PROCESS FOR THE CO-PRODUCTION OF CARBOXYLIC ACIDS AND CARBOXYLIC ACID ESTERS

Abstract: Process for the co-production of carboxylic acids of the general formula R¹-COOH and R²-COOH and carb­ oxylic acid esters of general formula R¹-COOCH₂R² and R²-COOCH₂R¹ from carboxylic acid esters of general formula R¹-COOR² and/or ethers of general formula R³OR⁴ (H¹, R², R³ R⁴ representing (substituted) alkyl or (substituted) aryl, alkaryl or aralkyl, R¹ also representing H), carbon monoxide and hydrogen at elevated tem­ perature and pressure in the presence of a ruthenium compound, a further Group VIII metal compound, and a compound R⁵Hal or R⁵COHal where R⁵ has one of the meanings given for R² and Hal is iodine or bromine, the reaction mixture being substantially free from other transition metal or Group II metal iodides or bromides, and containing not more than 1 mol of amine, amine oxide or a quaternary derivative thereof per gram atom of ruthenium. The process is of special interest for the selective conversion of methyl acetate into ethyl acetate and acetic acid at pressures well below 100 bar.

Description: PROCESS FOR THE CO-PRODUCTION OF CARBOXYLIC ACIDS AND CARBOXYLIC ACID ESTERS The present invention relates to a process for the co-production of carboxylic acids and carboxylic acid esters from carboxylic acid esters having one carbon atom less in the molecule, carbon monoxide and hydrogen in the presence of a catalytic system. The invention relates in particular to a process for the co-production of acetic acid and ethyl acetate from methyl acetate under mild process conditions. Carboxylic acid esters produced according to the process according to the present invention are thus homologues of the carboxylic acid esters used as starting materials. The production of carboxylic acid esters via homologation has already been described in the literature. For instance, it is known from Dutch published patent application 7807520 that carboxylic acid esters (especially ethyl acetate from methyl acetate) can be prepared at elevated temperatures at a pressure of at least 100 bar, preferably between 200 and 1500 bar in the presence of cobalt, rhodium, ruthenium, or iron or salts thereof. Apart from the fact that very high pressures have to be applied in order to get a reasonable conversion, the process as described also has the disadvantage that water is produced as the co-product. It will be clear that water can cause hydrolysis of the esters present in the reaction mixture (whether being present as product or as starting material). Even when very high, unattractive pressures (e.g. well over 1000 bar) are used substantial amounts of alkanols are produced. It is further known from German Offenlegungsschrift 2733663 that the homologation of methyl acetate (or of its precursor dimethyl ether) can be carried out using a ruthenium carbonyl compound and an iodide or bromide promotor at elevated temperatures and pressures. The process as described in the German Offenlegungsschrift also has to be carried out at very high pressures (well over 200 bar) and substantial amounts of other products (including not only alkanols but also methane) are formed. It is known from Dutch published patent application 7602096 that methyl acetate can be converted using carbon monoxide and hydrogen in the presence of a specific catalyst comprising a Group VIII noble metal compound and a halogen (especially iodine) source into acetic acid and ethylidene diacetate. However, ethyl acetate (the homologation product according to the process according to the present invention ) is not even mentioned as a by-product. European Patent Application No. 31606 discloses that by the use of a very specific catalytic system, the stoichiometry of the known reactions of methylacetate with carbon monoxide and hydrogen can be altered most advantageously to produce one mole of ethyl acetate and two moles of acetic acid from two moles of methyl acetate. The catalytic system comprises three metal compounds: a ruthenium compound, a further Group VIII metal compound, and a bromide or iodide of a Group II or transition metal. As is common in catalytic systems, the reaction mixture preferably also contains a promotor, typically an amine, such as alpha-picoline, or a phosphine, such as triphenylphosphine. Thus for example Example I of said specification illustrates the homologation of methyl acetate over a catalytic system comprising ruthenium III chloride trihydrate, rhodium III chloride trihydrate, zinc iodide, and alpha-picoline, while Comparative Example B of said specification shows that the reaction is not successful if the zinc iodide is replaced by methyl iodide. Most surprisingly, it has now been found that an alkyl or acyl iodide or bromide can replace the Group II or transition metal iodide or bromide in the catalytic system of European Patent Application No. 31606, provided that the reaction mixture contains not more than 1 mol of amine or amine oxide. It will be appreciated that in the reaction mixture quaternary derivatives are formed by the reaction of the amine or amine oxide with the alkyl or acyl iodide or bromide or HBr or HI formed in situ. Consequently, the use of separately prepared quaternary derivatives of amines and amine oxides instead of amines or amine oxides themselves is within the scope of the present invention. The present invention provides a process for the co-production of carboxylic acids of the general formula R1-COOH and R2-COOH and carboxylic acid esters of the general formula R1-COOCH2R2 and R2-COOCH2R1 wherein each of the groups R1 and R2, which may be the same or different, represents an alkyl group having from 1 to 20 carbon atoms which may be substitued by one or more inert substituents such as fluorine or chlorine containing moieties or hydroxy, alkoxy or alkanoyl groups, or an aryl, alkaryl or aralkyl group which may be substituted by one or more inert substituents such as fluorine or chlorine containing moieties or alkoxy or alkanoyl groups whilst R1 may also represent a hydrogen atom, characterized in that a carboxylic acid ester of the general formula R1-COOR2 and/or an ether of the general formula R30R4, wherein R1 and R2 are as defined hereinbefore and each of R3 and R4, which may oe the same or different, represents an alkyl group having from 1 to 20 carbon atoms which may be substituted by one or more inert substituents such as fluorine or chlorine containing moieties or hydroxy, alkoxy or alkanoyl groups, or an aryl, alkaryl or aralkyl group which may be substituted by one or more inert substituents such as fluorine or chlorine containing moieties or alkoxy or alkanoyl groups, is reacted with carbon monoxide and hydrogen at elevated temperature and pressure in the presence of a catalytic system which comprises a ruthenium compound, a further Group VIII metal compound, and a compound of the general formula R5Hal or R5COHal where R5 has one of the meanings given above for R2 and Hal represents an iodine or bromine atom, the reaction mixture being substantially free from other transition metal or Group II metal iodides or bromides, and containing not more than 1 mol of amine, amine oxide or a quaternary derivative thereof per gram atom of ruthenium. It should be noted that the composition of the reaction product mixture will be governed by the choice of the starting carboxylic acid esters and/or ethers. For instance, when starting materials are used wherein the groups R1 and R2 are identical, such as in methyl acetate, dimethyl ether and ethyl propionate, the reaction product mixture will normally contain only the carboxylic acid ester homologue and the appropriate acid. When starting materials are used wherein the groups R1 and R2 are not identical, a more complex reaction product mixture will be obtained which comprises normally at least two carboxylic acid ester homologues and two appropriate carboxylic acids. For instance, when ethyl acetate is used as the starting material the reaction product mixture comprises propyl acetate, ethyl propionate, propionic acid and acetic acid. It will be appreciated that any carboxylic acid ester homologue produced according to the present process can serve as starting material in the process according to the present invention thus forming the next carboxylic acid ester homologue(s) and the appropriate carboxylic acid(s). In addition, since carboxylic acids are produced in the process according to the present invention, transesterification reactions, i.e. reactions between carboxylic acids and carboxylic acid esters, or between different carboxylic acid esters, may also occur under the prevailing reaction conditions. It will be clear that transesterification reactions do not alter the product composition when the starting material comprises compounds wherein R1 and R2 are identical, but may alter the product composition when the groups R1 and R2 are not identical. For the purpose of the present invention, carboxylic acids and carboxylic acid esters, obtained via a further homologation of produced carboxylic acid ester, or obtained by a transesterification process under the prevailing conditions, are considered to be within the scope of the present invention. From the above it will be clear that preference is given to processes wherein starting materials are used wherein the groups R1 and R2 are identical since a less complex reaction mixture will be obtained. The process according to the present invention is of special interest for the co-production of acetic acid and ethyl acetate from methyl acetate according to the equation: EMI5.1 since the products can be obtained with high selectivity and close to the stoichiometrically expected ratio. This is of special interest when the process according to the invention is part of an integrated process, wherein acid produced - for instance acetic acid - is to be recycled in the process. Moreover, the process according to the present invention can be carried out conveniently at surprisingly low pressures, e.g. pressures well below 100 bar can be used advantageously. Suitable starting materials which can be used conveniently in the process according to the present invention include compounds of the general formula R1-COOR2 and/or R30R4, wherein each of R1, R2, R3 and R4, which may be the same or different, represents an alkyl group having from 1 to 12 carbon atoms, or an aryl, alkaryl or aralkyl group having up to 12 carbon atoms, whilst R1 may also represent a hydrogen atom. Preference is given to the use of compounds of the general formula R1-COOR2 and/or R30R4, wherein R1, R2, R3 and R4 are the same and each represents an alkyl group having from 1 to 12 carbon atoms or an aryl, alkaryl or aralkyl group having up to 12 carbon atoms. Most preferred starting materials are methyl acetate and dimethyl ether. When ethers of the general formula R30R4 are used as starting materials in the process according to the present invention, it would appear that these compounds will be converted primarily into the corresponding esters by the introduction of a carbon monoxide moiety into the molecule which molecule may then undergo the homologation reaction according to the present invention. If desired, the reaction according to the present invention may be carried out in two stages when an ether is used as the starting material. Firstly, the ether is converted into the corresponding ester which in its turn, in the same or in a different vessel, is converted into the final products. If desired, mixtures of carboxylic acid esters and/or ethers can be used as starting materials. Ruthenium compounds which can be used conveniently in the process according to the present invention include ruthenium (III) chloride, ruthenium (III) chloride trihydrate, ruthenium (IV) chloride, ruthenium (III) bromide, the ruthenium oxides, organic ruthenium salts such as ruthenium (III) propionate, ruthenium (III) butyrate, ruthenium pentacarbonyl, trirutheniumdodecacarbonyl and mixed ruthenium halocarbonyls such as bis-(rutheniumtricarbonyl-dibromide), and other organoruthenium complexes. Further Group VIII metal compounds which can be used together with a ruthenium compound in the catalytic system include palladium and, especially, rhodium compounds, although other Group VIII metal compounds can also be used. Examples of suitable rhodium compounds include rhodium oxide, rhodium (III) hydroxide, rhodium (III) chloride, rhodium (III) chloride trihydrate, rhodium (III) bromide, rhodium (III) iodide and the corresponding pyridine and phosphine complexes such as tris(pyridine) rhodium (III) chloride or dichloro bis-(triphenylphosphine) rhodium, rhodium (III) formate, rhodium (III) acetate, rhodium (III) butyrate, rhodium (III) naphthenate, dirhodium octacarbonyl, tetrarhodium dodecacarbonyl, hexarhodium hexadecacarbonyl, rhodium dicarbonylacetylacetonate and other organo-rhodium complexes. Preference is given to the use of rhodium (III) chloride trihydrate. Examples of suitable palladium compounds include palladium chloride, palladium chloride dihydrate, palladium bromide, palladium iodide, palladium oxide, or an organic palladium salt or complex such as palladium formate, palladium acetate, palladium butyrate and palladium acetylacetonate. Preferred palladium compounds are palladium chloride, palladium chloride dihydrate and palladium acetate. The molar ratio of ruthenium compound to further Group VIII metal compound is not critical and can vary between wide limits, e.g. atomic ratios of ruthenium to further Group VIII metal between 50:1 and 1:20, especially 10:1 and 1:5, are suitable. The amount of ruthenium compound and further Group VIII metal compound to be used is not critical and any amount which exerts catalytic activity can be used. Amounts as low as 0.001 ZOw, calculated on carboxylic acid ester or ether to be converted can be used, preference being given to amounts in the range of from 0.01-10 jgw, most preferably between 0.05-5 %w. Any iodide or bromide R5Hal or R5COHal may be used in the process according to the present invention, but preferably R5 has one of the preferred meanings given above for R2, and preferably the group R5 is identical to one of the groups Rl, R2, R3 or R4 in the starting material, as this avoids the formation of additional mixed products. Especially preferred is the use of a reaction mixture in which R1 and R2 are the same, and the iodide or bromide has the formula R2I, R2Br, R2COI or R2COBr. Thus for example when using the preferred feedstocks methyl acetate and/or dimethyl ether, methyl iodide or bromide or acetyl iodide or bromide, or any mixture thereof, is preferably used. The quantity of iodide or bromide added to the reaction mixture is not crucial. Suitably the number of moles of added iodide plus bromide per gram atom of total Group VIII metal is in the range of from 0.1:1 to 200:1, preferably 1:1 to 100:1, and especially 10:1 to 50:1. As stated hereinbefore, it has most surprisingly been found that a compound according to the general formula R5Hal and/or R5COHal can be used in stead of the Group II or transition metal iodide or bromide as long as a ruthenium compound and a further Group VIII metal compound are present. The process can be carried out conveniently in the absence of a promotor. Reasonable conversions of starting materials can be obtained whilst maintaining the desired selectivity towards ester and acid products. It has been found that the presence of a small amount of amine or amine oxide has a very beneficial effect on the reaction rate whilst maintaining a high selectivity towards the desired products. In this context, it should be noted that the use of a larger amount'of amine or amine oxide substantially destroys the stoichiometry of the desired products. It was found that the use of an alpha-picoline/ ruthenium III mol ratio of 6 in the homologation reaction of methyl acetate produced a large amount of acetic acid as well as by-products in a larger amount than ethylacetate. The use of a pyridinium oxide/ruthenium III mol ratio of 4 in the homologation reaction of methyl acetate produced large amounts of ethylidene diacetate and acetic anhydride and only a trace of ethyl acetate. Care should therefore be taken that the reaction mixture does not contain more than 1 mole of amine or amine oxide per gram atom of ruthenium, and preferably not more than 0.5 mol, especially between 0.05 and 0.5 mol of amine or amine oxide per gram atom of ruthenium. Although the use of an amine or amine oxide in an amine or amine oxide/ruthenium ratio above 1 does still lead to the production of homologues, it was found that other products appeared to be formed with a rapidly increasing rate, acetic acid anhydride and ethylidene diacetate becoming the predominant (by)-products. Suitably amines, amine oxides and quaternary derivatives thereof which may be present in the specified amounts include alkyl, cycloalkyl, aryl and aralkyl amines containing up to 30 carbon atoms and, especially, amines in which the nitrogen atom is part of a heterocyclic ring, for example pyrrole, alkyl-substituted pyrroles, pyrrolidine, alkyl-substituted pyrrolidines, pyridine, alkyl-substituted pyridines, piperidines, alkyl-substituted piperidines, pyrimidine, alkyl-substituted pyrimidines, pyrazine benztriazole, tetraethylenediamine, l,10-phenanthroline, alkyl-substituted 1,10-phenanthrolines, morpholine and alkyl-substituted morpholines, their oxides and their quaternary derivatives. Preference is given to the use of pyridine and an alkyl-substituted pyridine such as the various picolines, e.g. alpha-picoline or an oxide or quaternary derivative thereof. The process according to the present invention can be carried out using a wide range of temperatures. Temperatures up to 3000C can be suitably applied. Preference is given to temperatures in the range of from 50"C to 2000C, most preferred temperatures are in the range between 125"C and 175 C. The process according to the present invention can be carried out using low pressures, e.g. pressures as low as 5 bar. Pressures in the range of from 20 to 100 bar are preferred. Higher pressures, e.g. pressures as high as 1000 bar can be applied, but they are generally not economical because of the investment and energy costs involved. According to the reaction equation carbon monoxide and hydrogen are consumed in a molar ration of 1:1. It has been found, however, that without any substantial disadvantage wider molar ratios, e.g. ratios of from 1 to 10:1 can be applied. Preference is given to atIos- carbon de: Br I XaX c GS 1:0.5 to 1:3. The process according to the present invention may be carried out in the presence of a solvent. Suitable solvents include carboxylic acids such as acetic acid or propanoic acid; carboxylic acid esters, such as methyl acetate, ethyl acetate, methylpropionate or ethyl propionate (being used as solvent as well as starting material), and cyclic ethers such as tetrahydrofuran, 1,4-dioxane, 1,3-dioxane and the dioxolanes. Also dialkyl ethers used in excess as starting material may be regarded as solvent for the process according to the present invention. Suitable dialkylethers include dimethyl ether, diethyl ether and methyl t-butyl ether. Other compounds which can be used as solvent in the process according to the present invention include sulphones and sulphoxides. Examples of such compounds are dimethylsulphone, sulpholane, 2-methyl sulpholane, 3-methyl sulpholane, dimethylsulphoxide and diethyl sulphoxide. Especially good results are obtained when alkanoic acids such as acetic acid are used as solvent. If however a solvent other than an alkanoic acid is used, it may be desirable to carry out the reaction in the presence of small amounts of a strong acid. For example amounts of strong acid of up to 100 equivalents of acid per gram atom of total Group VIII metal, may be added. Suitable strong acids include those which in aqueous solution at 20"C have a pKa of less than 3.5, for example organic acids such as p-toluene sulphonic acid or trifluoromethane sulphonic acid, or mineral acids such as hydrochloric, sulphuric or perchloric acid. It has been found that the mild conditions according to the present invention even tolerate the presence of some water in the reaction medium. Although the presence of water is not preferred, amounts of up to 15 70aJ, based on total solvent, can be present. The process according to the present invention can be carried out in the liquid phase or in the gaseous phase. Preference is given to a liquid phase which enables a convenient introduction of carbon monoxide and hydrogen into the reaction vessel. If desired, the carbon monoxide and hydrogen can be introduced together into the reaction vessel. The process according to the present invention can be carried out batchwise, semicontinuously or continuously. The process according to the present invention is also of interest in that it can be integrated with known processes, either for the production of the starting materials (i.e. carboxylic acid esters or the corresponding ethers) or for the conversion of the carboxylic acid esters produced into other products, e.g. by transesterification processes. For instance, when the present process produces ethyl acetate, it can be integrated with a process for the preparation of methyl acetate from acetic acid and methanol using an acidic catalyst. Since the present process produces acetic acid, that compound may be recycled to serve as feedstock for the preparation of methyl acetate. If desired, the present process can also be integrated with a transesterification process, wherein ethylacetate is transesterified with methanol to give methyl acetate (which can be recycled to serve as feedstock for the present process) and ethanol which can either be sold as such or converted into other products such as ethylene. In such a case acetic acid and/or methyl acetate can be removed from the system in an amount equimolar with ethanol produced. The following Examples 11ustrace the invention. Example I The experiment was carried out in a 300 ml magnetdriven autoclave of 9astello7 C (Trade Mark) which contained 25 ml methyl acetate, 25 ml acetic acid, 60 mmol methyl iodide, û.5 mmol rhodium (III) chloride trihydrate and 1 mmol ruthenium (III) chloride trihydrate. The vessel was flushed with carbon monoxide, and then pressurised with carbon monoxide (20 bar partial pressure) and hydrogen (20 bar partial pressure). The autoclave was then heated to 1600C and kept at this temperature for 5 hours, during which time the pressure was maintained constant by feeding in carbon monoxide and hydrogen (1:1) as required. After this time the reaction mixture was analysed by gas-liquid chromatography and shown to contain 9.1 %w ethyl acetate. On a molar basis the conversion of the starting material was about 33 % with an almost 100 % selectivity towards the two products ethyl acetate and acetic acid. Only traces (less than 0.5 %) of by-products were detected: in particular, no alcohols were detected. Example II The method of Example I was repeated except that an additional 0.5 mmol rhodium III chloride trihydrate were added. After the reaction time was over, the reaction mixture contained 15.2 %w ethyl acetate, and 55% of the methyl acetate had been converted to the desired products. Only traces of by-products were observed. Example III The method of Example I was repeated except that the 25 ml acetic acid were replaced by 25 ml methyl acetate. The final reaction mixture contained 4.5 %w ethyl acetate and 6.1 70w acetic acid, and 7.5% of the methyl acetate had been converted to products. Example IV The method of Example I was repeated except that 0.1 mmol alpha-ico3ine were also added. 75% of the methyl acetate was converted into products, and the reaction mixture contained 18.5 %w ethyl acetate. Example V The method of Example IV was repeated except that only half of the amount of rhodium III chloride trihydrate was used (0.25 mmol). 50% of the methyl acetate was converted into products, and the reaction mixture contained 14.4 %w ethyl acetate. Example VI The method of Example V was repeated except that alpha-picoline was used in an amount of 0.5 mmol and rhodium III chloride trihydrate in an amount of 0.1 mmol. 50% of the methyl acetate was converted into products, and the reaction mixture contained 13.5 %w ethyl acetate. Example VII The method of Example IV was repeated but using pyridine (0.1 mmol) instead of alpha-picoline and an initial carbon monoxide pressure of 15 bar and hydrogen pressure of 30 bar. 80% of the methyl acetate was converted into products, and the reaction mixture contained 19.1 %w ethyl acetate. Example VIII The method of Example I was repeated but using 0.1 mmol of rhodium (III) chloride trihydrate instead of 0.5 mmol of rhodium (III) chloride trihydrate, a carbon monoxide partial pressure of 15 bar instead of 20 bar, and a hydrogen partial pressure of 30 bar instead of 20 bar. Furthermore, 0.5 mmol of pyridinium oxide was added to the reaction mixture. An amount of 45% of the methyl acetate was converted into products. The reaction mixture contained 14 7w ethyl acetate.

Claims: CLAIMS 1. A process for the co-production of carboxylic acids of the general formula R1-COOH and R2-COOH and carboxylic acid esters of the general formula R1-COOCH2R2 and R2-COOCH2R1, wherein each of the groups R1 and R2, which may be the same or different, represents an alkyl group having from 1 to 20 carbon atoms which may be substituted by one or more inert substituents such as fluorine or chlorine containing moieties or hydroxy, alkoxy or alkanoyl groups, or an aryl, alkaryl or aralkyl group which may be substituted by one or more inert substituents such as fluorine or chlorine containing moieties or alkoxy or alkanoyl groups whilst R1 may also represent a hydrogen atom, characterized in that a carboxylic acid ester of the general formula R1-COOR2 and/or an ether of the general formula R30R4 wherein R1 and .R2 are as defined hereinbefore and each of R3 and R4, which may be the same or different, represents an alkyl group having from 1 to 20 carbon atoms which may be substituted by one or more inert substituents such as fluorine or chlorine containing moieties or hydroxy, alkoxy or alkanoyl groups, or an aryl, alkaryl or aralkyl group which may be substituted by one or more inert substituents such as fluorine or chlorine containing moieties or alkoxy or alkanoyl groups, is reacted with carbon monoxide and hydrogen at elevated temperature and pressure in the presence of a catalytic system which comprises a ruthenium compound, a further Group VIII metal compound, and a compound of the general formula R5Hal or R5COHal where R5 has one of the meanings given above for R2 and Hal represents an iodine or bromine atom, the reaction mixture being substantially free from other transition metal or GroupII metal iodides or bromides, and containing not more than 1 mol of amine, amine oxide or a quaternary derivative thereof per gram atom of ruthenium. 2. A process according to claim 1 characterized in that as starting materials are used compounds of the general formula R1-COOR2 and/or R30R4 wherein each of R1, R2, R3 and R4 which may be the same or different, represents an alkyl group having from 1 to 12 carbon atoms or an aryl, alkaryl or aralkyl group having up to 12 carbon atoms, whilst R1 may also represent a hydrogen atom, and preferably are the same and represent an alkyl group having from 1 to 12 carbon atoms or an aryl, alkaryl or aralkyl group having up to 12 carbon atoms. 3. A process according to claim 1 or 2 characterized in that as ruthenium compound is used ruthenium (III) chloride, ruthenium (III) chloride trihydrate, ruthenium (IV) chloride, ruthenium (III) bromide, ruthenium oxide or an organic ruthenium salt or complex. 4. A process according to any one of the preceding claims characterized in that as further Group VIII metal compound is used a rhodium compound such as rhodium oxide, rhodium (III) hydroxide, rhodium (III) chloride, rhodium (III) chloride trihydrate, rhodium (III) bromide, rhodium (III) iodide or an organic rhodium salt or complex, preferably rhodium (III) chloride trihydrate, or a palladium compound such as palladium chloride, palladium chloride dihydrate, palladium bromide, palladium iodide, palladium oxyde or an organic palladium salt or complex, preferably palladium chloride, palladium chloride dibydrate or palladium acetatee 5. A process according to claim 4, characterized in that a rhodium compound is used as further Group VIII metal compound. 6. A process according to any one of the preceding claims, characterized in that the ruthenium compound and the further Group VIII metal compound are used in a ratio between 50:1 and 1:20, preferably between 10:1 and 1:5. 7. A process according to any one of the preceding claims, in which the group R5 is identical to one of the groups R1, R2, R3 or R4 in the starting material. 8. A process according to anyone of the preceding claims, in which an amine, amine oxide or a quaternary derivative thereof is present in the reaction mixture in an amount of from 0.05 to 0.5 moles per gram atom of ruthenium. 9. A process according to claim 8, in which pyridine or an alkyl-substituted pyridine, especially alpha-picoline or an oxide thereof is used as the amine or amine oxide. 10. A process according to any one of the preceding claims characterized in that the reaction is carried out at a temperature in the range of from 50"C to 2000C, and especially between 1250C and 1750C. 11. A process according to any one of the preceding claims characterized in that the process is carried out using a pressure between 20 and 100 bar.

Inventors: DRENT, EIT
Applicants: SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ B.V.
Application year: 1982
Main classification: C07C51
IPC codes: C07C51