Catalysts for the catalysed hydrogenation of carboxylic acids and their anhydrides to alcohols and/or esters

Abstract: An alcohol and/or a carboxylic acid ester is produced from a carboxylic acid or anhydride thereof by reacting the acid or anhydride with hydrogen at elevated temperature in the presence as catalyst of a composition comprising an alloy of (i) at least one noble metal of Group VIII of the Periodic Table and (ii) at least one metal capable of alloying with the Group VIII noble metal, optionally including a support and at least one of the metals rhenium, tungsten or molybdenum. The process is particularly applicable to the hydrogenation of monobasic acids, for example acetic acid, and the hydrogenation of maleic acid or maleic anhydride to gamma-butyrolactone.

Description: The present invention relates to catalysts for use in the catalysed hydrogenation of carboxylic acids and their anhydrides to produce the corresponding alcohol and/or carboxylic acid ester. The hydrogenation of carboxylic acids to produce the corresponding alcohol in the presence of heterogeneous catalysts is known from, for example, USP-A-4524225, USP-A-4104478, GB-A-1534232, GB-A-1551741, DE-A-3221077 and EP-A-147219. USP-A-4524225 describes the hydrogenation of C₆-C₂₄ fatty acids by contacting the fatty acid with hydrogen at 100 to 300°C and 0.7 to 20.7 MPag (100 to 3000 psig) in the presence of a zerovalent metal selected from Cu, Cr, Ru, Pt, Pd, Re and mixtures thereof dispersed on a support which may be alpha, theta or titanated alumina, titania, or AlPO₄ or a mixture thereof. USP-A-4104478 describes the production of C₄ to C₂₄ fatty alcohols by catalytically hydrogenating the corresponding fatty acid at 170 to 250°C and 2.0 to 14.2 MPa (20 to 140 atmospheres) over a catalyst system consisting of (a) 1 part wt. of activated Re, and (b) 0.25 to 1.5 parts of an extrinsic metal catalyst selected from Ru, Rh, Pt and Pd. GB-A-1534232 describes the preparation of alcohols by catalytic hydrogenation of carboxylic acids at elevated temperature and pressure in the presence of water and/or solvents using a Pd/Re catalyst on a support, the catalyst having a Pd:Re wt ratio of 0.01 to 5:1. GB-A-1551741 describes the one-step preparation of 1,4-butanediol from maleic acid by hydrogenation in the presence of a catalyst containing (A) elements of Group VII, preferably Mn or Re, or their compounds, and (B) elements of Group VIII, preferably Ru, Rh, Pd, Os, Ir or Pt, more preferably Pd or Pt or their compounds or mixtures thereof. DE-A-3221077 describes the continuous production of ethanol by the hydrogenation of acetic acid at elevated pressure and temperature using a catalyst based on cobalt. EP-A-147219, published after the priority date claimed for the subject application on an application claiming an earlier priority date, describes the hydrogenation of maleic acid using a Pd/Re/C catalyst. Our copending European application publication No. 0198682 (BP Case No. 6347) provides a process for the production of an alcohol and/or a carboxylic acid ester from a C₂ to C₁₂ carboxylic acid by contacting the carboxylic acid at elevated temperature and pressure with hydrogen in the presence of a heterogeneous catalyst characterised in that the catalyst comprises a first component which is either molybdenum or tungsten and a second component which is a noble metal of Group VIII of the Periodic Table of the Elements. Finally, our copending European application publication No. 0198681 (BP Case No. 5930) discloses a process for the production of either ethanol from acetic acid or propanol from propionic acid which process comprises contacting either acetic acid or propionic acid in the vapour phase with hydrogen at elevated temperature and a pressure in the range from 1x10⁵ to 1.5x10⁷ Pa (1 to 150 bar) in the presence of a catalyst comprising as essential components (i) a noble metal of Group VIII of the Periodic Table of the Elements, and (ii) rhenium. A problem associated with the use of heterogeneous hydrogenation catalysts in the aforesaid reactions is the co-production of unwanted alkanes, e.g. methane and ethane, by side-reactions, thereby decreasing the selectivity to desirable products. We have now found that the problem of alkane formation can be reduced by the use of alloyed catalysts. Accordingly, in one aspect the present invention provides a process for the production from either a carboxylic acid or an anhydride thereof of the corresponding alcohol and/or carboxylic acid ester which process comprises reacting the carboxylic acid or anhydride thereof with hydrogen at elevated temperature in the presence as catalyst of a composition comprising an alloy of (i) at least one noble metal of Group VIII of the Periodic Table of the Elements, and (ii) at least one metal capable of alloying with the aforesaid Group VIII noble metal. Hydrogen is commercially available on a large scale and may be used with or without further purification. A desirable purification may be removal of carbon monoxide. The process of the invention is applicable to both carboxylic acids and carboxylic acid anhydrides. The carboxylic acid or carboxylic acid anhydride may be saturated or unsaturated. Mono-, di- or polybasic acids and their anhydride derivatives may be employed. Suitably the carboxylic acid or anhydride may contain from 2 to 12 carbon atoms. Suitable monobasic acids include acids having the formula R-COOH wherein R is a substituted or unsubstituted aliphatic, aromatic or araliphatic group, which acids are hydrogenated to alcohols of the formula RCH₂OH. Suitably the group R may be a C₂ to C₁₂ alkyl group. Examples of suitable monobasic acids include acetic acid, propionic acid, butyric acid and heptanoic acid. A preferred monobasic acid is acetic acid. As regards the catalyst composition, the noble metals of Group VIII of the Periodic Table of the Elements are palladium, platinum, rhodium, ruthenium, osmium and iridium. Of the aforesaid noble metals, palladium, rhodium and ruthenium are preferred. Metals capable of alloying with palladium include silver, gold, copper, nickel, rhodium tin, cobalt, aluminium, manganese, gallium, iron, chromium and platinum, of which silver, gold and copper are preferred, silver being more preferred. Metals capable of alloying with ruthenium include iron, cobalt, manganese, germanium and rhenium. Although a catalyst composition comprising an alloy of (i) at least one noble metal of Group VIII of the Periodic Table of the Elements, and (ii) at least one metal capable of alloying with the aforesaid Group VIII noble metal (hereinafter to be designated component (A)) and incorporating at least one of the metals rhenium, tungsten or molybdenum (as component (B)) may be used as catalyst in the hydrogenation of monobasic carboxylic acids, it is preferred to employ a catalyst incorporating a support (as component (C)). Suitable supports include high surface area graphitised (HSAG) carbons, graphites, activated carbons, silicas, aluminas and silica/aluminas, of which HSAG carbons and high surface area silicas are preferred. Particularly suitable supports are the high surface area graphitised carbons described in GB-A-2136704 which may be in powder or pellet form. The carbon is preferably in particulate form e.g. as pellets. The size of the carbon particles will depend on the type of reactor used. The carbons are porous carbons. Carbons may be characterised by their BET, basal plane, and edge surface areas. The BET surface area is the surface area determined by nitrogen adsorption using the method of Brunauer Emmett and Teller J. Am. Chem. Soc. 60,309 (1938). The basal plane surface area is the surface area determined from the heat of adsorption on the carbon of n-dotriacontane from n-heptane by the method described in Proc. Roy. Soc. A314 pages 473 - 498, with particular reference to page 489. The edge surface area is the surface area determined from the heat of adsorption on the carbon of n-butanol from n-heptane as disclosed in the Proc. Roy. Soc. article mentioned above with particular reference to page 495. The carbons for use in the present invention have a BET surface area of at least 100 m²/g, more preferably at least 200 m²/g, most preferable at least 300 m²/g. The BET surface area is preferably not greater than 1000 m²/g, more preferably not greater than 750 m²/g. The ratio of BET to basal plane surface area is preferably not greater than 4:1, more preferably not greater than 2.5:1. It is particularly preferred to use carbons with ratios of BET to basal plane surface area of not greater than 1.5:1. It is preferred to use carbons with ratios of basal plane surface area to edge surface area of at least 10:1, preferably at least 50:1. It is not believed that there is an upper limit on the ratio, although in practice it will not usually exceed 200:1. The preferred carbon support may be prepared by heat treating a carbon-containing starting material. The starting material may be an oleophilic graphite e.g. prepared as disclosed in GB 1,168,785 or may be a carbon black. However, oleophilic graphites contain carbon in the form of very fine particles in flake form and are therefore not very suitable materials for use as catalyst supports. We prefer to avoid their use. Similar considerations apply to carbon black which also have a very fine particle size. The preferred materials are activated carbons derived from vegetable materials e.g. coconut charcoal, or from peat or coal or from carbonizable polymers. The materials subjected to the heat treatment preferably have particle sizes not less than those indicated above as being preferred for the carbon support. The preferred starting materials have the following characteristics: BET surface area of at least 100, more preferably at least 500 m²/g. The preferred heat treatment procedure for preparing carbon supports having the defined characteristics, comprise successively(1) heating the carbon in an inert atmosphere at a temperature of from 900°C to 3300°C, (2) oxidizing the carbon at a temperature between 300°C and 1200°C, (3) heating in an inert atmosphere at atemperature of between 900°C and 3000°C. The oxidation step is preferably carried out at temperatures between 300° and 600°C when oxygen (e.g. as air) is used as the oxidising agent. The duration of the heating in inert gas is not critical. The time needed to heat the carbon to the required maximum temperature is sufficient to produce the required changes in the carbon. The oxidation step must clearly not be carried out under conditions such that the carbon combusts completely. It is preferably carried out using a gaseous oxidizing agent fed at a controlled rate to avoid over oxidation. Examples of gaseous oxidising agents are steam, carbon dioxide, and gases containing molecular oxygen e.g. air. The oxidation is preferably carried out to give a carbon weight loss of at least 10% wt based on weight of carbon subjected to the oxidation step, more preferably at least 15% wt. The weight loss is preferably not greater than 40% wt of the carbon subjected to the oxidation step, more preferably not greater than 25% wt of the carbon. The rate of supply of oxidizing agent is preferably such that the desired weight loss takes place over at least 2 hours, more preferably at least 4 hours. Where an inert atmosphere is required it may be supplied by nitrogen or an inert gas. Preferred silica supports are those having a high surface area, typically greater than 50 m²/g. Suitably the catalyst composition comprises from 0.1 to 20% by weight, preferably from 1 to 10% by weight of component (A), from 0.1 to 20% by weight, preferably from 1 to 10% by weight of component (B), the remainder of the catalyst comprising a support. The catalyst composition may be further modified by incorporation of a metal or metals of Group IA or Group IIA. The alloy constituting component (A) of the catalyst composition of the present invention may be produced in any suitable manner, for example thermally or by a colloidal method. The component (A) may then be admixed with component (B). Components (A) and (B) may be applied to a support either individually or in combination by conventional means. A supported catalyst composition as hereinbefore described may suitably be produced by a process comprising the steps (i) depositing on a support at least one noble metal compound and a compound of at least one metal capable of forming an alloy with the Group VIII noble metal, said compounds being thermally decomposable/reducible to the metal, (ii) heating the composition obtained in step (i) under conditions and at a temperature such that the compounds are thermally decomposed/reduced to the metals and form an alloy thereof, and (iii) depositing on the composition obtained in step (ii) a compound of at least one of the metals rhenium, tungsten or molybdenum. A preferred process for producing a supported catalyst composition as hereinbefore described comprises the steps of: (I) impregnating a support with a solution or solutions of (i) at least one soluble Group VIII noble metal compound thermally decomposable/reducible to the noble metal and (ii) a soluble compound thermally decomposable/reducible to the metal of at least one metal capable of alloying with the Group VIII noble metal and removing the solvent therefrom, (II) heating the composition obtained in step (I) under conditions and at a temperature such that the compounds are thermally decomposed/reduced to the metals and form an alloy thereof, and (III) impregnating the composition obtained in step (II) with a compound of at least one of the metals rhenium, tungsten or molybdenum and removing the solvent therefrom. The solvent used in steps (I) and (III) of the process may be the same or different, preferably the same, and may be any suitable solvent, for example water. Techniques for impregnating supports with solutions of metal compounds and removing the solvent therefrom are well known in the art and require no further elaboration. Such techniques include the incipient wetness technique and the excess solution technique. In step (II) the composition may suitably be heated at a temperature above about 600°C to thermally decompose/reduce thermally decomposable/reducible compounds of the metals to the elemental metals and produce alloys thereof. This heating step may suitably be accomplished in the presence of an inert gas, for example nitrogen. Although about 600°C is indicative of the temperature at which palladium and silver must be heated to form the alloy, the optimum temperature will depend on the nature of the particular combination of metals involved. Preferably, a further step is interposed between step (I) and step (II) and optionally following step (III) wherein the impregnated support is dried, suitably by heating at a temperature in the range from 50 to 150°C. It will be appreciated by those skilled in the art that this step may be incorporated into step (II), if desired. Following step (III) there may be incorporated a further step (IV) wherein thermally decomposable/reducible compounds of at least one of the metals rhenium, tungsten or molybdenum is (are) thermally decomposed/reduced to the metallic form. Alternatively, this may be accomplished in a catalyst activation step. Suitable molybdenum, tungsten or rhenium compounds which are decomposable/reducible to the metal and/or oxide include salts of the metals and salts wherein the metals are present in the anionic moiety, for example, ammonium molybdate or ammonium tungstate. Suitable noble metal compounds which are decomposable/reducible to the noble metal include, for example, noble metal salts such as the carboxylates, halides and nitrates and ammonium salts containing the noble metal in the anion moiety, for example ammonium tetrachloropalladate. Suitable compounds of metals capable of alloying with a noble metal include salts of the metals, for example nitrates, carboxylates and halides. The metal of Group IA, Group IIA or Group IVA of the Periodic Table of the elements may be added to the catalyst composition at any point during its preparation. Thus, the supported alloy composition may be impregnated with a solution of a soluble compound of the metal. Alternatively, a soluble compound of the metal may be added to the impregnation solutions. A preferred catalyst comprises (i) an alloy of palladium and silver, and (ii) rhenium supported on a high surface area graphitised carbon of the type described in the aforesaid GB-A-2136704. Before use in the process of the invention the catalyst is preferably activated by contact at elevated temperature with either hydrogen or a hydrogen/inert gas, for example nitrogen mixture, suitably for a period of from 1 to 20 hours. The elevated temperature may suitably be in the range from 200 to 350°C. Alternatively, the catalyst may be activated by heating to the reaction temperature in the presence of reactants. Using monobasic acids the process of the invention may suitably be operated at an elevated temperature in the range from 100 to 300°C, preferably from 150 to 250°C. The pressure may suitably be less than 50 bar. The process may be operated in the liquid phase or the vapour phase. The process may be operated batchwise or continuously, preferably continuously. The catalyst may be employed in the form of a fixed bed, a moving bed or a fluidised bed. The Gas Hourly Space Velocity for continuous operation may suitably be in the range from 50 to 50,000 h⁻¹, preferably from 2,000 to 30,000 h⁻¹. In addition to the alcohol, the process of the invention generally also produces the corresponding ester as a by-product, for example the hydrogenation of acetic acid generally also produces ethyl acetate and the hydrogenation of propionic acid generally also produces propyl propionate. The proportion of the ester in the product will depend on the nature of the catalyst. The proportion of ester may be further increased, if desired, by feeding additional carboxylic acid and/or by introducing an acidic function into the catalyst to promote 'in situ' esterification. It is possible, therefore, to produce a product mainly comprising the carboxylic acid ester, particularly by operating in the liquid phase at low conversions, for-example less than 50%. It is an advantage of the process of the present invention that the selectivity of monobasic acid hydrogenation to desired products (alcohol/ester) can be increased at the expense of undesirable products (alkanes). The process of the present invention is particularly applicable to the hydrogenation of dicarboxylic acids and their anhydrides, more particularly to the hydrogenation of unsaturated dicarboxylic acids and their anhydrides. Examples of suitable dicarboxylic acids and their anhydrides include glutaric acid, glutaric anhydride, adipic acid, adipic anhydride, succinic acid, succinic anhydride, maleic acid and maleic anhydride. The hydrogenation of maleic acid or maleic anhydride to gamma-butyrolactone is generally difficult to accomplish because the gamma-butyrolacetone product generally reacts further with hydrogen to produce 1,4-butanediol and tetrahydrofuran. In addition to decreasing unwanted alkane production, the alloy catalysts of the present invention can also inhibit the further reaction of gamma-butyrolacetone to by-products, for example 1,4-butanediol and tetrahydrofuran. In another aspect therefore the present invention provides a process for the production of gamma-butyrolactone from either maleic acid or maleic anhydride which process comprises reacting either maleic acid or maleic anhydride at elevated temperature with hydrogen in the presence as catalyst of components (A) and (B) as hereinbefore described. Component (A) preferably comprises either palladium, ruthenium or rhodium, more preferably palladium as the noble metal (i) and either silver, gold or copper, more preferably silver, as the metal (ii) capable of alloying with palladium. A particularly preferred alloy is an alloy of palladium and silver. Components (A) and (B) may be used as catalyst either with or without the hereinbefore described component (C), though the presence of component (C), i.e. a support, is preferred. A preferred support is an HSAG carbon as hereinbefore described. The catalyst is preferably activated before use in rhe process by the method as hereinbefore described. The process may be operated batchwise or continuously and the maleic acid or anhydride may be introduced in either the liquid phase or the vapour phase. In the liquid phase it is preferred to use a solvent for the maleic anhydride. As the solvent there may be used either water or an inert organic solvent, for example 1,4-dioxane, water being a suitable solvent for maleic acid and 1,4-dioxane a suitable solvent for maleic anhydride. As regards the reaction conditions, the temperature may suitably be in the range from 50 to 350°C, preferably 150 to 300°C, and the pressure may suitably be in the range from 1x10⁵ to 3x10⁷ Pag (1 to 300 barg), preferably 1x10⁶ to 1.5x10⁷ Pag (10 to 150 barg). The Liquid Hourly Space Velocity (LHSV) for continuous operation may suitably be in the range from 0.05 to 10, preferably from 0.1 to 5. The gas to liquid ratio for liquid phase operation may suitably be in the range from 1:300, preferably from 1:100. In a final aspect the present invention provides a catalyst composition suitable for use in the hydrogenation of carboxylic acids and their anhydrides which composition comprises components (A) and (C) as hereinbefore described. The catalyst composition may suitably incorporate component (B) as hereinbefore described. A particularly preferred catalyst composition comprises an alloy of palladium and silver and an HSAG carbon as hereinbefore described, optionally incorporating also rhenium. The invention will now be further illustrated by reference to the following Examples and Comparison Tests. In the following Examples and Comparison Tests the term "HSAG carbon" denotes high surface area graphitised carbon, prepared and characterised as follows: The carbon used as support was prepared from a commercially available activated carbon sold by Ceca under the designation Acticarbone ACL40. The activated carbon was heat treated as follows. The carbon was heated from room temperature in a stream of nitrogen to 1700-1800°C over a period of about one hour. The temperature was held at 1700-1800°C for about twenty minutes then the carbon was cooled to room temperature. A water cooled heat exchanger was used to lower the temperature in a period of one hour. The carbon was then heated in air in a rotating kiln furnace at approximately 520°C for a time known from experience to give a weight loss of 20 %wt at a rate of less than 5% wt per hour. The carbon was then heated in nitrogen to between 1700°C and 1800°C and cooled to room temperature in a nitrogen atmosphere. The resulting graphite-containing carbon was then crushed to 1.003-0.5mm (16-30 mesh BSS). The resulting carbon had the following properties: BET surface area 628 m²/g Basal plane surface area 460 m²/g Edge surface area 8 m²/g BET/basal surface area ratio 1.36 m²/g Basal plane/edge surface area ratio 58 The carbon was then refluxed in 5% hydrochloric acid in aqueous solution for 2-3 hours, filtered and washed with distilled water. It was refluxed in distilled water for 2-3 hours, filtered and dried overnight in a vacuum oven at 100°C. CATALYST PREPARATION - PALLADIUM BASED CATALYSTS In the following procedures nominal loading is defined as weight of metal (not salt) added to the support expressed as a percentage of the weight of support. Example 1 An aqueous solution containing dissolved palladium nitrate and silver nitrate was added to HSAG carbon. The water was removed on a rotary evaporator, and the resulting impregnated carbon was then dried at 100°C in a vacuum overnight. The amounts of the various components were chosen to give a composition with a nominal loading as follows: 1.7% Ag, 2.5% Pd. The composition was then cooled and transferred to a glass tube, and was then heated in a stream of nitrogen using the following conditions: from room temperature to 600°C over a period of eight hours then eight hours at 600°C followed by cooling to room temperature in nitrogen. The resulting catalyst composition is designated Catalyst A. Example 2 Catalyst A was then mixed with an aqueous solution of rhenium heptoxide, the solvent again removed on a rotary evaporator, and the composition dried overnight in a vacuum oven at 100°C to give a catalyst of nominal loading - 1.7% Ag, 2.5% Pd, 5% Re. The resulting catalyst composition is designated Catalyst B. Comparison Test 1 The procedure of Example 1 was repeated except that silver nitrate was omitted from the preparation and the amounts of the various components were chosen to give a composition with a nominal loading as follows:- 2.5% Pd. A second difference was that the composition was heated in a stream of nitrogen using the following conditions: from room temperature to 300°C over a period of six hours, then ten hours at 300°C followed by cooling to room temperature in nitrogen. The resulting catalyst composition which is not according to the present invention is designated Catalyst C. Comparison Test 2 The procedure of Example 2 was repeated using catalyst C of Comparison Test 1 instead of Catalyst A to give a composition of the normal loading:- 2.5% Pd, 5% Re. The resulting catalyst composition which is not according to the present invention is designated Catalyst D. Comparison Test 2A Comparison Test 1 was repeated except that the composition was heated to 600°C instead of 300°C. Thereafter the procedure of Comparison Test 2 was followed to give a catalyst designated as Catalyst D1. Examples 3-6 A procedure similar to that described in Examples 1 and 2 was used to produce Ag/Pd/Re/HSAG catalysts having a range of silver loadings as follows:- Ex 3, Catalyst E - 0.8% Ag/2.5% Pd/5% Re/HSAG Ex 4, Catalyst F - 3.3% Ag/2.5% Pd/5% Re/HSAG and different Pd loadings as follows:- Ex 5, Catalyst G - 1.7% Ag/1.25% Pd/10% Re/HSAG Ex 6, Catalyst H - 1.7% Ag/1.25% Pd/10% Re/HSAG Details of the preparation procedures and the catalyst compositions are shown in Table 1. Examples 7-9 A procedure similar to that described in Examples 1 and 2 was used except that instead of silver nitrate there was used copper nitrate to produce Cu/Pd/Re/HSAG catalysts as follows:- Ex 7, Catalyst 1 - 0.6% Cu/2.5% Pd/5% Re/HSAG Ex 8, Catalyst J - 1.0% Cu/2.5% Pd/5% Re/HSAG Ex 9, Catalyst K - 0.5% Cu/1.25% Pd/10% Re/HSAG Details of the preparative procedures and the catalyst compositions are given in Table 1. Example 10 A procedure similar to that described in Examples 1 and 2 was used except that instead of silver nitrate there was used gold chloride to produce a catalyst (L) having the composition:- 1.7% Au/2.5% Pd/5% Re/HSAG Details of the preparative procedure and the composition are given in Table 1. Example 11 A procedure similar to that described in Examples 1 and 2 was used except that instead of silver nitrate there was used nickel nitrate to produce a catalyst (M) having the composition:- 0.5% Ni/2.5% Pd/5% Re/HSAG Details of the preparative procedure and the catalyst composition are given in Table 1. Comparison Test 3 The procedure of Comparison Test 2 was repeated except that the relevant proportions were altered to produce a catalyst (N) having the composition:- 1.25% Pd/10% Re/HSAG Details of the preparative procedure and the catalyst composition are given in Table 1. Alloy Catalyst Characterisation by X-Ray Diffraction The alloys were examined by X-ray diffraction (XRD), before rhenium impregnation to determine their stoichiometries and average crystallite sizes. The alloys and their constituents are all face-centred cubic structures and the alloys had lattice parameters between those of their parent elements. By using an internal standard to measure accurately the alloy latice parameter the composition can be estimated by interpolation assuming a linear relationship between composition and lattice parameters. In some catalysts the presence of several phases made it impossible to measure lattice parameters with sufficient accuracy to permit a composition analysis. The average crystallite size of the alloys was in the range observed for the palladium only catalysts. The data, together with catalyst compositions as measured by XRF is given in Table 2. Palladium/Silver Most of the palladium and silver became incorporated into an alloy and in all but one sample only one alloy was formed. The compositional information gained from XRD agreed moderately well with the composition measured by XRF. Palladium/Copper Some of the copper was 'invisible' to XRD suggesting that it was present as a highly dispersed or amorphous phase. The rest of the copper was incorporated into a palladium/copper alloy. One sample also contained a significant amount of palladium metal. Palladium/Gold This one sample contained a mixture of alloy compositions plus palladium metal. It suggests that more extreme conditions may be needed to promote better alloying and possibly a better catalyst. Palladium/Nickel It would appear that longer heating times and/or higher temperatures may be required to better promote the formation of nickel/palladium alloys. Palladium/Rhenium A catalyst similar in composition to catalyst D and prepared in a similar manner but differing only in the respect that the HSAG was heat treated differently and had slightly different properties was analysed by XRD. This catalyst contained only one crystalline phase-palladium metal with an average crystallite size greater than 1x10⁻⁸m (100 Angstoms). CATALYST TESTING (I) Hydrogenation of acetic acid For experiments at pressures in the range 1x10⁵-1.1x10⁶ Pag (1 - 11 barg), 2.5 mls of catalyst was loaded into a corrosion resistant stainless steel tube of internal diameter 6 - 7 mm, and the reactor tube assembly placed in a tubular furnace. The catalyst was then activated by heating at atmospheric pressure in a stream of hydrogen to either 280°C or 300°C over a two hour period, and then holding at the final temperature for one hour. After activation, the catalyst was cooled in hydrogen to the desired reaction temperature. A mixture of carboxylic acid vapour and hydrogen was then passed over the catalyst, and pressure was adjusted to the required value by means of a back-pressure regulator. The vapour/hydrogen mixture was formed in a vapourising zone, to which acetic acid liquid and hydrogen gas were separately metered. The product vapours and gases leaving the reactor were sampled on-line and analysed by gas-liquid chromatorgrapy (glc). The temperature was measured by means of a thermocouple inserted into the catalyst bed. The product mixtures typically contained the appropriate alcohol and ester (the latter formed by esterification of alcohol with unreacted acid), together with traces of the appropriate dialkyl ether, and aldehyde, and by-product methane, ethane and (with propionic acid only) propane. In general, with carbon and silica supported catalysts, the main product is alcohol, especially at high conversions. For the purposes of the Examples, conversions and selectivities have been calculated as respectively, the proportion of carboxylic acid hydrogenated, and the proportion of the hydrogenated carboxylic acid which is not converted into alkane by-product. Thus, selectivity denotes the ability of the catalyst to carry out hydrogenation without alkanation. In all examples (unless stated otherwise) only small amounts (<2%) of dialkyl ether and aldehyde are formed. DEFINITIONS WHSV = Weight Hourly Space Velocity = kg liquid feed per kg catalyst per hour. LHSV = Liquid Hourly Space Velocity = litres liquid feed per litre of catalyst per hour. Productivity to alkyls = kg acid converted to all products other than alkane by-products per kg catalyst per hour. Examples 12-15 Acetic acid was hydrogenated over the catalyst composition B of Example 2. The WHSV was ca 3.8 ( LHSV = 1.34 h-1 ), the ratio hydrogen to acetic acid was ca 10:1 molar, and the pressure was 1.03x10⁶ Pag (10.3 barg). In each case the catalyst was activated at 280°C. The results are collected in Table 3 and plotted in Figure 1. No deactivation was observed over run periods of up to 24 hours. COMPARISON TESTS 4-7 The procedure of Examples 2-5 was repeated except that catalyst composition D was used in place of catalyst compositin B. The results are collected in Table 3 and plotted in Figure 1. Example Catalyst Temperature °C Productivity to Alkyls (kg/kg/h) Selectivity (%) 12 B 249 1.69 91.4 13 B 231 0.98 94.5 14 B 215 0.69 95.7 15 B 194 0.37 97.0 Comp Test 4 D 251 1.70 86.5 Comp Test 5 D 232 1.07 91.7 Comp Test 6 D 217 0.80 93.5 Comp Test 7 D 196 0.43 95.6 The results show that alloying the palladium with silver increases the selectivity and slightly decreases the productivity to alkyls. D is included for comparison purposes and is not according to the present invention. The Figure shows the advantage to be gained by alloying the palladium with silver. By using the appropriate temperature the same productivity (P1) can be obtained at higher selectivity with B (S2 is greater than S1). Also a higher productivity can be obtained using B (P2 is greater than P1) at a constant selectivity (S2). Examples 16 to 19 The procedure of Examples 12 to 15 was repeated except that instead of Catalyst B of Example 2 there was used Catalyst E of Example 3. The results are presented in Table 4. Examples 20 to 23 The procedure of Examples 12 to 15 was repeated except that instead of Catalyst B of Example 2 there was used Catalyst F of Example 4. The results are presented in Table 4. Comparison Tests 8 to 11 The procedure of Examples 12 to 25 was repeated except that instead of Catalyst B of Example 2 there was used Catalyst D1 of Comparison Test 2A. The results are presented in Table 4. PALLADIUM/SILVER/RHENIUM/HSAG Catalyst Code Nominal Catalyst Composition Temperature °C Productivity to Ethyls (kg/kg/h) Selectivity (%) Ethyls Methane Ethane D 2.5% Pd/ 5% Re/HSAG 251 1.70 86.5 7.9 5.6 232 1.07 91.7 4.3 4.0 217 0.80 93.5 3.2 3.3 196 0.43 95.6 1.8 2.5 D1 2.5% Pd/ 5% Re/HSAG 250 1.96 87.2 6.5 6.2 231 1.14 92.2 3.7 4.2 220 0.83 93.8 2.7 3.5 195 0.43 95.7 1.7 2.7 E 0.8% Ag/ 2.5% Pd/ 5% Re/HSAG 249 1.82 88.7 5.4 5.9 231 1.18 92.7 3.1 4.2 213 0.78 94.6 2.2 3.3 191 0.37 96.2 1.4 2.5 B 1.7% Ag/ 2.5% Pd/ 5% Re/HSAG 249 1.69 91.4 3.6 5.1 231 0.98 94.5 1.9 3.6 215 0.69 95.7 1.4 2.9 194 0.37 97.0 0.8 2.2 F 3.3% Ag/ 2.5% Pd/ 5% Re/HSAG 251 1.77 90.2 4.5 5.3 231 1.01 94.2 2.3 3.5 218 0.78 95.2 1.8 3.1 196 0.41 96.7 1.0 2.3 The results provided in Table 4 are presented in graphical form in Figure 2. It can be seen from Figure 2 that adding silver as an alloy with palladium to the palladium/rhenium/HSAG catalyst shifts the productivity/selectivity 'operating line'. The improvements in catalyst performance can be taken in one of two ways, by choosing the appropriate operating temperature. At a productivity of 1kg/kg catalyst/h the selectivity of the catalyst can be improved from 92% to 94% by alloying with silver. Alternatively, at a selectivity of 92% the productivity can be improved from 1.0 to 1.6 kg/kg catalyst/h. In general there is more divergence from the operating lines, and hence more benefits from alloying, at higher temperatures, i.e. high productivities and low selectivities. Examples 24 to 27 The procedure of Examples 12 to 15 was repeated except that instead of Catalyst B of Example 2 there was used Catalyst I of Example 7. The results are presented in Table 5. Examples 28 to 31 The procedure of Examples 12 to 15 was repeated except that instead of Catalyst B of Example 2 there was used Catalyst J of Example 8. The results are presented in Table 5. Examples 32 to 35 The procedure of Examples 12 to 15 was repeated except that instead of Catalyst B of Example 2 there was used Catalyst L of Example 10. The results are presented in Table 5. Examples 36 to 39 The procedure of Examples 12 to 15 was repeated except that instead of Catalyst B of Example 2 there was used Catalyst M of Example 11. The results are presented in Table 5. PALLADIUM/COPPER (GOLD OR NICKEL)/RHENIUM/HSAG Catalyst Nominal Catalyst Composition Temperature (°C) Productivity to Ethyls (kg/kg/h) Selectivityg(%) Ethyls Methane Ethane D 2.5% Pd/ 5% Re/HSAG 251 1.70 86.5 7.9 5.6 232 1.07 91.7 4.3 4.0 217 0.80 93.5 3.2 3.3 196 0.43 95.6 1.8 2.5 I 0.6% Cu/ 2.5% Pd/ 5% Re/HSAG 248 1.53 89.6 5.7 4.8 230 0.86 93.9 2.8 3.2 218 0.64 95.3 2.1 2.6 204 0.34 96.9 1.1 2.0 J 1% Cu/ 2.5% Pd/ 5% Re/HSAG 245 1.04 92.7 2.8 3.6 230 0.72 94.7 1.9 3.4 212 0.43 96.0 1.3 2.8 191 0.22 96.9 0.8 2.3 L 1.7% Au/ 2.5% Pd/ 5% Re/HSAG 249 1.65 89.9 4.3 5.8 231 1.11 93.3 2.7 4.1 214 0.67 95.2 1.7 3.2 195 0.37 96.6 1.1 2.3 M 0.5% Ag/ 2.5% Pd/ 5% Re/HSAG 250 1.29 89.3 5.9 4.8 230 0.84 93.6 3.2 3.2 218 0.54 95.0 2.3 2.7 198 0.26 96.4 1.5 2.2 The results provided in Table 5 are presented in graphical form in Figure 3. It can be seen that in the case of copper the selectivity improvements were greater than for silver, the methane selectivity was reduced by at least 55% and ethane selectivity was reduced by 15% but the concomitant decrease in productivity was also greater. Thus, there was less overall benefit from alloying with copper compared with silver. It can been seen from Figure 3 that at a productivity of 1.0 kg/kg catalyst/h the selectivity improves from 92% to 93%. Gold behaves in a similar way to silver. Alloying with nickel increases the selectivity. Examples 40 to 43 The procedure of Examples 12 to 15 was repeated except that instead of Catalyst B of Example 2 there was used Catalyst G of Example 5. The results are presented in Table 6. Examples 44 to 47 The procedure of Examples 12 to 15 was repeated except that instead of Catalyst B of Example 2 there was used Catalyst H of Example 6. The results are presented in Table 6. Examples 48 to 51 The procedure of Examples 12 to 15 was repeated except that instead of Catalyst B of Example 2 there was used Catalyst K of Example 9. The results are presented in Table 6. Comparison Tests 12 to 15 The procedure of Examples 12 to 15 was repeated except that instead of Catalyst B of Example 2 there was used Catalyst N of Comparison Test 3. The results are presented in Table 6. THE EFFECT OF ALLOYING ON CATALYSTS WITH A LOW PALLADIUM LOADING (1.25%) AND A HIGH RHENIUM LOADING (10%) Catalyst Nominal Catalyst Composition Temperature (°C) Productivity to Ethyls (kg/kg/h) Selectivityg(%) Ethyls Methane Ethane E 1.25% Pd/ 10% Re/HSAG 246 2.34 90.8 3.8 5.0 231 1.65 93.6 2.2 4.1 212 1.01 95.4 1.5 3.2 190 0.54 96.7 0.8 2.5 G 1.7% Ag/ 1.25% Pd/ 10% Re/HSAG 251 2.52 90.1 3.0 7.0 231 1.64 94.0 1.6 4.4 214 1.09 95.6 1.1 3.3 196 0.52 96.8 0.7 2.5 H 1.7% Ag/ 1.25% Pd/ 10% Re/HSAG 253 2.36 89.6 3.3 7.2 230 1.43 93.7 1.7 4.7 212 0.97 95.3 1.2 3.7 191 0.49 96.7 0.8 2.6 K 0.5% Au/ 1.25% Pd/ 10% Re/HSAG 245 1.64 91.9 2.2 5.9 230 1.09 94.1 1.5 4.4 212 0.64 95.7 1.0 3.3 190 0.32 96.9 0.7 2.4 (II) Hydrogenation of maleic acid and maleic anhydride Catalyst Preparation Hereinafter nominal loading is defined as weight of metal (not salt) added to the support expressed as a percentage of the weight of support. Comparison Test 16 - Catalyst P An aqueous solution containing dissolved palladium nitrate was added to HSAG. The water was removed on a rotary evaporator, and the resulting impregnated carbon was dried at 150°C in an oven overnight. The amount of palladium nitrate was chosen to give a nominal loading of 3% Pd. The catalyst was then cooled and transferred to a glass tube, and was heated in a stream of nitrogen using the following conditions: from room temperature to 300°C over a period of eight hours then eight hours at 300°C followed by cooling to room temperature in nitrogen. This composition was then mixed with an aqueous solution of rhenium heptoxide, the solvent again removed on a rotary evaporator, and the composition dried overnight in an oven at 150°C to give a catalyst of nominal loading -3% Pd -3% Re. Example 52 - Catalyst Q The procedure of Comparison Test 16 was repeated except that silver nitrate was added to the solution of palladium nitrate. The amounts of the various components were chosen to give a composition with nominal loadings as follows 1.54% Ag, 3% Pd, 3% Re. A second difference was that the composition before the addition of rhenium was heated in a stream of nitrogen using the following conditions: from room temperature to 600°C over a period of eight hours, then eight hours at 600°C followed by cooling to room temperature in nitrogen. Example 53 - Catalyst R The procedure of Example 52 was repeated to give a composition of nominal loading : 3% Pd - 3.07% Ag - 3% Re. Example 54 - Catalyst S The procedure of Example 52 was repeated to give a composition of nominal loading 3% Pd - 6.14 Ag - 3% Re. Catalyst Testing i) General Method Batch Reactions Comparison Test 17 and 18 and Examples 55 to 60 A 300 ml stainless steel autoclave was purged with nitrogen and then charged with catalyst (usually 1.0g) and appropriate solution. For the anhydride hydrogenation this consisted of 20g maleic anhydride dissolved in 120g 1,4-dioxane. For maleic acid hydrogenation this consisted of 20g maleic anhydride in 120g de-ionised water. The autoclave was then purged using hydrogen and then pressurised to 8MPa (80 barg) with hydrogen. Heating and stirring was commenced (5°C/min, 1000 rpm) until 230°C was attained. This temperature was maintained for twelve hours with continued stirring. After this period the heating/stirring was ceased and the autoclave allowed to cool to room temperature. Gas and liquid phases were sampled and analysed by gas-liquid chromatography. Results are given in Tables 7 and 8. ii) Continuous Studies Comparison Test 19 and Example 61 Continuous testing of catalysts for maleic acid hydrogenation (13 wt % maleic anhydride in de-ionised water) was carried out using a 0.1 dm³ semi-technical unit. For experiments at 5MPa (725 psig), 100 mls of catalyst was loaded into a stainless steel reactor of internal diameter 25 mm which could be heated in three separate zones (top, catalyst bed, bottom). The catalyst was then activated by heating at 3.5MPa (500 psig) in a 50:50 stream of H₂:N₂ to 280°C, at a rate of 15°C/hr, and then holding for six hours. After activation, the catalyst was cooled in hydrogen to the desired reaction temperature. A mixture of maleic acid liquid and hydrogen was then passed over the catalyst, and pressure was adjusted to the required value by means of an air operated automatic pressure control valve. Catalyst performance was assessed by carrying out 10 hour mass balances preceded by 10 hour pre-runs to allow steady-state condition to be attained. Product vapours, gases and liquid were sampled, after gas/liquid separation, and analysed by off-line gas-liquid chromatography. The temperatures were measured by means of thermocouples inserted into the top, middle and bottom of the catalyst bed. Results are in Table 9. Comparison Test 20 The procedure of Examples 55 to 60 for maleic anhydride hydrogenation was repeated except that the catalyst was 3% Pd supported on alumina prepared in the manner of the 3% Pd/HSAG intermediate of Comparison Test 16. The results are presented in Table 10. Example 62 (Comparative) Comparison Test 20 was repeated except that instead of the 3% Pd/Al₂O₃ catalyst there was used a 3% Pd/6% Ag/Al₂O₃ catalyst, prepared in a similar manner (omitting rhenium) to catalyst Q of Example 52. The results are presented in Table 10. Example 63 Comparison Test 20 was repeated except that instead of the 3% Pd/Al₂O₃ catalyst there was used a 3% Pd/6% Ag/3% Re/Al₂O₃ catalyst prepared in the manner of catalyst Q of Example 52. The results are presented in Table 10. Example Productivity (kg/kgcat/h Selectivity to total C₄ Solvents (%) Selectivity (%) Total Conversion (%) Methane OH CT20 0.85 99.6 0.2 0.2 50 62 1.52 99.7 0.0 0.3 92 63 1.49 98.6 0.1 1.3 91 Comparison Test 21 The procedure of Examples 55 to 60 for maleic acid hydrogenation was repeated except that the catalyst was 3% Pd supported on alumina prepared in similar manner to the 3% Pd/HSAG intermediate of Comparison Test 16. The results are presented in Table 11. Example 64 (Comparative) Comparison Test 21 was repeated except that instead of the 3% Pd/Al₂O₃ catalyst there was used a 3% Pd/6% Ag/Al₂O₃ catalyst prepared in a similar manner (omitting rhenium) to catalyst Q of Example 52. The results are presented in Table 11. Example 65 Comparison Test 21 was repeated except that instead of the 3% Pd/Al₂O₃ catalyst there was used a 3% Pd/6% Ag/3% Re/Al₂O₃ catalyst prepared in the manner of catalyst R of Example 53. The results are presented in Table 11. Example Productivity (kg/kgcat/h Selectivity to total C₄ Solvents (%) Selectivity (%) Total Conversion (%) Methane OH CT21 0.4 97.7 1.9 0.4 14+ 64 0.38 99.6 0.3 0.1 23 65 0.54 99.0 0.4 0.6 32 CATALYST PREPARATION - RUTHENIUM BASED CATALYSTS Comparison Test 22 - Catalyst T HSAG(5g) was impregnated with Ru(NO)(NO₃) solution (7.3 wt% Ru)(1.61g) diluted to 50 ml with distilled water. The solution was rotary evaporated to dryness at 70°C and -8x10⁴ Pa (-800 mbar) pressure. The sample was then dried in a vacuum oven at 120°C for 16 hours prior to reduction at 300°C under a stream of flowing hydrogen at 100kPa (1 atm). pressure for 4 hours. The gas flow was switched to nitrogen and the catalyst allowed to cool under this gas. The now ruthenised graphite was impregnated with an aqueous solution (50ml) containing Re₂O₇ (0.65g) and evaporated to dryness at 70°C and -8x10⁴ Pa (-800 mbar) pressure prior to drying for 16 hours in a vacuum oven at 120°C. Nominal catalyst loading: 2.35 wt% Ru-5 wt% Re/HSAG Example 66 - Catalyst U HSAG (5g) was coimpregnated with Ru(NO)(CO₃)₃ solution (7.3 wt% Ru)(1.61g) and Fe(NO₃)₃.9H₂O(0.47g) in distilled water (100 ml). The solution was rotary evaporated to dryness and dried in a vacuum oven as for Catalyst T. The sample was then reduced as for Catalyst T however, on switching the gas flow to nitrogen the sample temperature was elevated to 800°C. The sample was allowed to cool under flowing nitrogen. Re₂O₇ was impregnated on to the sample in the same manner as for Catalyst T. Nominal catalyst loading:- 2.35 wt% Ru-1.3 wt% Fe-5 wt%Re/HSAG Example 67 - Catalyst V This catalyst was prepared in the same manner as Catalyst U except that CO(NO₃)₂. 6H₂O(0.30g) was used instead of Fe(NO₃)₃.9H₂O. Nominal catalyst loading:- 2.35 wt% Ru-1.2 wt% Co-5 wt% Re/HSAG Example 69 - Catalyst X This catalyst was prepared in the same manner as Catalyst V except that only 0.15g of the cobalt salt was used in the coimpregnation step with ruthenium. Nominal catalyst loading:- 2.35 wt% Ru-0.60 wt% Co-5 wt% Re/HSAG XRD Analysis of the Alloyed Catalysts All the samples examined showed unalloyed second metal (iron or cobalt) but none provided any evidence for the presence of unalloyed ruthenium. All the samples, i.e. catalysts U,V and X also showed significant amounts of unidentified crystalline material. Little information would appear to be available in the literature on XRD studies of Ru-Fe and Ru-Co alloys. However, since the ruthenium content of these catalysts, in atomic terms, is always at least equal to that of the second metal, it would appear likely that the unidentified material is a ruthenium rich Ru-Fe or Ru-Co alloy. Catalyst Testing Hydrogenation of acetic acid Procedure Reactions were carried out in a single pass plug flow microreactor employing a 2.5 ml catalyst charge. Total reactant pressure was maintained at 1x10⁶ Pag (10 barg). LHSV was approx 1.35 and the ratio of hydrogen to acetic acid was 10:1. Reaction products were analysed by gc employing both flame ionisation detection and thermal conductivity detection. Results were obtained at three different temperatures, viz. about 230°C, about 210°C and about 190°C. Comparison Test 23 Catalyst T was used in the procedure above. The results are given in Table 12. Examples 70-73 Catalysts U, V and X were used in the procedure above. The results are given in Table 12. Catalyst T U V X Actual Temp. (°C) 234 233 235 230 Conversion (%) 41.32 55.40 56.67 36.08 Sel. (CH₄) (%) 33.04 16.89 14.21 12.85 Sel. (C₂H₆) (%) 14.19 7.77 7.11 6.99 Sel. (EtOH) (%) 47.80 54.83 64.80 71.90 Sel. (EtOAc) (%) 4.34 18.03 13.28 7.45 Catalyst T U V X Actual Temp. (°C) 215 210 215 210 Conversion (%) 26.01 32.05 32.21 25.26 Sel. (CH₄) (%) 26.25 11.42 8.03 9.66 Sel. (C₂H₆) (%) 11.28 6.25 4.88 5.63 Sel. (EtOH) (%) 57.25 66.30 68.51 67.29 Sel. (EtOAc) (%) 4.81 11.45 18.19 15.72 Catalyst T U V X Actual Temp. (°C) 194 191 192 192 Conversion (%) 14.45 19.99 13.52 14.91 Sel. (CH₄) (%) 18.79 7.80 6.40 5.61 Sel. (C₂H₆) (%) 8.96 4.87 4.79 4.05 Sel. (EtOH) (%) 66.83 72.02 77.01 63.85 Sel. (EtOAC) (%) 4.91 9.67 10.58 23.74

Claims: A catalyst composition comprising a component (A) comprising an alloy of (i) at least one noble metal of Group VIII of the Periodic Table of the elements and (ii) at least one metal capable of alloying with the aforesaid Group VIII noble metal and a component (B) comprising at least one of the metals rhenium, tungsten and molybdenum. A catalyst composition as claimed in claim 1 in which the at least one noble metal comprises at least one of palladium, rhodium and ruthenium. A catalyst composition as claimed in claim 2 in which the noble metal comprises palladium and the at least one metal capable of alloying with the noble metal comprising at least one of silver, gold and copper. A catalyst composition as claimed in claim 3 in which the metal capable of alloying with the noble metal comprises silver. A catalyst composition as claimed in any one of the preceding claims in which the composition further incorporates a support component (C) comprising a high surface area graphitised (HSAG) carbon, a graphite, an activated carbon, a silica, an alumina, or a silica/alumina. A catalyst composition as claimed in claim 5 in which the support component (C) comprises a high surface area graphitised (HSAG) carbon, a graphite or an activated carbon. A catalyst composition as claimed in any one of the preceeding claims further comprising a metal or metals of Group IA or Group IIA of the Periodic Table of Elements. A catalyst composition as claimed in any one of claims 5 to 7 in which the high surface area graphitised (HSAG) carbon has a BET surface area of at least 300 m²/g; a ratio of BET to basal plane surface area of not greater than 4:1; and a ratio of basal plane surface area to edge surface area of at least 10:1; said graphitised carbon having been prepared by the successive steps of (1) heating a carbon material in an inert atmosphere at a temperature of from 900 to 3300°C, (2) oxidising the carbon at a temperature of between 300°C and 1200°C and (3) heating in an inert atmosphere at a temperature of between 900°C and 3000°C. A catalyst composition as claimed in claim 8 in which the BET surface area of the high surface area graphitised carbon support is not greater than 1000 m²/g. A catalyst composition as claimed in claim 8 or claim 9 in which the ratio of BET to basal plane surface area is not greater than 2.5:1. A catalyst composition as claimed in any one of claims 8 to 10 in which the ratio of basal surface area to edge surface area is at least 50:1. A catalyst composition as claimed in any one of claims 8 to 11 in which the ratio of basal plane surface area to edge surface area does not exceed 200:1. A catalyst composition as claimed in any one of claims 8 to 12 in which in the step (2) of the preparation of the high surface area graphitised carbon support, the weight loss of carbon is at least 10% and not greater than 40%. A process for preparing a catalyst composition as claimed in claim 5 or claim 6 which comprises the steps of: (I) impregnating a support with a solution or solutions of (i) at least one soluble Group VIII noble metal compound thermally decomposable/reducible to the noble metal and (ii) a soluble compound thermally decomposable/reducible to the metal of at least one metal capable of alloying with the Group VIII noble metal and removing the solvent therefrom, (II) heating the composition obtained in step (I) under conditions and at a temperature such that the compounds are thermally decomposed/reduced to the metals and form an alloy thereof, and (III) impregnating the composition obtained in step (II) with a compound of at least one of the metals rhenium, tungsten or molybdenum and removing the solvent therefrom.

Inventors: KITSON MELANIE, WILLIAMS PETER SEFTON, KITSON, MELANIE, WILLIAMS, PETER SEFTON
Applicants: BP CHEM INT LTD, BRITISH PETROLEUM CO PLC, BP CHEMICALS LIMITED, THE BRITISH PETROLEUM COMPANY P.L.C.
Application year: 1988
Main classification: B01J23
IPC codes: B01J23, C07C29