Process for preparing unsaturated carboxylic acids

Abstract

A process for the preparation of an unsaturated carboxylic acid which comprises reacting an unsaturated aldehyde with molecular oxygen in the vapor phase in the presence of an oxidation catalyst composition having the following empirical formulaMo.sub.a P.sub.b Cr.sub.c Q.sub.d L.sub.e O.sub.fwherein Q is at least one element selected from the group consisting of Tl, Rb, Cs and K; L is at least one element selected from the group consisting of Sr, Zn, Cd, V, Nb, B, Pb, Bi and W; and a, b, c, d, e and f each represent the number of atoms of each element; the atomic ratio of a:b:c:d:e is 12:0.1-8:0.1-8:0.1-8:0.01-6; and f is the number of oxygen atoms determined by the valence requirement of the other elements present.

Description

This invention relates to a process for preparing unsaturated carboxylic acids by the vapor phase oxidation of unsaturated aldehydes using a specific catalyst which can give the unsaturated carboxylic acids in high selectivity and yield and has a long active lifetime.

Prior patents and literature relating to the vapor phase catalytic oxidation of unsaturated aldehydes are directed chiefly to the production of acrylic acid from acrolein, and very few relate to the production of methacrylic acid from methacrolein. Actually, many of the catalysts which give good results in the oxidation of acrolein exhibit low activity (low conversion) when applied to the oxidation of methacrolein. If the reaction is carried out at an elevated temperature in order to increase the conversion of methacrolein, side-reactions such as a complete oxidation reaction (the formation of CO and CO.sub.2) occur to reduce the yield (per pass) and selectivity of methacrylic acid. On the other hand, the catalysts so far suggested for the oxidation of methacrolein are commercially unsuitable and not entirely satisfactory for one or combinations of the following reasons, such as low activity, short active lifetime and low productivity (space time yield for methacrylic acid) because of the necessity to prolong the reaction time or to reduce the methacrolein concentration in the feed gas.

Under such circumstances, it has been considered very difficult to produce methacrylic acid commercially by the oxidation of methacrolein, in spite of the fact that the production of acrylic acid from acrolein has been carried out commercially. Accordingly, the development of catalysts useful for oxidation of methacrolein should be studied from a different point of view from the catalysts for the oxidation of acrolein.

U.S. Pat. No. 3,795,703 discloses a Mo--P--Cr--Q catalyst (Q being at least one member selected from the group consisting of Tl, Rb, Cs and K) for the oxidation of methacrolein with a view to removing such drawbacks mentioned above. According to this U.S. patent specification, the catalyst is usable also as an oxidation catalyst for acrolein,, and gives relatively good results in the oxidation reaction and has a long active life time. It is naturally desirable in commercial operations, however, to improve the performance of the above catalyst further in order to gain better reaction results in, for example, the yield per pass, the selectivity of unsaturated carboxylic acids, and the space time yield for unsaturated carboxylic acids.

Accordingly, the object of this invention is to improve the aforesaid conventional Mo--P--Cr--Q catalyst, and specifically, to improve the conventional catalyst without impairing its feature of a long active lifetime so that the yield and selectivity of unsaturated carboxylic acids and the productivity (space time yield) of these acids can be increased. This object can be attained by using a catalyst comprising the constituents of the conventional Mo--P--Cr--Q catalyst and, in addition, at least one element selected from the group consisting of Sr, Zn, Cd, V, Nb, B, Pb, Bi and W.

More specifically, an oxidation catalyst composition of the present invention comprises a catalytic oxide of molybdenum, phosphorus, chromium, at least one element selected from the group consisting of thallium, rubidium, cesium and potassium, and at least one element selected from the group consisting of strontium, zinc, cadmium, vanadium, niobium, boron, lead, bismuth, and tungsten, the catalyst composition having the following empirical formula

Mo.sub.a P.sub.b Cr.sub.c Q.sub.d L.sub.e O.sub.f wherein Q is at least one element selected from the group consisting of Tl, Rb, Cs and K; L is at least one element selected from the group consisting of Sr, Zn, Cd, V, Nb, B, Pb, Bi and W; and a, b, c, d, e and f each represent the number of atoms of each element; the preferred atomic ratio of a:b:c:d:e is in the range of about 12:0.1-8:0.1-8:0.1- 8:0.01-6; and f is the number of oxygen atoms determined by the valence requirements of the other elements present; a more preferred atomic ratio of a:b:c:d:e is in the range of about 12:0.3-5:0.3-5:0.3-5:0.05-3.

As described above, the difference between the catalyst of this invention and the conventional catalyst is that the former contains an L component, that is, at least one element selected from the group consisting of Sr, Zn, Cd, V, Nb, B, Pb, Bi and W. This difference in catalyst composition gives rise to a remarkable improvement in the performance of the catalyst of this invention.

The catalysts according to the present invention can be used as an oxidation catalyst to produce unsaturated carboxylic acids in higher yields and selectivities than conventional catalysts used in the stable oxidation reaction of unsaturated aldehydes under feasible reaction conditions. Furthermore, the catalyst life can be maintained at a high level for prolonged periods of time, and the reaction can be performed continuously over an extended period of time.

The catalyst may be made, for example, by the oxide mixing method, the evaporative drying method or the coprecipitation method, all of which are well known in the art. The starting constituent elements of the catalyst do not always have to be in the form of an oxide but may be in the form of a metal, metal salt, acid or base so long as they can be converted to the corresponding metal oxides by calcination. Typical examples include salts such as ammonium salts, nitrate or halides; free acids such as molybdic acid or phosphoric acid; heteropolyacids containing molybdenum, such as phosphomolybdic acid, and heteropolyacid salts such as ammonium salt of the phosphomolybdic acid. Prior to use, the catalyst composition is preferably calcined for several hours up to 15 or 16 hours at about 250.degree.-700.degree. C., preferably about 350.degree.-600.degree. C., in air, a reducing atmosphere or feed gas.

The catalyst can be prepared, for example, by mixing an aqueous solution containing a water-soluble compound of the Q element with an aqueous solution containing ammonium molybdate and ammonium chromate, adding an aqueous solution containing phosphoric acid and an aqueous solution containing a nitrate of the L element such as strontium nitrate, evaporatively drying the mixture while stirring, calcining the solid obtained, pulverizing the calcined product, and then, if necessary, molding it into pellets.

Other examples of the catalyst preparation are described for example, in the working examples to be given later. Preferably, the catalyst is prepared by mixing the starting compounds so that the constituent elements will form complex compounds such as heteropolyacids, their acid salts or ammonium salts, calcining the obtained complex compounds, pulverizing the calcined product and then, if necessary, molding it into pellets.

Those skilled in the art can select the desired method of preparing the catalyst. It is not yet clear however, in what state the individual elements of the catalyst composition, including oxygen, are during the reaction when the catalyst is exhibiting its catalytic action.

While the catalyst can be used in the molded or powdered form, it is also possible to use it after dilution with an inert diluent. If desired, the catalyst can be deposited on a suitable inert carrier material. Examples of suitable carriers include alumina, silicon carbide, graphite, inert titania, zirconium oxide, thorium chloride, pumice, silica gel, or celite. The amount of the diluent or carrier is not critical since it has no substantial effect on the activity of the catalyst.

When the catalysts of the present invention are used to prepare an unsaturated carboxylic acid by reacting an unsaturated aldehyde with molecular oxygen at an elevated temperature in the vapor phase, the unsaturated aldehyde may preferably be acrolein or methacrolein. The source of molecular oxygen can be pure oxygen or air. Furthermore, it is possible to introduce into the reaction zone an inert diluent gas such as steam, nitrogen, argon, carbon dioxide, helium or a saturated hydrocarbon, for example, methane, ethane, propane or pentane.

The concentration of the unsaturated aldehyde in the feed gas to be introduced into the reactor is preferably from about 1 to about 25% by volume. On the other hand, the molar ratio of the starting unsaturated aldehyde to molecular oxygen is conveniently about 1:(0.1-25.0), preferably about 1:(0.1-20.0). The reaction temperature is usually in the range of about 300.degree. to 500.degree. C., preferably about 330.degree. to about 450.degree. C., and the reaction pressure can be from a reduced pressure of less than atmospheric pressure to a superatmospheric pressure up to about 15 atms. Preferably, the reaction pressure is about 0.5 to about 10 atmospheres. The contact time (on the basis of 0.degree. C. and 1 atm.) is from about 0.1 to about 20 seconds, preferably about 0.1 to about 15 seconds. The type of reactor with which the catalysts of the present invention is used may be any of those which are conventional, such as the fluidized, moving or fixed bed type. The reaction product can be recovered by known techniques; for example, condensation and liquefaction by means of a condenser on the extraction with water or a suitable solvent.

The invention is illustrated by the following Examples. The conversion of the unsaturated aldehyde, the yield of the unsaturated carboxylic acid and the selectivity therefor are defined below. The analysis was carried out by gas chromatography in all cases. ##EQU1##

The abbreviations used in the tables appearing in the Examples have the following meanings.

Rt = reaction temperature Mal = methacrolein Maa = methacrylic acid conv. = conversion sel. = selectivity

Furthermore, in the following examples the indication of the composition of the catalyst does not specifically refer to the presence of oxygen.

EXAMPLE 1

(i) 212 g of ammonium molybdate and 22.8 g of ammonium chromate were dissolved in 300 ml of water by heating. An aqueous solution of 23 g of 85 wt.% phosphoric acid in 50 ml. of water, an aqueous solution obtained by dissolving 39 g of cesium nitrate (CsNO.sub.3) in 200 ml. of water by heating and an aqueous solution obtained by dissolving 10.55 g of strontium nitrate (Sr(NO.sub.3).sub.2 ) in 200 ml of water were added to the solution prepared above. Then, the entire mixture was evaporated to dryness with stirring. The solid obtained was calcined at 450.degree. C. for 16 hours in a muffle furnace, pulverized and screened to a screen size of 4 to 8 mesh (Tyler No. 4 - No. 8, 4.00 mm - 2.38 mm). The atomic ratio of Mo:P:Cr:Cs:Sr of the resulting catalyst composition (Cat. No. (1)) was 12:2:1.5:2:0.5. Similarly Cat. No. (2) to Cat. No. (9) were prepared using 7.43 g of Zn(NO.sub.3).sub. 2 .multidot.6H.sub.2 O, 7.7 g of Cd(NO.sub.3).sub.2 .multidot.4H.sub.2 O, 11.7 g of NH.sub.4 VO.sub.3, 13.45 g of Nb(HC.sub.2 O.sub.4).sub.5, 3.1 g of H.sub.3 BO.sub.3, 16.55 g of Pb(NO.sub.3).sub.2, 12.13 g of Bi(NO.sub.3).sub.2 .multidot.5H.sub.2 O and 26.1 g of 5(NH.sub.4).sub.2 0.multidot.12WO.sub.3 .multidot.5H.sub.2 O instead of Sr(NO.sub.3).sub.2.

(ii) Cat. No. (10) to Cat. No. (15) were prepared in the same way as mentioned above (i) using 29.5 g of RbNO.sub.3 or 20.2 g of KNO.sub.3 instead of CsNO.sub.3.

(iii) For comparison, Cat. No. (C-1 ) to Cat. No. (C-13) were prepared in the same way as mentioned above (i) and (ii).

A stainless steel reaction tube 2.5 cm in inside diameter and 60 cm in length was packed with 100 ml. of the catalyst, and heated by a molten metal bath. A feed gas having a methacrolein:O.sub.2 :N.sub.2 :H.sub.2 O molar ratio of 1:1.5:17.5:10 was passed through the reaction tube while the contact time was adjusted to 1.8 seconds (on the basic of 0.degree. C., and 1 atm.). The results obtained are shown in Table 1.

The reaction temperatures indicated in the table are the maximum temperatures of the catalyst bed at which the best results were obtained.

The results given in Table 1 demonstrate that the catalysts of the present invention give methacrylic acid in high selectivity and high yield in spite of the short contact time. This also shows that the catalysts of the present invention give excellent space time yields of the unsaturated carboxylic acids.

Table 1______________________________________ MAL MAARun Catalyst Composition RT conv. YieldNo. No. (Atomic Ratio) (.degree. C.) (%) (Sel.) (%)______________________________________(The Present Invention)I-1 (1) Mo.sub.12 P.sub.2 Cr.sub.15 Cs.sub.2 Sr.sub.0.5 418 83.4 64.7 (77.6)2 (2) Mo.sub.12 P.sub.2 Cr.sub.15 Cs.sub.2 Zn.sub.0.25 418 80.8 63.1 (78.7)3 (3) Mo.sub.12 P.sub.2 Cr.sub.15 Cs.sub.2 Cd.sub.0.25 420 83.8 64.0 (76.4)4 (4) Mo.sub.12 P.sub.2 Cr.sub.15 Cs.sub.2 V.sub.0.1 412 79.8 66.2 (83.0)5 (5) Mo.sub.12 P.sub.2 Cr.sub.15 Cs.sub.2 Nb.sub.0.25 415 81.9 65.5 (80.0)6 (6) Mo.sub.12 P.sub.2 Cr.sub.15 Cs.sub.2 B.sub.0.5 420 85.9 64.7 (75.3)7 (7) Mo.sub.12 P.sub.2 Cr.sub.15 Cs.sub.2 Pb.sub.0.5 405 82.4 63.3 (76.8)I-8 (8) Mo.sub.12 P.sub.2 Cr.sub.15 Cs.sub.2 Bi.sub.0.25 427 84.5 62.8 (74.3)9 (9) Mo.sub.12 P.sub.2 Cr.sub.15 Cs.sub.2 W.sub.1 404 84.6 64.5 (76.2)10 (10) Mo.sub.12 P.sub.2 Cr.sub.15 H.sub.2 Sr.sub. 422 72.6 54.0 (74.4)11 (11) Mo.sub.12 P.sub.2 Cr.sub.15 H.sub.2 Zn.sub.0.25 420 73.2 52.5 (71.7)12 (12) Mo.sub.12 P.sub.2 Cr.sub.15 H.sub.2 P.sub.0.5 415 70.6 54.4 (77.1)13 (13) Mo.sub.12 P.sub.2 Cr.sub.15 Rb.sub.2 V.sub.0.1 410 77.7 56.1 (72.2)14 (14) Mo.sub.12 P.sub.2 Cr.sub.15 Rb.sub.2 Nb.sub.0.25 410 75.1 55.5 (73.9)15 (15) Mo.sub.12 P.sub.2 Cr.sub.15 Rb.sub.2 Pb.sub.0.5 407 76.7 54.9 (71.6)(Comparison)16 (C-1) Mo.sub.12 P.sub.2 Cr.sub.15 Cs.sub.2 410 78.1 55.3 (70.8)17 (C-2) Mo.sub.12 P.sub.2 Cr.sub.15 Tl.sub.2 412 78.3 52.0 (66.4)18 (C-3) Mo.sub.12 P.sub.2 Cr.sub.15 K.sub.2 410 67.7 45.7 (67.5)19 (C-4) Mo.sub.12 P.sub.2 Cr.sub.15 Rb.sub.2 415 72.4 47.1 (65.1)20 (C-5) Mo.sub.12 P.sub.2 Cr.sub.15 Sr.sub.0.5 421 58.7 30.3 (51.6)I-21 (C-6) Mo.sub.12 P.sub.2 Cr.sub.15 V.sub.0.1 418 56.7 24.5 (48.3)22 (C-7) Mo.sub.12 P.sub.2 Cr.sub.15 Nb.sub.0.25 417 46.7 22.2 (47.5)23 (C-8) Mo.sub.12 P.sub.2 Cr.sub. 15 Bi.sub.0.25 422 34.4 18.6 (54.1)24 (C-9) Mo.sub.12 P.sub.2 Cs.sub.2 W.sub.1 420 65.9 45.1 (68.4)25 (C-10) Mo.sub.12 P.sub.2 Cs.sub.2 B.sub.0.5 416 63.1 44.3 (70.2)26 (C-11) Mo.sub.12 P.sub.2 Tl.sub.2 Cd.sub.0.25 414 58.5 38.0 (65.0)27 (C-12) Mo.sub.12 P.sub.2 K.sub.2 Zn.sub.0.25 414 44.9 28.6 (63.7)28 (C-13) Mo.sub.12 P.sub.2 Rb.sub.2 Pb.sub.0.5 405 53.4 30.6 (57.3)______________________________________

EXAMPLE 2

The procedure of Example 1 was repeated to prepare catalysts shown in Table 2, and the same reaction as in Example 1 was performed. The results obtained are shown in Table 2.

Table 2______________________________________ MAL MAARun Catalyst Composition RT conv. YieldNo. No. (Atomic Ratio) (.degree. C.) (%) (Sel.) (%)______________________________________II-1 (16) Mo.sub.12 P.sub.2 Cr.sub.15 Cs.sub.2 Sr.sub.1 421 82.4 61.5 (75.0)2 (17) Mo.sub.12 P.sub.2 Cr.sub.2 Cs.sub.2 Sr.sub.0.25 416 79.4 63.2 (79.6)3 (18) Mo.sub.12 P.sub.2 Cr.sub.15 Cs.sub.2 Nb.sub.0.5 409 80.4 62.5 (77.7)4 (19) Mo.sub.12 P.sub.1 Cr.sub.2 Cs.sub.2 Nb.sub.0.1 411 80.3 61.0 (76.0)5 (20) Mo.sub.12 P.sub.2 Cr.sub.2 Cs.sub.15 V.sub.0.1 410 79.8 65.5 (82.1)6 (21) Mo.sub.12 P.sub.2 Cr.sub.2 Cs.sub.2 B.sub.0.5 419 86.0 64.5 (75.0)7 (22) Mo.sub.12 P.sub.1 Cr.sub.1 Cs.sub.2 Bi.sub.0.25 420 82.4 61.3 (74.4)8 (223) Mo.sub.12 P.sub.2 Cr.sub.1 Cs.sub.2 Bi.sub.0.5 423 82.8 62.5 (75.5)9 (24) Mo.sub.12 P.sub.2 Cr.sub.15 K.sub.2 Pb.sub.0.2 408 73.0 53.4 (73.2)10 (25) Mo.sub.12 P.sub.3 Cr.sub.2 K.sub.1 B.sub.3 428 69.5 52.0 (74.8)11 (26) Mo.sub.12 P.sub.3 Cr.sub.15 K.sub.2 V.sub.0.2 425 73.1 53.6 (73.3)12 (27) Mo.sub.12 P.sub.15 Cr.sub.15 Rb.sub.2 Sr.sub.0.25 412 75.6 54.2 (71.7)13 (28) Mo.sub.12 P.sub.2 Cr.sub.15 Rb.sub.2 Nb.sub.0.5 413 73.2 54.2 (74.0)14 (29) Mo.sub.12 P.sub.2 Cr.sub.15 Cs.sub.1 Rb.sub.1 B.sub.0.5 419 84.0 60.6 (72.1)15 (30) Mo.sub.12 P.sub.2 Cr.sub.15 Cs.sub.2 Zn.sub.0.25 415 80.2 64.1 (79.9) V.sub.0.116 (31) Mo.sub.12 P.sub.2 Cr.sub.15 Cs.sub.2 W.sub.0.5 412 85.0 63.5 (74.7) Bi.sub.0.2______________________________________

EXAMPLE 3

Methacrolein was oxidized continuously for prolonged periods of time under the same conditions in Example 1 using each of the catalysts shown in Table 4 which were obtained in Example 1. The performance of each catalyst used after a lapse of 30 days of reaction is shown in Table 3. The temperature of the molten metal bath was kept almost constant during the reaction. In the table, "O" under "time that elapsed" means the initial stage of the reaction. It is seen from Table 3 that the catalysts prepared according to the present invention do not lose their activity even after a lapse of a long period of time, and prove to be excellent catalysts having a very long active lifetime.

Table 3__________________________________________________________________________ Time that MAL MAARun Catalyst Composition elapsed RT conv. YieldNo. No. (Atomic Ratio) (Day) (.degree. C.) (%) (sel.) (%)__________________________________________________________________________III-1 (1) Mo.sub.12 P.sub.2 Cr.sub.1.5 Cs.sub.2 Sr.sub.0.5 0 418 83.4 64.7 (77.6) 30 414 80.8 63.1 (78.1)2 (4) Mo.sub.12 P.sub.2 Cr.sub.1.5 Cs.sub.2 V.sub.0.1 0 412 79.8 66.2 (83.0) 30 411 79.4 67.1 (84.5)3 (6) Mo.sub.12 P.sub.2 Cr.sub.1.5 Cs.sub.2 B.sub.0.5 0 420 85.9 64.7 (75.3) 30 420 86.1 64.5 (74.9)4 (11) Mo.sub.12 P.sub.2 Cr.sub.1.5 K.sub.2 Zn.sub.0.25 0 420 43.2 52.5 (71.7) 30 420 74.3 52.0 (70.0)5 (15) Mo.sub.12 P.sub.2 Cr.sub.1.5 Rb.sub.2 Pb.sub.0.5 0 407 76.7 54.9 (71.6) 30 405 76.5 55.1 (72.0)__________________________________________________________________________

EXAMPLE 4

Acrolein was oxidized under the same conditions as in Example 1 using catalysts No. (4) and No. (6) shown in Table 3 which were obtained in Example 1, while adjusting the composition of the feed gas to acrolein: O.sub.2 :N.sub.2 :H.sub.2 O = 1:2:8:9 (molar ratio).

In the case of using the catalyst No. (4), the conversion of acrolein was 92.5% and the yield of acrylic acid was 85.1% (92.0% of the selectivity therefor) at a reaction temperature of 410.degree. C. In the case of catalyst No. (6), the conversion of acrolein was 95.1%, and the yield of acrylic acid, 85.3% (the selectivity therefor, 89.7%).

Claims

1. A process for the preparation of an unsaturated carboxylic acid selected from the group consisting of acrylic acid and methacrylic acid which comprises reacting an unsaturated aldehyde selected from the group consisting of acrolein and methacrolein with molecular oxygen in the vapor phase in the presence of an oxidation catalyst composition having the following empirical formula

Mo.sub.a P.sub.b Cr.sub.c Q.sub.d L.sub.e O.sub.f

wherein Q is at least one element selected from the group consisting of Rb, Cs and K; L is at least one element selected from the group consisting of Sr, Zn, Cd, V, Nb, B, Pb, Bi and W; and a, b, c, d, e and f each represent the number of atoms of each element; the atomic ratio of a:b:c:d:e is 12:0.1-8:0.1-8:0.1-8:0.01-6; and f is the number of oxygen atoms determined by the valence requirement of the other elements present.

2. The process of claim 1, wherein the unsaturated aldehyde is acrolein.

3. The process of claim 1, wherein the unsaturated aldehyde is methacrolein.

4. The process of claim 1, wherein the reaction temperature is 300.degree. to 500.degree. C.

5. The process of claim 1, wherein the source of molecular oxygen is air.

6. The process of claim 1, wherein an inert diluent gas is introduced into the reaction zone.

7. The process of claim 1, wherein the catalyst is diluted with an inert diluent or supported on an inert carrier.

8. The process of claim 1, wherein the atomic ratio of a:b:c:d:e is 12:0.3-5:0.3-5:0.3-5:0.05-3.

9. The process of claim 8 wherein Q is Cs.

10. The process of claim 1, wherein Q is Rb.

11. The process of claim 1, wherein Q is Cs.

12. The process of claim 1, wherein Q is K.

13. The process of claim 1 wherein L is Sr.

14. The process of claim 1 wherein L is Zn.

15. The process of claim 1 wherein L is Cd.