH % Yield % Selectivity Conversion Hours On__________________________________________________________________________ Stream51 1/5/11 400 1.7 0.34 71.0 71.2 99.8 3952 1/5/11 398 1.7 0.34 67.5 70.6 95.6 6853 1/5/11 402 1.7 0.34 60.5 65.4 92.5 13654 1/5/15 402 1.4 0.34 66.9 69.0 96.9 20355 1/4/20 413 1.1 0.34 66.7 72.9 91.5 33056 1/4/26 423 0.9 0.34 65.7 71.2 92.2 40157 1/5.5/26 412 0.9 0.34 63.3 67.1 94.3 49958 1/5/24 397 1.0 0.34 61.0 70.9 86.0 61659 1/5/24 406 1.0 0.34 65.3 68.9 94.7 80960 1/5/25 426 1.4 0.22 57.9 66.4 87.2 97961 1/5/25 407 0.9 0.34 70.2 71.6 98.1 1,04562 1/5/25 402 1.0 0.34 68.8 69.4 99.1 1,074__________________________________________________________________________ TABLE V__________________________________________________________________________OXYDEHYDROGENATION OF ISOBUTYRIC ACID TO METHACRYLIC ACID OVER A.sub.aFe.sub.1.0 P.sub.1.84 O.sub.x CATALYSTS Promoter & HoursExample Mole Ratio Feed Ratio Temperature Contact Methacrylic Acid % OnNo. (Aa) IBA/Air/H.sub.2 O .degree.C. Time (Sec.) WWH % Yield % Selectivity Conversion Stream__________________________________________________________________________63 Ce.sub.0.2 1/5/31 391 1.8 0.18 53.8 57.0 94.3 864 Ce.sub.0.2 1/8/50 390 1.8 0.11 58.7 59.7 98.3 1665 Co.sub.0.33 1/4.8/24.7 428 0.9 0.28 61.0 65.1 93.8 1966 Co.sub.0.33 1/4.8/24.7 446 0.9 0.28 61.9 64.0 96.6 5567 Co.sub.0.33 1/3.9/26.1 432 0.9 0.29 70.9 74.0 95.9 2468 Co.sub.0.33 1/3.9/26.1 442 0.9 0.29 69.2 73.5 94.2 5069 Cr.sub.0.22 1/4.8/24.7 425 0.9 0.36 55.6 60.5 92.0 5070 Cr.sub.0.22 1/4.8/24.7 425 0.9 0.36 49.1 63.7 91.5 7071 Cr.sub.0.22 1/4.6/26.1 432 0.9 0.36 65.3 68.3 95.5 2372 Cr.sub.0.22 1/5/26.1 423 0.9 0.36 67.0 67.8 98.8 3673 Dy.sub.0.22 1/5/25 411 1.0 0.23 65.8 66.7 98.7 4774 Dy.sub.0.22 1/5/25 417 0.9 0.23 65.6 68.5 95.7 7475 Eu.sub.0.22 1/5/25 407 0.9 0.28 63.5 65.8 96.5 2476 Eu.sub.0.22 1/5/25 407 0.9 0.28 62.3 65.7 94.9 4177 Eu.sub.0.22 1/4.6/26.1 396 0.9 0.29 68.1 72.5 93.9 3178 Ge.sub.0.2 1/4/26 412 1.7 0.22 48.5 52.6 92.379 Ge.sub.0.2 1/4/25 418 1.7 0.22 54.8 57.3 95.780 Ho.sub.0.22 1/4.8/24.7 412 0.9 0.26 58.4 61.7 94.6 4081 Ho.sub.0.22 1/4.8/24.7 414 0.9 0.26 54.1 63.6 85.1 5782 Ho.sub.0.22 1/5/26.1 434 0.9 0.27 63.4 64.2 98.7 2483 Ho.sub.0.22 1/4.9/26.1 424 0.9 0.27 67.3 69.0 97.6 5484 La.sub.0.22 1/5.4/24.7 424 0.9 0.3 63.5 66.0 96.2 2685 La.sub.0.22 1/5.4/24.7 425 0.9 0.3 64.2 66.4 96.7 3086 Lu.sub.0.22 1/4.8/24.7 424 0.9 0.30 59.2 62.5 94.8 2787 Lu.sub.0.22 1/4.8/24.7 434 0.9 0.30 53.7 63.0 85.3 5088 Nd.sub.0.22 1/4/23 396 1.7 0.17 60.3 62.9 95.8 789 Nd.sub.0.22 1/4/24 402 1.7 0.17 65.4 70.3 93.1 3090 Ni.sub.0.33 1/4.8/24.7 432 0.9 0.33 57.2 60.7 94.2 2591 Ni.sub.0.33 1/4.8/26.1 428 0.9 0.32 64.7 64.8 99.8 2592 Ni.sub.0.33 1/4.8/26.1 418 0.9 0.32 69.1 69.7 99.2 5093 Ni.sub.0.33 1/3.7/26.1 413 0.9 0.32 73.2 75.1 97.5 7194 Sm.sub.0.22 1/4.4/25.3 425 0.9 0.27 66.7 67.6 98.7 2595 Sm.sub.0.22 1/4.8/25.3 432 0.9 0.27 66.2 69.0 96.0 4996 Ti.sub.0.2 1/4/22 409 1.6 0.26 63.1 66.7 94.6 697 Ti.sub.0.2 1/4/28 413 1.3 0.26 58.2 62.2 93.6 12.sup. 98.sup.b Th.sub.0.2 1/4.1/25.3 410 1.0 0.28 75.1 75.8 99.0 23.sup. 99.sup.b Th.sub.0.2 1/3.7/25.3 410 1.0 0.28 76.3 77.4 98.6 48.sup. 100.sup.c Th.sub.0.2 1/4.8/25.3 417 0.9 0.34 71.6 72.6 98.6 23.sup. 101.sup.c Th.sub.0.2 1/3.8/25.3 419 1.0 0.34 73.6 74.8 98.4 35.sup. 102.sup.d Th.sub.0.2 1/4.8/25.3 392 1.0 0.25 68.8 68.9 99.9 24.sup. 103.sup.d Th.sub.0.2 1/3.5/25.3 382 1.0 0.24 76.2 77.2 98.6 44104 Tm.sub.0.22 1/4.8/24.7 412 0.9 0.27 60.1 65.3 92.0 25105 Tm.sub.0.22 1/4.8/24.7 423 0.9 0.27 56.4 62.7 89.9 46106 U.sub.0.3 1/3.3/24.7 404 1.0 0.21 78.0 80.9 96.4 24107 U.sub.0.2 1/5.4/24.7 418 0.9 0.23 71.1 71.2 99.9 25108 U.sub.0.2 1/4.9/24.7 394 0.9 0.23 74.2 75.0 98.9 48109 U.sub.0.2 1/5.3/24.7 395 0.9 0.23 72.5 73.0 99.2 67110 U.sub.0.2 1/4.7/24.7 382 1.0 0.23 75.0 76.5 98.0 73111 U.sub.0.2 1/4.0/24.7 388 1.0 0.23 76.1 77.7 98.0 99112 V.sub.0.22 1/4.8/25 391 1.0 0.41 50.1 51.1 98.1 25113 V.sub.0.22 1/4.7/25 382 1.0 0.41 49.8 52.2 95.4 45114 Yb.sub.0.22 1/4/23 392 1.7 0.18 64.5 68.4 94.3 6115 Yb.sub.0.22 1/4/23 396 1.7 0.28 61.1 66.3 92.2 15116 Zn.sub.0.33 1/4/25 442 1.6 0.2 58.4 60.3 96.9 10117 Zr.sub.0.2 1/5/23 398 1.7 0.16 65.1 66.7 97.6 5118 Zr.sub.0.2 1/4/22 398 1.7 0.16 65.6 70.0 93.7 7__________________________________________________________________________ .sup.b molar ratio Fe = 1.2 .sup.c Molar ratio Fe = 0.8 .sup.d Molar ratio P = 1.5 TABLE VI__________________________________________________________________________OXYDEHYDROGENATION OF ISOBUTYRIC ACID TO METHACRYLIC ACID OVERAaFe.sub.1.0 P.sub.1.84 DdO.sub.x CATALYSTS Promoter & HoursExample Mole Ratio Feed Ratio Temperature Contact Methacrylic Acid % OnNo. (AaDd) 1BA/Air/H.sub.2 O .degree.C. Time (Sec.) WWH % Yield % Selectivity Conversion Stream__________________________________________________________________________119 Ag.sub.0.4 Mn.sub.0.4 1/4.3/26.1 400 0.9 0.29 75.1 75.4 99.6 19120 Ag.sub.0.4 Mn.sub.0.4 1/4.3/26.1 385 0.9 0.29 74.7 76.4 97.8 24121 Ag.sub.0.4 Mn.sub.0.4 1/4.1/36.8 385 0.7 0.29 74.1 77.8 95.3 44122 Ag.sub.0.5 U.sub.0.3 1/4.5/25.3 387 1.0 0.18 74.6 75.9 98.3 20123 Ag.sub.0.5 U.sub.0.3 1/4.5/25.3 377 1.0 0.18 73.7 76.9 95.8 23124 Ag.sub.0.5 U.sub.0.3 1/4.5/25.3 382 1.0 0.18 74.2 75.8 97.9 43__________________________________________________________________________ TABLE VII__________________________________________________________________________OXYDEHYDROGENATION OF ISOBUTYRIC ACID TO METHACRYLIC ACID OVERAg.sub.0.8 Fe.sub.1.0 P.sub.1.84 O.sub.x WITH SILICA DILUENTS Weight HoursExample Percent Feed Ratio Temperature Contact Methacrylic Acid % OnNo. Diluent IBA/Air/H.sub.2 O .degree.C. Time (Sec.) WWH % Yield % Selectivity Conversion Stream__________________________________________________________________________125 20 1/4.8/26.1 415 0.9 0.16 75.0 76.1 98.6 26126 20 1/4.2/26.1 419 0.9 0.16 74.5 76.3 97.6 39127 20 1/4.0/25.3 388 1.0 0.23 77.0 79.1 97.3 49128 30 1/4.4/25.3 380 1.0 0.23 72.6 73.4 98.8 25129 30 1/3.8/25.3 375 1.0 0.23 73.5 75.8 96.9 53130 40 1/4.5/25.3 382 1.0 0.25 73.5 76.0 96.7 25131 40 1/3.9/25.3 394 1.0 0.25 75.1 76.6 98.1 49132 50 1/4.6/25.3 397 0.9 0.26 70.4 71.8 98.5 24__________________________________________________________________________ TABLE VIII__________________________________________________________________________OXYDEHYDROGENATION OF ISOBUTYRIC ACID TO METHACRYLIC ACID OVER COATEDCATALYSTS HoursExample Weight % Feed Ratio Temperature Contact Methacrylic Acid % OnNo. Active IBA/Air/H.sub.2 O .degree.C. Time (Sec.) WWH % Yield % Selectivity Conversion Stream__________________________________________________________________________Ag.sub.0.8 Fe.sub.1.0 P.sub.1.84 O.sub.x on 10-30 mesh alundum133 16.4 1/4.1/24.7 445 0.9 0.18 76.0 77.2 98.4 23134 16.4 1/3.8/36.8 434 0.7 0.18 69.2 75.3 91.9 31135 30 1/3.9/26.1 427 0.9 0.15 78.2 82.6 94.7 24136 30 1/4/26.1 432 0.9 0.15 79.0 81.7 96.7 36Mn.sub.0.5 Fe.sub.1.0 P.sub.1.84 O.sub.x on 1/8 inch alundum137 35 1/5/25.9 409 0.9 0.21 69.5 72.2 96.2 23138 35 1/4.7/25.3 421 0.9 0.21 66.8 67.7 98.7 48139 45 1/4.8/26.1 414 0.9 0.22 64.9 66.2 98.0 26140 45 1/4.2/36 430 0.7 0.22 66.6 67.4 98.9 34__________________________________________________________________________ TABLE IX__________________________________________________________________________OXYDEHYDROGENATION OF ISOBUTYRIC ACID TO METHACRYLIC ACIDOVER 17 WEIGHT PERCENT COATED A.sub.a Fe.sub.1.0 P.sub.1.8 O.sub.x ONALUNDUM PROMOTER AND METHACRYLIC ACIDEXAMPLE NO. MOLE RATIO % YIELD % SELECTIVITY % CONVERSION__________________________________________________________________________141 Ag.sub.0.6 55.1 55.1 100142 Cd.sub.0.3 50.4 50.5 99.8143 Ce.sub.0.2 51.3 51.3 100144 Dy.sub.0.2 54.7 55.0 99.5145 La.sub.0.2 55.6 55.6 100146 Mn.sub.0.3 46.1 55.5 83147 Ni.sub.0.3 44.9 44.9 100148 Ti.sub.0.15 63.7 64.1 99.3149 U.sub.0.15 40.6 40.8 99.6150 Zr.sub.0.15 48.5 48.5 100__________________________________________________________________________

Claims

1. A catalyst composition represented by the formula

A.sub.a Fe.sub.b P.sub.c O.sub.x

wherein

A is selected from the group Cd, Cr, Ge, Th, Ti, U, Zr, rare earths and mixtures thereof; and

wherein

a is greater than zero but less than or equal to 1.0

b=0.75-1.5

c=1.0-2.0, and

x is the number of oxygens needed to satisfy the valence requirements of the remaining elements.

2. A catalyst as in claim 1 wherein said rare earths are selected from the group La, Ce, Nd, Sm, Eu, Dy, Ho, Tm, Yb and Lu.

3. A catalyst as in claim 1 wherein a is about 0.15 to about 0.5.

4. A catalyst as in claim 1 wherein said catalyst contains thorium.

5. A catalyst as in claim 1 wherein said catalyst contains uranium.

6. A catalyst as in claim 1 wherein said catalyst additionally contains inert diluents.

7. A catalyst as in claim 1 wherein said catalyst is coated upon a support.

8. A catalyst as in claim 1 wherein said catalyst contains at least one rare earth element.

9. A catalyst composition represented by the formula

A.sub.a Fe.sub.b P.sub.c Ag.sub.d Mn.sub.d O.sub.x

wherein

A is selected from the group Cd, Cr, Ge, Te, Th, Ti, U, Zr, rare earths and mixtures thereof; and

wherein

a=0-1.0

b=0.75-1.5

c=1.0-2.0

d is greater than zero and the total amount of Ag and Mn ranges from about 0.2 to 2.0, and

x is the numeral of oxygens needed to satisfy the valence requirements of the remaining elements.

10. A catalyst as in claim 9 wherein said catalyst is Fe.sub.1.0 P.sub.1.84 Ag.sub.0.4 Mn.sub.0.4 O.sub.x.

11. A catalyst composition represented by the formula

A.sub.a Fe.sub.b P.sub.c Mn.sub.d O.sub.x

wherein

A is selected from the group Cd, Cr, Ge, Te, Th, Ti, U, Zr, rare earths and mixtures thereof; and

wherein

a=0.15-1.0

b=0.75-1.5

c=1.0-2.0

d=0.2-2.0, and

x is the number of oxygens needed to satisfy the valence requirements of the remaining elements.

12. A catalyst composition as in claim 11 wherein said A element is Te.