PROCESS FOR PRODUCING AROMATIC CARBOXYLIC ACIDS AND METHYL ESTERS THEREOF

Abstract: A process for producing an aromatic carboxylic acid or its methyl ester which comprises oxidizing at least one aromatic compound having at least one methyl or formyl group directly bonded to a nuclear carbon atom of the aromatic ring in the liquid phase with molecular oxygen or a gas containing molecular oxygen in the presence of a heavy metal compound as a catalyst in the substantial absence of an aliphatic carbox­ ylic acid as a solvent to form the corresponding aromatic carboxylic acid, and if desired, esterifying the oxidation reac­ tion mixture containing the aromatic carboxylic acid with methanol; said oxidation reaction being carried out in the copresence of 0.1 mole to 10 moles, per mole of said heavy metal compound catalyst, of a lithium compound.

Description: This invention relates to a process for producing aromatic carboxylic acids and methyl esters thereof in high yields. More specifically, this invention pertains to a process for producing an aromatic carboxylic acid or its methyl ester which canprises oxidizing at least one aromatic compound having at least one methyl or formyl group directly bonded to a ring carbon atom of its aromatic ring with molecular oxygen or a gas containing molecular oxygen in the liquid phase in The presence of a heavy metal catalyst, and if desired, esterifying The resulting oxidation reaction product containing the corresponding carboxylic acid with methanol. Suitable aromatic compounds having at least one methyl or formyl group directly bonded to a ring carbon atom of the aromatic ring (to be referred to simply as starting aromatic compounds) are aromatic compounds having a benzene, naphthalene or biphenyl ring, especially the benzene ring. For commercial practice, toluene, p-xylene, p-toluic acid, p-tolualdehyde, methyl p-toluate, a mixture of p-xylene and methyl p-toluate, and a mixture of ptolualdehyde and methyl p-toluate are preferred as the starting aromatic compounds. May methods have previously been knows for producing aromatic carboxylic acids by oxidizing such starting aromatic compounds with molecular oxygen or a gas containing molecular oxygen (e.g., air). Methods have also been known for obtaining methyl esters of aromatic carboxylic acids by esterifying the oxidation reaction product containing the aromatic carboxylic acid with methanol. The present invention is specifically directed to the process Which comprises oxidizing the aforesaid starting aromatic compound in The liquid phase with molecular oxygen or a gas containing molecular oxygen in the presence of a heavy metal catalyst. This process is carried out in the substantial absence of an aliphatic carboxylic acid such as acetic acid without using a halogen or a halogen compound, such as bromine1 hydrogen bromide, ammonium bromide or sodium bromide, as a promotor. This is very advantageous because such halogen or halogen compounds, particularly bromine or bromine compounds, have the property of corroding The oxidation reaction apparatus. Specific examples of such an oxidation process are as follows: (1) Oxidation of toluene disclosed in British Patent No. 1,430,830. (2) Oxidation of p-xylene or p-toluic acid disclosed in British Patent No. 1,234,009, and U. S. Patents Nos. 3,883,584 and 3,873,611. (3) Oxidation of methyl toluate disclosed in British Patent No. 727,989. (4) Oxidation of a mixture of p-xylene and methyl p-toluate disclosed in British Patents Nos. 809,730 and 1,313,083, andU. S. Patent No. 3,890,374. (5) Oxidation of a mixture of p-tolualdehyde and methyl p-toluate disclosed in Japanese Patent Publi- cation No. 23,493/65. All of these processes (1) to (5) can be applied to the production of aromatic carboxylic acids in accordance with this invention. The aromatic carboxylic acids and methyl esters thereof are useful as various raw materials or intermediates. Particularly, benzoic acid is useful as a food additive, and as a raw material for the production of epsilon-caprolactam, phenol, terephthalic acid and dyes. Terephthalic acid and dimethyl terephthalate are very useful industrial compounds for the production of fiberor film-forming polyesters. Accordingly, any process which can afford the aforesaid aromatic carboxylic acids or methyl esters thereof in high yields would be very valuable for commercial industrial purposes. It is knoan that among the aforesaid processes for the aforesaid aromatic carboxylic acids or methyl esters thereof, a method involving the use of an oxidation catalyst comprising a cobalt compound and a manganese cowpound lshich are at least partly soluble in the oxidation. reaction system, and a method involving the use of the aforesaid manganese compound and a nickel compound at least partly soluble in the oxidation reaction system can afford aromatic carboxylic acids or methyl esters thereof in relatively high yields. The details of the process which comprises oxidizing toluene, or a mixture of pxylene and methyl p-toluate with molecular oxygen using a cobalt compound and a manganese compound as an oxidation catalyst are described in British Patents Nos. 1,313,083 and 1,430,830. The details of the process involving oxidizing a mixture of p-xylene and methyl p-toluate with molecular oxygen using a manganese compound and a nickel compound as a catalyst are described in U. S. Patent No. 3,890,374. The processes described in these British and U. S. Patents are also applicable to the process of the present invention. Investigations of the present inventors have shown that aromatic carboxylic acids and oxidation intermediates thereof can be produced in. higher yields by carrying out the oxidation in the co-presence of a suitable lithium compound in the processes which involve oxidizing at least one compound having at least one methyl or formyl group directly bonded to a nuclear carbon atom of the aromatic ring in the liquid phase with molecular oxygen in the presence of a heavy metal compound, particularly a heavy metal compound at least partly soluble in the reaction system, as a catalyst in the substantial absence of an aliphatic carboxylic acid solvent, including the processes described in the aforesaid British or U. S. Patents. The suitable amount of the lithium compound is 0.1 to 10 moles per mole of the heavy metal compound. It is an object of this invention therefore to provide a process for producing the aforesaid aromatic carboxylic acids or methyl esters thereof in higher yields than in the conventional processes for producing the aforesaid aromatic carboxylic acids or methyl esters thereof in the presence of a heavy metal compound as a catalyst. Another object of this invention is to provide a process for producing aromatic carboxylic acids or methyl esters Thereof at higher conversions and selectivities by carrying out the oxidation reaction at higher temperatures than in the conventional process for producing aromatic carboxylic acids or methyl esters thereof using a heavy metal compound as a catalyst. Still another object of this invention is to provide a process for producing aromatic carboxylic acids or methyl esters thereof, in which the individual parts of a reaction apparatus including a heat exchanger or esterification tower are not clogged by the deposition of the heavy metal compound catalyst even when the concentration of the heavy metal compound in the oxidation reaction system is increased. Further objects and advantages of this invention will become apparent from the following description. The above objects and advantages of this invention are achieved by fl process for producing aromatic carboxylic acids or methyl esters thereof which comprises oxidizing at least one aromatic compound having at least one methyl or formyl group directly bonded to a nuclear carbon atom of the aromatic ring in the liquid phase with molecular oxygen or a gas containing molecular oxygen in the presence of a heavy metal catalyst in the substantial absence of an aliphatic carboxylic acid solvent and without substantially using a halogen or halogen compound such as bromine or a bromine compound to form the corresponding aromatic carboxylic acid, and if desired, esterifying the oxidation reaction product containing the aromatic carboxylic acid lfith methanol, said oxidation reaction being carried out in the further presence of 0.1 mole to 10 moles, per mole of the heavy metal catalyst, of a lithium compound. The lithium compound used in this invention is believed to act on the oxidation reaction as a co-catalyst. The lithium compound used in this invention may be any lithium compound which is at least partly soluble in the oxidation reaction system of this invention, or any lithium compound which is insoluble but when added to the reaction system of this invention, reacts with a compound present in the reaction system such as carboxylic acids to be converted to a soluble lithium compound. Examples of suitable lithium compounds for use in the process of this invention are listed below. (i) Organic carboxylic acid salts (a) Salts of aliphatic carboxylic acids having 1 to 20 carbon atoms such as formic acid, acetic acid, prop ionic acid, butyric acid, palmitic acid, oleic acid, stearic acid and adipic acid, (b) salts of aromatic carboxylic acids having 7 to 20 carbon atoms such as benzoic acid, toluic acid, isophthalic acid, terephthalic acid, and monomethyl terephthalate, and salts of alicyclic carboxylic acids having 5 to 20 carbon atoms such as naphthenic acid, cyclohexane-monocarboxylic acid and methylcyclohexane-monocarboxylic acid. (ii) Complex salts Acetylacetonate complex salts, methylacetoacetate complex salts, and ethylacetoacetate complex salts. (iii) Inorganic compounds Lithium hydroxide, lithium oxide and lithium carbonate. These lithium compounds are merely exemplary1 and the invention is in no lay limited to them. Other lithium compounds can be used if they are at least partly soluble in the oxidation reaction system and are convertible to soluble compounds when added to the oxidation reaction system. Metallic lithium can equally be used because it is converted-to a soluble compound in the oxidation reaction system. The lithium compound should be used in an amount of 0.1 mole to 10 moles per mole of the heavy metal compound used as the oxidation reaction catalyst. If the amount of the lithium compound is less than 0.1 mole, the effect of its use is not appreciable. On the other hand, when it is used in an amount exceeding 10 moles1 the yield of the final product is rather lower than in the case of using only the heavy metal compound catalyst. Advantageously, the amount of the lithium compound is 0.2 to 5 moles, especially 0.3 to 3 moles, per mole of the heavy metal compound catalyst. Examples of the heavy metal compound used as a catalyst in This invention are soluble compounds of metals having variable valences such as cobalt, manganese, nickel and chromium. Among them, a catalyst comprising a cobalt compound, a catalyst comprising a cobalt compound and a manganese compound, and a catalyst comprising a manganese compound and a nickel compound are especially preferred for the practice of the process of this invention. It is especially advantageous to carry out the process of this invention in the presence of the catalyst composed of a cobalt compound and a manganese compound in combination with the lithium compound. These cobalt, manganese or nickel compounds may be any cobalt, manganese or nickel compounds Which are at least partly soluble in the oxidation reaction system of this invention, or are converted to compounds at least partly soluble in the reaction system, as de scribed hereinabove with regard to the lithium compound. Organic acid salts, complex salts and inorganic compound salts of these metals corresponding to those described with regard to the lithium compound can be used. Suit able compounds are salts of cobalt, manganese or nickel with aliphatic carboxylic acids having 1 to 20 carbon atoms, especially 10l7er aliphatic carboxylic acids such as acetic acid and aromatic carboxylic acids having a benzene ring such as benzoic acid, toluic acid and tere rphthalic acid. These heavy metal compound catalysts can be lusted in concentrations and proportions usually knolm in the art. For example, in the case of using a cobalt compound catalyst or a catalyst comprising a cobalt compound and a manganese compound; the-cobalt compound is desirably used in an amount of 100 to 600 ppm, preferably 200 to 500 ppm, calculated as cobalt metal in the reaction mix ture. It is especially preferred in the case of the catalyst comprising a cobalt and a manganese compound which is especially preferred in the present invention that the cobalt compound bemused in the concentration within the above-specified ranges as cobalt metal in the reaction mixture, and the atomic ratio of cobalt metal to manganese metal be adjusted to 100:1 to 100:25. Preferred aromatic compounds as starting mater ials in the process of this invention are toluene, p xylene, p-toluic acid, p-tolualdehyde, methyl p-toluate, a mixture of p-xylene and methyl p-toluate, and a mixture of p-tolualdehyde and methyl p-toluate. A mixture of p-xylene and methyl p-toluate and a mixture of p-tolu aldehyde and methyl p-toluate are especially preferred in the performance of the process of this invention. The processes using these aromatic compounds are generally called the Witten-Hercules process, and its details are described, for example, in British Patent No. 1,313,083, and Japanese Patent Publication No. 23,493/1965. The suitable lfeight ratio of p-xylene or ptolualdehyde to methyl p-toluate in the starting mixture is from 1:4 to 4:1. It is especially advantageous in this invention to perform the process in the presence of a combination of the catalyst comprising a cobalt and a manganese compound in combination with the lithium compound using a mixture of p-xylene and methyl p-toluate as a starting material. The reaction temperature used to perform the process of this invention is in the range of 140 to 2200C which is generally used in knows conventional methods. The preferred temperature range is from 160 to 22000 C when the heavy metal compound catalyst comprises a combination of a cobalt and a manganese compound, and 170 to 2200C len it comprises a combination of a manganese and a nickel compound. In particular, lhen a mixture of p-xylene and methyl p-toluate is to be oxidized in the presence of the catalyst comprising a cobalt and a manganese compound, it is advantageous to employ an oxidation temperature of 160 to 2000C, above all 160 to f900C. By performing this reaction in the copresence of the lithium compound in accordance with this invention, it is possible to produce monomethyl terephthalate and p-toluic acid and useful oxidation intermediates convertible to these compounds in higher yields than in the case of performing the reaction without the lithium compound. In particular, when the reaction of this invention is carried out at 160 to 190 C, monomethyl terephthalate, p-toluic acid and useful oxidation intermediates convertible to these compounds can be produced with higher conversions and selectivities of p-xylene and methyl p-toluate than in the case of performing the reaction in the presence of a catalyst composed of a cobalt and a manganese compound in the absence of the lithium compound. The gas containing molecular oxygen used in the oxidation reaction of this invention may be a gaseous mixture of oxygen and an inert gas such as nitrogen, helium, argon and carbon dioxide. For example, an oxygencontaining gas diluted with an inert gas is used. Air is most readily available and economical. The reaction pressure used in the reaction of this invention is atmospheric pressure to 250 kg/cmê as 2 the total pressure, and 0.2 to 50 kg/cm as the partial pressure of oxygen. When the partial pressure of oxygen p is lover than O.Z kg,'cm', the rate of the oxidation re- action is decreased. On the other hand, increasing of the total pressure beyond 250 kg/cm2 is not preferred because the cost of the apparatus increases enormously. The preferred partial pressure of oxygen is 0.4 to 5 kg/cmê The present invention is advantageously applicable to the Witten-Hercules process which comprises the oxidation of a mixture of p-xylene and methyl p-toluate in the presence of a catalyst comprising a cobalt and a manganese compound. In the Witten-Hercules process, the mixture of p-xylene and methyl p-toluate is oxidized with air in the liquid phase in the presence of a catalyst comprising a cobalt and manganese. Then, generally without separating the metal catalyst used in the oxidation reaction, the oxidation reaction mixture is esterified with methanol. Methyl p-toluate and dimethyl terephthalate in the esterification reaction mixture are separated by distillation, and the dimethyl terephthalate is sent to the subsequent purifying step. In the meantime, the methyl p-toluate is recycled to the oxidation reaction zone and is again subjected to the oxidation reaction together with pxylene. After the separation of methyl p-toluate and dimethyl terephthalate by distillation, the distillation residue contains the catalyst compounds. The catalyst compounds are recycled to the oxidation reaction zone either as such together with the distillation residue, or after they are isolated from The distillation residue by extraction or the like. In this way, the catalyst compounds are recycled. However, depending upon the conditions of the process step, the catalyst compounds recycled gradually deposit in the reaction system and makes it impossible to operate the process stably. This would result in great industrial losses. The present inventors have found that the use of the lithium compound has the advantage of preventing the deposition of the oxidation catalyst. Accordingly, when the process of this invention is applied to the Witten-Hercules process which comprises oxidizing a mixture of p-xylene and methyl p-toluate with air in the liquid phase in the presence of a heavy metal catalyst, and then esterifying the oxidation reaction product with methanol, the desired aromatic carboxylic acid or its methyl ester can be obtained in higher yields than in the case of not using the lithium compound. Moreover, the use of the lithium compounds prevents the deposition of the oxidation catalyst on the apparatus which may occur depending upon the conditions of the process, and the process can be stably operated. Accordingly, this is an especially preferred embodiment of this invention. Even when the lithium compound is used as a cocatalyst in accordance with this invention, the esterification of the oxidation reaction mixture can be performed without any trouble by using the same esterification conditions as in the conventional processes. Furthermore, the lithium compound can be recovered together with the heavy metal compound catalyst, and recycled to the oxidation zone. The process of this invention can of course be applied to the other processes described hereinabove, and similar effects can be achieved. The following examples illustrate the present invention more specifically. It should be understood however that the present invention is not limited to these examples. Examples 1 to 5 and Comparative Examples 1 to 3 A 500 cc stainless steel autoclave equipped with a reflux condenser, a stirrer and a gas blow inlet Gas charged with 80 g of p-xylene (PX), 120 g of methyl p-toluate (MPT), 5- g of p-toluic acid (PTA), cobalt acetate, manganese acetate and lithium acetate. While stirring the mixture at high speed at a temperature of 170 C and a pressure of 5 kg/cm2 *G, air was bloom into the mixture so that the flow rate of the air at the exit was 1200 cc/min. at atmospheric pressure. After the absorption of oxygen began, the reaction was performed for 3 hours. After the reaction, the product was cooled, and withdrawn. The product was analyzed for composition, and the yield of effective products which are intermediates for dimethyl terephthalate (DMT) (i.e., compounds convertible to DMT by oxidation and/or esterification, such as PTA, monomethyl terephthalate ( T), terephthalic acid (TA), pmethylbenzyl alcohol, p-methoxycarbonylbenzyl alcohol, p-tolualdehyde, p-formylbenzoic acid and its methyl ester) was calculated in accordance with the following equation. Yield of Moles of the resulting effective effective products products - Moles of PX and MPT x loo (%) consumed The concentrations of the cobalt acetate and manganese acetate in the starting mixture were adjusted to 400 ppm (1.39 milligram-atom) and 24 ppm (0.09 milligram-atom) respectively as metals, and the amount of lithium acetate was varied as shorn in Table 1 below. For comparison, the above procedure was repeated without adding lithium acetate. The yields of the effective products in these runs are also shorn in Table 1. Table 1 EMI12.1 <tb> Example <SEP> Amount <SEP> of <SEP> lithium <tb> (Ex.) <SEP> or <tb> Comparative <SEP> Li/heavy <SEP> effective <tb> Example <SEP> metal <SEP> products <tb> (CEx.) <SEP> mg-atom <SEP> ppm <SEP> ratio <SEP> (mole%) <tb> CEx. <SEP> 1 <SEP> 0 <SEP> 0 <SEP> 0 <SEP> 85.2 <tb> CEx. <SEP> 2 <SEP> 0.03 <SEP> 1 <SEP> 0.02 <SEP> 85.3 <tb> Ex. <SEP> 1 <SEP> 0.15 <SEP> 5 <SEP> 0.1 <SEP> 87.3 <tb> Ex. <SEP> 2 <SEP> 0.74 <SEP> 25 <SEP> 0.5 <SEP> 90.8 <tb> Ex. <SEP> 3 <SEP> 1.48 <SEP> 50 <SEP> 1 <SEP> 92.0 <tb> Ex. <SEP> 4 <SEP> 2.96 <SEP> 100 <SEP> 2 <SEP> 91.1 <tb> Ex. <SEP> 5 <SEP> 7.40 <SEP> 250 <SEP> 5 <SEP> 88.9 <tb> CEx. <SEP> 3 <SEP> 17.76 <SEP> 600 <SEP> 12 <SEP> 80.6 <tb> Examples 6 to 10 and Comparative Examples 4 and 5 Using the same type of autoclave as used in Examples 1 to 5, experiments were carried out under the same conditions as in Examples 1 to 5 except that the amounts of cobalt acetate, manganese acetate and lithium acetate were changed as indicated in Table 2. The yields of the effective products obtained in these runs are shown in Table 2. Table 3 EMI13.1 <tb> <SEP> Amount <SEP> of <SEP> Concentration <tb> Example <SEP> catalyst <SEP> of <SEP> catalyst <tb> (Ex.) <SEP> or <SEP> (mg/atom) <SEP> in <SEP> the <SEP> start- <SEP> Yield <tb> Compara- <SEP> Li/ <SEP> ing <SEP> mixture <SEP> of <SEP> the <tb> tive <SEP> heavy <SEP> (ppm) <SEP> effective <tb> Example <tb> (CEx.) <SEP> Co <SEP> Mn <SEP> Li <SEP> ratio <SEP> Co <SEP> Mn <SEP> Li <SEP> (%) <tb> Ex. <SEP> 6 <SEP> 0.35 <SEP> 0.02 <SEP> 0.35 <SEP> 0.95 <SEP> 100 <SEP> 6 <SEP> 12 <SEP> 86.7 <tb> Ex. <SEP> 7 <SEP> 0.70 <SEP> 0.04 <SEP> 0.70 <SEP> 0.95 <SEP> 200 <SEP> 12 <SEP> 24 <SEP> 89.0 <SEP> <tb> Ex. <SEP> 8 <SEP> 1.22 <SEP> 0.08 <SEP> 1.22 <SEP> 0.94 <SEP> 350 <SEP> 21 <SEP> 41 <SEP> 93.1 <tb> Ex. <SEP> 9 <SEP> 1.74 <SEP> 0.11 <SEP> 1.74 <SEP> 0.94 <SEP> 500 <SEP> 30 <SEP> 59 <SEP> 91.2 <SEP> <tb> Ex. <SEP> 10 <SEP> 2.43 <SEP> 0.16 <SEP> 2.43 <SEP> 0.94 <SEP> 700 <SEP> 42 <SEP> 82 <SEP> 85.9 <tb> CEx. <SEP> 4 <SEP> 0.35 <SEP> 0.02 <SEP> 0 <SEP> 0 <SEP> 100 <SEP> 6 <SEP> 0 <SEP> 83.4 <tb> CEx. <SEP> 5 <SEP> 2.55 <SEP> 0.16 <SEP> 0 <SEP> 0 <SEP> 700 <SEP> 42 <SEP> 0 <SEP> 82.6 <tb> Exarfples 11 to 14 Using the same type of autoclave as used in Examples 1 to 5, the same procedure as in Examples 1 to 5 was repeated except that the amounts of cobalt acetate and lithium acetate were set at 345 ppm (1.2 mg-atom) and 41 ppm (1.2 mg-atom) respectively as metals, and the amount of manganese acetate was changed as shown in Table 3. The yields of the effective products obtained in these runs are shown in Table 3. Table 3 EMI13.2 <tb> <SEP> Mn/Co <SEP> Yield <SEP> of <SEP> the <tb> <SEP> Concentra- <SEP> gram <SEP> effective <SEP> <tb> <SEP> amount <SEP> of <SEP> Mn <SEP> tion <SEP> of <SEP> Mn <SEP> atomic <SEP> products <tb> Example <SEP> (mg-atom) <SEP> (ppm) <SEP> ratio <SEP> (%) <tb> <SEP> 11 <SEP> 0.024 <SEP> 6 <SEP> 2/100 <SEP> 91.8 <tb> <SEP> 12 <SEP> 0.060 <SEP> 16 <SEP> 5/100 <SEP> 92.7 <tb> <SEP> 13 <SEP> 0.084 <SEP> 23 <SEP> 7/100 <SEP> 93.0 <tb> <SEP> 14 <SEP> 0.120 <SEP> 32 <SEP> 10/100 <SEP> 92.9 <tb> Examples 15 to 21 and Comparative Examples 6 and 7 The same autoclave as used in Examples 1 to 5 was charged with 80 g of PX, 120 g of MPT and 5 g of PTA, and cobalt acetate, manganese acetate and lithium acetate as catalyst in a concentration of 350 ppm, 25 ppm, and 40 ppm, respectively as metals. The same reaction as in Examples 1 to 5 was carried out at each of the reaction temperatures indicated in Table 4. The yields of the effective products are shown in Table 4. For comparison, the above procedure was performed without using lithium acetate (Comparative Examples 6 and 7). The results are also shown in Table 4. Table 4 EMI14.1 <tb> Example <tb> (Ce.) <SEP> or <tb> Comparative <SEP> Reaction <SEP> Reaction <SEP> Yield <SEP> of <SEP> the <tb> Example <SEP> temperature <SEP> time <SEP> effective <SEP> products <tb> (CEx. <SEP> ) <SEP> ( <SEP> C) <SEP> (hr) <SEP> (%) <tb> <SEP> Ex. <SEP> 15 <SEP> 140 <SEP> 3.5 <SEP> 87.5 <tb> <SEP> Ex. <SEP> 16 <SEP> 150 <SEP> 3.5 <SEP> 90.2 <tb> <SEP> Ex. <SEP> 17 <SEP> 160 <SEP> 3.0 <SEP> 92.3 <tb> <SEP> Ex. <SEP> 18 <SEP> 170 <SEP> 3.0 <SEP> 93.4 <tb> <SEP> Ex. <SEP> 19 <SEP> 180 <SEP> 2.5 <SEP> 93.2 <tb> <SEP> Ex. <SEP> 20 <SEP> 190 <SEP> 2.5 <SEP> 92.9 <SEP> <tb> <SEP> Ex. <SEP> 21 <SEP> 200 <SEP> 2.0 <SEP> 92.7 <tb> <SEP> CEx. <SEP> 6 <SEP> 180 <SEP> 2.5 <SEP> 85.4 <SEP> <tb> <SEP> CEx. <SEP> 7 <SEP> 200 <SEP> 2.0 <SEP> 81.0 <tb> Examples 22 to to 26 and Comparative Examples 8 to 10 The same autoclave as in Examples 1 to 5 was charged with 70 g of P::, 130 g of MPT, 5 g of PTA and manganese acetate, nickel acetate and lithium acetate. While stirring the mixture at a pressure of 7 kg/cm2.G and a temperature of 1900C, air e*Tas blown into it so that the flow rate of the air at the exit became 1500 cc/min. After the absorption of oxygen began1 the reaction was performed for 3 hours. After the reaction, the reaction mixture was treated in the same way as in Examples 1 to 5, and the yield of the effective products was determined. In the above experiment, the concentrations of manganese acetate and nickel acetate in the starting mixture were set at 200 ppm (0.746 mg-atom) and 200 ppm (0.698 mg-atom), respectively, as metal, and the amount of lithium acetate was changed as shown in Table 5. For comparison, the above experiment ,ras performed without using lithium acetate. The results are also shown in Table 5. Table 5 EMI15.1 <tb> Example <SEP> Amount <SEP> of <SEP> lithium <tb> (Ex.) <SEP> or <tb> <SEP> Comparative <SEP> Li/heavy <SEP> effective <tb> Example <SEP> metal <SEP> products <tb> <SEP> (CEx.) <SEP> mg-atom <SEP> ppm <SEP> ratio <SEP> (mole%) <tb> <SEP> CEx. <SEP> 8 <SEP> 0 <SEP> 0 <SEP> 0 <SEP> 84.8 <tb> <SEP> CEx. <SEP> 9 <SEP> 0.03 <SEP> 1 <SEP> 0.02 <SEP> 85.0 <tb> <SEP> Ex. <SEP> 22 <SEP> 0.14 <SEP> 5 <SEP> 0.1 <SEP> 87.4 <tb> <SEP> Ex. <SEP> 23 <SEP> 0.72 <SEP> 24 <SEP> 0.5 <SEP> 90.1 <tb> <SEP> Ex. <SEP> 24 <SEP> 1.44 <SEP> 49 <SEP> 1 <SEP> 91.5 <tb> <SEP> Ex. <SEP> 25 <SEP> 2.89 <SEP> 98 <SEP> 2 <SEP> 91.4 <tb> <SEP> Ex. <SEP> 26 <SEP> 7.22 <SEP> 244 <SEP> 5 <SEP> 90.4 <tb> <SEP> CEx. <SEP> 10 <SEP> 17.33 <SEP> 587 <SEP> 12 <SEP> 83.2 <tb> Examples 27 to 31 and Comparative Example 11 Using the same autoclave as in Examples 22 to 26, the same procedure as in Examples 22 to 2G was repeated except that the amounts of manganese acetate nickel acetate and lithium acetate were changed as shown in Table 6. The yields of the effective products are shown in Table 6. Table 6 EMI16.1 <tb> <SEP> Amount <SEP> of <SEP> Concentration <tb> <SEP> Example <SEP> catalyst <SEP> of <SEP> catalyst <tb> <SEP> (Ex.) <SEP> or <SEP> (mg-atom) <SEP> in <SEP> the <SEP> start- <SEP> Yield <tb> <SEP> Compara- <SEP> Li/ <SEP> ing <SEP> mixture <SEP> of <SEP> the <tb> <SEP> tive <SEP> heavy <SEP> (ppm) <SEP> effective <tb> <SEP> Example <SEP> metal <SEP> products <tb> (CEx.) <SEP> Mn <SEP> Ni <SEP> Li <SEP> ratio <SEP> Co <SEP> Ni <SEP> Li <SEP> (%) <tb> <SEP> Ex. <SEP> 27 <SEP> 0.28 <SEP> 0.26 <SEP> 0.54 <SEP> 1.0 <SEP> 75 <SEP> 75 <SEP> 18 <SEP> 90.2 <tb> Ex. <SEP> 28 <SEP> 0.37 <SEP> 0.35 <SEP> 0.72 <SEP> 1.0 <SEP> 100 <SEP> 100 <SEP> 24 <SEP> 91.1 <tb> Ex. <SEP> 29 <SEP> 1.12 <SEP> 1.05 <SEP> 2.17 <SEP> 1.0 <SEP> 300 <SEP> 300 <SEP> 73 <SEP> 90.4 <tb> <SEP> Ex. <SEP> 30 <SEP> 1.87 <SEP> 1.75 <SEP> 3.62 <SEP> 1.0 <SEP> 500 <SEP> 500 <SEP> 123 <SEP> 88.8 <tb> Ex. <SEP> 31 <SEP> 2.61 <SEP> 2.44 <SEP> 5.05 <SEP> 1.0 <SEP> 700 <SEP> 700 <SEP> 171 <SEP> 85.6 <tb> CEx. <SEP> 11 <SEP> 2.61 <SEP> 2.44 <SEP> 0 <SEP> 0 <SEP> 700 <SEP> 700 <SEP> 0 <SEP> 82.7 <tb> Exanples 32 to- 36 Using the same autoclave as used in Examples 22 to 26, the same procedure as in Examples 22 to 26 gas repeated except that the amounts of manganese acetate, nickel acetate and lithium acetate were changed as shown in Table 7. The yields of the effective products obtained are shown in Table 7. Table 7 EMI16.2 <tb> <SEP> Amount <SEP> of <SEP> Concentration <tb> <SEP> catalyst <SEP> of <SEP> catalyst <tb> (mg/atom) <SEP> in <SEP> the <SEP> start- <SEP> Yield <tb> Li/ <SEP> ing <SEP> mixture <SEP> of <SEP> the <tb> heavy <SEP> (ppm) <SEP> effective <tb> metal <SEP> products <tb> <SEP> Example <SEP> Mn <SEP> Ni <SEP> Li <SEP> ratio <SEP> Mn <SEP> Ni <SEP> Li <SEP> (%) <tb> <SEP> 32 <SEP> 1.46 <SEP> 0.03 <SEP> 1.49 <SEP> 1.0 <SEP> 390 <SEP> 10 <SEP> 50 <SEP> 88.4 <tb> <SEP> 33 <SEP> 1.31 <SEP> 0.17 <SEP> 1.48 <SEP> 1.0 <SEP> 350 <SEP> 50 <SEP> 50 <SEP> 90.8 <tb> <SEP> 34 <SEP> 1.12 <SEP> 0.35 <SEP> 1.47 <SEP> 1.0 <SEP> 300 <SEP> 100 <SEP> 50 <SEP> 91.1 <tb> <SEP> 35 <SEP> 0.37 <SEP> 1.05 <SEP> 1.42 <SEP> 1.0 <SEP> 100 <SEP> 300 <SEP> 48 <SEP> 91.3 <tb> <SEP> 36 <SEP> 0.19 <SEP> 1.22 <SEP> 1.41 <SEP> 1.0 <SEP> 50 <SEP> 350 <SEP> 48 <SEP> 90.5 <tb> <RTI ID=17.1> Example 6 37 to 41 The same autoclave as used in Examples 22 to 26 was charged with 70 g of PX, 130 g of T, 5 g of PTA and manganese acetate, nickel acetate and lithium acetate in a concentration in the starting mixture of 200 ppm, 200 ppm and 50 ppm, respectively, as metals. The reaction was performed at each of the temperatures shown in Table 8. The yields of the effective products obtained are shown in Table 8. Table 8 EMI17.1 <tb> <SEP> Yield <SEP> of <SEP> the <tb> <SEP> Reaction <SEP> Reaction <SEP> effective <tb> <SEP> temperature <SEP> time <SEP> products <tb> Example <SEP> ( C) <SEP> (hr) <SEP> (%) <tb> <SEP> 37 <SEP> 160 <SEP> 4.5 <SEP> 89.4 <tb> <SEP> 38 <SEP> 180 <SEP> 3 <SEP> O <SEP> go.o <SEP> <tb> <SEP> 39 <SEP> 200 <SEP> 3.0 <SEP> 91.7 <tb> <SEP> 210 <SEP> 1.5 <SEP> 91.4 <tb> <SEP> 41 <SEP> 230 <SEP> 1.5 <SEP> 89. <SEP> 8 <SEP> <tb> Example 42 A mixture composed mainly of p-xylene and methyl p-toluate was oxidized in the liquid phase with air in the presence of (i) a mixture of cobalt acetate and manganese acetate or (ii) a mixture of nickel acetate and manganese acetate to form an oxidation reaction mixture containing p-toluic acid and monomethyl terephthalate as main ingredients. The oxidation reaction mixture was then esterified with methanol to form an ester mixture containing methyl p-toluate and dimethyl terephthalate as main ingredients. The concentrations of cobalt and manganese or manganese and nickel as metals in the ester mixture were as follows: (i) Co= 1003 ppm, tOn= 61 ppm (ii) Mn = 1015 ppm, Ni = 1014 ppm One hundred grams of tile ester mixture was fed into a 200 ml three-necked flask, and lithium acetate was added in an amount equal in gram-atom to the heavy metals. The mixture was maintained at 2500C for 24 hours under sealing of N2. Then, the ratio of the heavy metals deposited after the heating rpas calculated. The presence or absence of lithium acetate and the ratio of the heavy metals deposited are shown in Table 9. Ratio of Amount of heavy metals heavy metals = ( 1 - ##################### ) x 100 deposited (%) metals Table 9 EMI18.1 <tb> <SEP> Ratio <SEP> of <SEP> heavy <SEP> metal <tb> <SEP> Addition <SEP> of <SEP> deposited <tb> <SEP> lithium <tb> Run <SEP> No. <SEP> acetate <SEP> Co <SEP> ?4n <SEP> Ni <SEP> Catalyst <tb> <SEP> 42-1 <SEP> No <SEP> 66 <SEP> O <SEP> - <SEP> (i) <tb> <SEP> 42-2 <SEP> Yes <SEP> O <SEP> O <SEP> - <SEP> (i) <tb> <SEP> 42-3 <SEP> No <SEP> - <SEP> 59 <SEP> 72 <SEP> (ii) <tb> <SEP> 42-4 <SEP> Yes <SEP> - <SEP> 17 <SEP> 29 <SEP> (ii) <tb> Example 43 and Comparative Example 12 The same autoclave as used in Examples 1 to 5 was charged with 60 g of PX, 140 g of tST and 5 g of PTA and as a catalyst, cobalt acetate and lithium acetate. While stirring the mixture at high speed at a temperature of 160 C and a pressure of 4 kg/cmê#G, air was blown into it so that the flow rate of the air at the exit became 1200 cc. The reaction was performed for 3.5 hours after absorption of oxygen began. After the reaction, the same procedure as. in Examples 1 to 5 was performed, and the yields of effective products were determined. The amounts od cobalt acetate and lithium acetate added in the oxidation e=eriment were 250 ppm (0.875 mg-atom), and 30 ppm (0.888 mg-atom), respectively1 as metals in terms of their concentrations in the starting mixture. For comparison, the same experiment as above was repeated except that lithium acetate was not added The yields of the effective products in these experiments are shown in Table 10. Table 10 EMI19.1 <tb> <SEP> Concentration <tb> <SEP> Amount <SEP> of <SEP> of <SEP> catalyst <tb> <SEP> catalyst <SEP> in <SEP> the <SEP> start- <SEP> Yield <tb> <SEP> added <SEP> ing <SEP> mixture <SEP> Li/ <SEP> of <SEP> the <tb> <SEP> (mg-atom) <SEP> (ppm) <SEP> heavy <SEP> effective <tb> <SEP> metal <SEP> products <tb> <SEP> Co <SEP> Li <SEP> Co <SEP> Li <SEP> ratio <SEP> (%) <tb> Example <SEP> 43 <SEP> 0.875 <SEP> 0.888 <SEP> 250 <SEP> 30 <SEP> 1.01 <SEP> 85.7 <tb> Comparative <SEP> 0.875 <SEP> 0 <SEP> 250 <SEP> 0 <SEP> 0 <SEP> 81.8 <tb> Example <SEP> 12 <tb> Example 44 and Comparative Example 13 The same autoclave a-s used in Examples 1 to 5 was charged with 200 g of toluene, 5 g of benzoic acid, and as a catalyst, cobalt acetate, manganese acetate and lithium acetate in a concentration, as metal in the starting mixture, of 150 ppm (0.525 mg-atom), 5 ppm (0.019 mg-atom), and 15 ppm (0.443 mg-atom3, respectively. While stirring the mixture at high speed at a temperature of 1700C and a pressure of 7 kgZcm .G, air was bloom into it so that the flow rate of the air at the exit became 1,500 cc/min. The reaction was performed for 3 hours after absorption of oxygen began. After the reaction, the reaction mixture was cooled, withdrawn. and analyzed for the amounts of benzoic acid, benzyl alcohol, benzaldehyde, benzyl benzoate and other products formed. Benzyl alcohol, benzaldehyde and benzyl benzoate are intermediates to benzoic acid, and are evaluated as effective products. The yield of the effective products was calculated in accordance with the following equation. Total amount (millimoles) Yield (%) of of benzoic acid and effective = ###################### x 100 products toluene consumed For comparison, the above procedure was repeated except that lithium acetate was not added. The yields of the effective-products in these experiments are also shown in Table 11. Table 11 EMI20.1 <SEP> Amount <SEP> of <SEP> Concentration <tb> <SEP> catalyst <SEP> of <SEP> catalyst <tb> <SEP> (mg-atom) <SEP> in <SEP> the <SEP> start- <SEP> Yield <tb> <SEP> ing <SEP> mixture <SEP> Li/ <SEP> of <SEP> the <tb> <SEP> (ppm) <SEP> heavy <SEP> effective <tb> <SEP> metal <SEP> products <tb> <SEP> Co <SEP> Mn <SEP> Li <SEP> Co <SEP> Mn <SEP> Li <SEP> ratio <SEP> (%) <tb> <SEP> Example <SEP> 0.525 <SEP> 0.019 <SEP> 0.443 <SEP> 150 <SEP> 5 <SEP> 15 <SEP> 0.84 <SEP> 92.7 <tb> <SEP> Compa <tb> <SEP> rative <tb> Example <SEP> 0.525 <SEP> 0.019 <SEP> 0 <SEP> 150 <SEP> 5 <SEP> 0 <SEP> 0 <SEP> 90.4 <tb> <SEP> 13 <tb>

Claims: 1. A process for producing an aromatic carboxylic acid or its nethyl ester which comprises oxidizing at least one aromatic compound having at least one methyl or formyl group directly bonded to a nuclear carbon atom of the aromatic ring in the liquid phase with molecular oxygen or a gas containing molecular oxygen in the presence of a heavy metal compound as a catalyst in the substantial absence of an aliphatic carboxylic acid as a solvent to form the corresponding aromatic carboxylic acid, and if desired, esterifying the oxidation reaction mixture containing the aromatic carboxylic acid with methanol; said oxidation reaction being carried out in the copresence of 0.1 mole to 10 moles, per mole of said heavy metal compound catalyst, of a lithium compound. 2. The process of claim 1 herein said aromatic compound is at least one aromatic hydrocarbon selected from the group consisting of p-xylene, p-toluic acid, methyl p-toluate and p-tolualdehyde. 3. The process of claim 1 wherein said aromatic compound is a mixture of p-xylene and methyl p-toluate. 4. The process of any one of claims 1 to 3 lSerein said heavy metal catalyst is either 1) a cobalt compound at least partly soluble in the reaction system, 2) a mixture of a cobalt compound at least partly soluble in the reaction system and a manganese compound at least partly soluble in the reaction system, or 3) a mixture of a nickel compound at least partly soluble in the reaction system and a manganese compound at least partly soluble in the reaction system. 5. The process of any one of claims 1 to 3 Wherein said heavy metal compound catalyst is a mixture of (A) a cobalt compound at least partly soluble in the reaction system and (B) a manganese compound at least partly soluble in the reaction system, said cobalt compound being present in the reaction system such that the concentration of cobalt metal is 100 to 600 ppm. 6. The process of claim 5 wherein said cobalt compound and manganese compound are present in the reaction system such that the atomic ratio of cobalt metal to manganese metal is from 100:1 to 100:25. 7. The process of any one of claims 5 to 6 llerein the oxidation reaction is carried out at a temperature of 160 to 2000C. 8. The process of any one of claims 1 to 7 wherein the lithium compound is present in gn amount of 0.2 mole to 5 moles per mole of said heavy metal compound catalyst. 9. A process for producing methyl esters of aromatic carboxylic acids consisting predominantly of dimethyl terephthalate and methyl p-toluate, which comprises contacting a mixture of p-xylene and methyl p-toluate in the liquid phase with molecular oxygen of a gas containing molecular oxygen at a temperature of 160 to 220 C in the substantial absence of an aliphatic carboxylic acid solvent in the presence of, as a catalyst, (,) a cobalt compound at least partly soluble in the reaction system and (B) a manganese compound at least partly soluble in the reaction system, and (C) a lithium compound at least partly soluble in the reaction system, the concentration of said cobalt compound in the entire reaction mixture being 100 to 600 ppm as metal, and the atomic ratio of cobalt metal to manganese metal being from 100:1 to 100:25, and the amount of said lithium compound being 0.1 mole to 10 moles per mole of The cobalt compound and manganese compound combined; and esterifying the oxidation reaction mixture with methanol.

Inventors: ANNO, TATSURO, ISHIDA, KENJI, NONOBE, MASAO, OMOTO, YORIHIKO TEIJIN OKAMOTO SHATAKU A-504, TAKEDA, SHINICHI
Applicants: TEIJIN HERCULES CHEMICAL CO., LTD.
Application year: 1979
Main classification: C07C51
IPC codes: C07C51, C07C69, C07C67, C07C65, C07B61, C07C63, B01J31