GB1601121A

GB1601121A - Production of acid anhydrides by oxidation and catalysts therefor

Info

Publication number: GB1601121A
Application number: GB21610/77A
Authority: GB
Original assignee: Imperial Chemical Industries Ltd
Current assignee: Imperial Chemical Industries Ltd
Priority date: 1977-05-23
Filing date: 1977-05-23
Publication date: 1981-10-28
Also published as: BE867189A; ZA782940B; JPH0242537B2; JPS62258746A

Description

(54) PRODUCTION OF ACID ANHYDRIDES BY OXIDATION AND CATALYSTS THEREFOR (71) We, IMPERIAL CHEMICAL INDUSTRIES LIMITED, Imperial Chemical House, Millbank, London SW1P 3JF, a British Company do hereby declare the invention for which we pray that a patent may be granted to us, and the method by which it is to be performed, to be particularly described in and by the following statement: This invention relates to the production of acid anhydrides especially maleic anhydride and catalysts therefor.

It is known to produce maleic anhydride by oxidising hydrocarbons, for example benzene or hydrocarbons having the formula R'-CH2-CH-CH2-CH2R" ' where R' and R" are individually hydrogen or alkyl groups, R' and R" having together at most six and preferably at most four carbon atoms, or cyclo-alkanes having a -CH-CH2-CH2-CH- group, preferably in a ring, for example cyclohexane. Mixtures of hydrocarbons, for example naphtha, may be used but n-butane is a preferred feedstock. n-Butenes may be used. The hydrocarbon is generally oxidised by contacting it in the vapour phase together with oxygen with a solid catalyst and recovering maleic anhydride from the product. Oxygen may be provided in the form of air by mixing the hydrocarbon in a concentration generally, except in the case of fluidised bed processes, lower than the lower explosive limit with air and contacting the mixture with the catalyst under appropriate conditions of temperature and pressure (the "fuel lean" system). In this case the product gas, after recovery of maleic anhydride, is usually vented or burned. The oxidation may also be carried out as disclosed in German Offenlegunschrift 2.412,913 by mixing the hydrocarbon with air in a concentration higher than the upper explosive limit, contacting it with a catalyst under appropriate conditions of temperature and pressure and recovering maleic anhydride from the product gas (i.e. a "fuel rich" system). It is possible to operate within the explosive limits using a fluidised bed reactor.

It is important that the catalyst should have a high selectivity, that is that the yield of maleic anhvdride should be as high as possible based on the hydrocarbon consumed in the process. In processes in which the product gas after recovery of maleic anhydride is vented or burned it is important, therefore, that the pass yield should be high, i.e. that the proportion of the hydrocarbon converted to maleic anhydride on a single pass should be as high as possible. If any unconverted hydrocarbon is recycled it is desirable that a high pass yield should be achieved in order to avoid recycling an unduly high proportion of the hydrocarbon but the selectivity in terms of the yield of maleic anhydride based on the hydrocarbon consumed in each pass is relatively more important.

It is an object of this invention to provide catalysts for the oxidation of hydrocarbons to maleic anhydride which possess an acceptable selectivity as judged in the case of a "fuel lean" system by the pass yields obtainable with them under suitable conditions and in the case of a "fuel rich" system by the selectivities based on the hydrocarbon consumed at an acceptable conversion under suitable conditions.

Catalysts for the oxidation of hydrocarbons to maleic anhydride have been made by reacting a vanadium compound with phosphoric acid in an acid solution, evaporating to dryness to give a vanadium/phosphorus mixed oxide catalyst precursor and activating the catalyst by heat treatment. The solution may be an aqueous solution as disclosed for example in British Patent No. 1,409.094 or a solution in an organic solvent for example as described in British Patent No. 1,416,099.

The catalyst precursor may alternatively be precipitated by the addition of water to the vanadium/phosphoric acid solution under controlled conditions for example as described in South African Patent Application No. 41 of 1976. The latter technique however is difficult to control and requires an extra filtration stage as compared with a process for producing the precursor which merely involves evaporating the precursor solution. Evaporation of the precursor solution however tends to produce a mixture of compounds and phases and on activation the catalyst tends to have a low surface area. We have found that one material which is present and is deleterious is that identified by G. Ladwig in Z. Chem. 1968 Vol. 8, pages 307 & 308 as a hydrogen phosphate without strong H-bonding of formula VO (H2PO4)2, which is herein referred to as phase E.

This invention provides a process for producing a catalyst for the production of acid anhydrides especially maleic anhydride which comprises reacting a vanadium compound with phosphoric acid, producing a solid vanadium/phosphorus mixed oxide catalyst precursor, contacting the solid precursor with an acid stronger than H3PO4 (judged in terms of its first dissociation constant in water), which is preferably non-oxidising, at a concentration of at least 3N and preferably at least 5N, preferably in an aqueous solution, recovering the precursor and extracting it with water or with another solvent for phase E for example dimethyl sulphoxide until substantially only material insoluble in water or the said solvent is left, separating the precursor and producing a phase transition to a catalytically active form by heating it.

The precursor may dissolve in the strong acid and be recovered from it by distilling the strong acid from it.

The phase transition occurs at the temperatures normally encountered in the production of the acid anhydrides, and thus it may not be necessary to carry it out before use. If desired the phase transition may be carried out before use by heating to a temperature of for example 340 to 500"C.

The process may suitably be carried out by reacting the vanadium compound with phosphoric acid in an acidic solution which is suitably an aqueous acidic solution and precipitating a vanadium/phsophorus mixed oxide catalyst precursor by removing solvent, preferably at least 90% and more preferably at least 95% of the solvent being removed, preferably leaving a dry or nearly dry solid, which is during this procedure or subsequently put in contact with the acid stronger than phosphoric acid at a concentration of at least 3N.

The catalytically active form of the catalyst normally comprises the beta form (phase B).

The characteristics of the beta form are disclosed in U.S. Patent No. 3864280. The beta form is readily produced from the B' form which may also be present and is believed to be an oxidised equivalent of the beta form. It is further identified in Example 2.

We have found that catalysts produced according to the above process commonly contain a vanadium/phosphorus mixed oxide of the type described as phase X. In a paper by Jordan & Calvo, Canadian Journal of Chemistry 51 2621-5, 1973 the isolation of individual crystals of phase X from a substantially amorphous mass and identification of the X-ray diffraction characteristics of phase X is described.

Catalysts produced in accordance with this invention unlike the product disclosed by Jordan & Calvo possess a high surface area. We have found that in a high surface area catalyst the presence of phase X increases the catalytic effectiveness by conferring on the catalyst attractive activities and selectivities in the oxidation of hydrocarbons to maleic anhydride.

We believe that the proportion of phase X in the catalytically active form is increased by contact of the catalyst precursor with a highly acidic medium at an elevated temperature which is preferably at least 500C and more preferably at least 80"C for example up to 250 and preferably up to 1500C. Thus if for example the vanadium/phosphorus mixed oxide catalyst precursor is precipitated by evaporation of a solution containing a volatile acid, for example one boiling in the above range at atmospheric pressure, for example aqueous HBr or preferably HCI, to dryness as previously described there is a tendency to produce a high phase X content in the catalytic form eventually produced therefrom.

We also believe that a thorough separation of phase E and any other phases coincidentally removed from the catalyst precursor as aforesaid increases the phase X content of the catalytically active form. It is also believed that extracting the precursor in water or the aforesaid solvent by removing unwanted phases increases the surface area of the catalytically active form.

The invention therefore also comprises a catalyst for the oxidation of hydrocarbons to acid anhydrides especially maleic anhydride which comprise at least 40% and preferably at least 50% by weight of phase X, the catalyst having a surface area of at least 7 square metres per gram and preferably at least 10 square metres per gram. The phase X content may be estimated from the integrated intensity of its characteristic lines in an X-ray diffraction pattern. If desired an internal standard may be used in such estimations.

It is preferred that the catalyst should contain less than 15% and more preferably less than 10% of amorphous vanadium/phosphorus mixed oxides. It is also preferred that if the catalyst contains vanadium/phosphorus mixed oxides other than as phase X, they should be at least partly present as phase B or B'.

If desired a catalyst promoter may be incorporated in the catalyst. Such a promoter may be tungsten, nickel, cadmium, zinc, bismuth, lithium, copper, uranium, zirconium, hafnium, chromium, iron, manganese, molybdenum and/or preferably cobalt and/or a rare earth promoter for example cerium or more preferably lanthanum, the atomic ratio of the promoter to vanadium being preferably in the range 0.0015:1 to 1:1. The promoter may be incorporated in the catalyst by including a suitable compound in the solution from which the vanadium/phosphorus mixed oxide is precipitated or may be introduced to the precursor immediately after precipitation, after boiling or after activation of the catalyst suitably by physical admixture or preferably by impregnating the solid with a solution of a suitable compound of the promoter and drying the impregnated solid. Vanadium/phosphorus mixed oxide catalysts having surface areas greater than 10, more preferably greater than 15m2/gram promoted with rare earth metal promoters especially lanthanum and/or cerium are believed to be novel.

The atomic ratio of vanadium to phsophorus is preferably in the range 0.5:1 to 2:1, and is preferably in the range 1:0.8 to 1:1.7.

It is preferred that the surface area of the catalyst should be at least 10 m2/g after the phase transition and it is more preferably at least 15 m2/g for example in the range 10 or 15 to 50 m2/g. Preferably the surface area does not exceed 150 m2/g and more preferably it is 970mug.

The vanadium compound may be introduced to the solution by dissolving for example vanadium pentoxide, vanadium-sesqui-oxide, a vanadyl halide for example VOCl2, a vanadium oxytrihalide, a vanadium-oxydihalide, vanadyl sulphate or vanadium (V) phosphate in the solvent. Preferably an acid stronger than phosphoric acid is present for example hydrochloric, hydrobromic. sulphuric or nitric acid. Such acids may be formed in situ from anions present in the vanadium compound or for example by hydrolysis of phosphorus oxytrihalides. The phosphoric acid may be supplied as ortho-phosphoric acid or its metal salts for example sodium di-hydrogen phosphate, as monofluoro phosphoric acid, phosphorus pentoxide. a phosphorus oxytrihalide or as a condensed phosphorus acid for example pyrophosphoric acid or tripolyphosphoric acid. Such acids are converted to phosphoric acid if for example water is present. If desired a reducing agent for example oxalic, formic, citric or other reducing carboxylic acid may be added to reduce vanadium (V) to vanadium (IV).

Suitably the catalyst may be treated with a suspension of an inert support for example an alumina, silicon carbide, Kieselguhr, pumice or preferably silica support. A suitable coloidal silica sol is for example the material supplied under the trademark "LUDOX" by E I Du Pont de Nemours & Co. Such supports may be incorporated into the catalyst or into the precursor, or the precursor may be formed from a solution incorporating such supports.

The surface area of the catalyst excluding the reinforcement or support may be determined directly when the catalyst is prepared first and the reinforcement or support is added subsequently. If the catalyst is formed on a reinforcement or support however the surface area of the catalyst according to this invention is defined as that which is possessed by a catalyst identically prepared but in the absence of the reinforcement or support.

The solution from which the precursor is obtained is preferably an aqueous solution but may if desired comprise also an organic solvent for example isobutanol or tetrahydrofuran.

Preferably at least 1 gram molecule of water per gram atom of vanadium is present. Suitably the solvent is water only.

If desired catalysts may be prepared according to the invention by reacting a compound of vanadium with phosphoric acid preferably in the presence of a suitable solvent, for example water and/or a lower alcohol for example methanol, to produce a form of alpha VOPO4 which is then conditioned in the presence of a strong acid for example hydrochloric acid at elevated temperatures as aforesaid. The conditioned precipitate may then be extracted with water or another solvent for phase E and converted to a catalytically active form by heating until a phase transition occurs as aforesaid.

The invention also comprises a process of oxidising a hydrocarbon as aforesaid to maleic anhydride by contacting it in the presence of oxygen with a catalyst as aforesaid. It is preferred to carry out the process using n-butane as the hydrocarbon and it is suitably fed to the catalyst in a concentration of 0.5 - 1.5% by volume in air to a fixed or fluidised bed of the catalyst. The oxidation is preferably carried out at a temperature in the range 250 - 600"C and more preferably 300 - 450"C. The reaction may be carried out at a pressure of 0.5 to 20 atmospheres absolute and is more preferably carried out at a pressure in the range 1-3 atmospheres.

The invention also comprises a process in which phthalic anhydride is produced by oxidising orthoxylene or naphthalene with oxygen in the presence of a catalyst according to the invention.

Example 1 - Comparative Example Vanadium pentoxide (60.6g) and concentrated aqueous hydrochloric acid (790 mls) were heated with stirring for about 2 hours to give a dark blue solution. To this solution orthophosphoric acid (88%,89.1g) was added and the resulting solution was refluxed for a further period of about 2 hours. The solution was then evaporated to dryness and the resulting solid was dried in an oven at 110 C. The P:V ratio of this catalyst precursor was 1.2:1. A portion of this dried solid was mixed with a pelletting agent sold under the trade name "Sterotex" (2% by wt) and pelletised under a pressure of 17 tons. The pellet was then crushed and sieved to give particles 500-710y in size and a 5.0 mls portion was charged to a tubular fixed bed reactor. The catalyst was then calcined in situ by heating to 385"C at a rate of 3"cumin whilst 1.5% n butane by volume in air flowed through the bed at a gas hourly space velocity of 1000 hi". After 100 hrs the temperature was raised to 450"C for 1 hour and then lowered to 425"C. After calcination, at a reactor temperature of 425"C, at atmospheric pressure and GHSV of 500 hrs~' of a mixture of 1.5% by volume n-butane in air the catalyst gave 20% molar pass yield of maleic anhydride at a butane conversion of 34%.

At a reactor temperature of 385 C, atmospheric pressure and GHSV of 500 hr~l the catalyst gave a 9% molar pass yield of maleic anhydride at a butane conversion of 13%. At a reactor temperature of 385"C, atmospheric pressure and GHSV of 1000 hr1 the catalyst gave a 6% molar pass yield of maleic anhydride at a butane conversion of 11%. The surface area of the final catalyst was 3m2/g.

A sample of the final catalyst was examined by X-ray diffractometry and was found to contain mainly the Beta phase as disclosed in the U.S. patent No. 3985775. The final catalyst was found to contain less than 5% phase X.

Example 2 Vanadium pentoxide (60.6g) and concentrated aqueous hydrochloric acid (790 mls) were heated with stirring for about 2 hours to give a dark blue solution. To this solution orthophosphoric acid (89.1 g, 88%) was added and the resulting solution was refluxed for a further period of about two hours. The solution was then evaporated to dryness and the resulting solid was dried in an air oven at 110 . The P:V atomic ratio of this catalyst precursor was 1.2:1. The resulting solid was then boiled with water (20 mls/g. solid) for about 1 hour and filtered hot, washed with a small amount of warm water and dried at llO"C. A portion of the dried solid was mixed with a pelletting agent sold under the trade name "Sterotex" (3% by wt) and pelletised to 17 tons. The pellet was then crushed and sieved to give particles 500 - 71011in size and a 5.0 ml portion was charged to a tubular fixed bed reactor. The catalyst was then calcined in situ by the procedure detailed in example 1.

After calcination, the catalyst gave a molar pass yield of 48% at a butane conversion of 75% at a reactor temperature of 420"C and a GHSV of 600 hr~l of 1.5% n-butane by volume in air at atmospheric pressure. At a reactor temperature of 385"C and GHSV of 600 hf' the catalyst gave a 33% molar pass yield at a butane conversion of 45%. The surface area of the final catalyst was 9 m2/g-. A sample of the final catalyst was examined by X-ray diffractometry and in addition to the X-ray powder diffraction pattern of the beta phase it was found that the characteristic X-ray powder diffraction pattern of phase X and phase B'(which are listed in tables 1 and 2 respectively) were present.

By analysis of the peak areas of the diffracted reflections of the beta phase, phase X and phase B', it was found that 40% phase X was present in the catalyst.

TABLE 1 X-ray powder diffraction of phase X d(A) spavins were obtained using CuKa radiation. Only lines from spacings between 4.44 and 1.83 were measured.

20 d ( ) Relative * Intensity 20.0 4.44 < 1 21.0 4.24 < 1 24.9 3.57 6 29.1 3.07 5 29.8 3.00 10 39.2 2.30 < 1 40.7 2.22 < 1 42.7 2.12 < 1 46.1 1.97 1 47.9 1.90 1 49.9 1.83 1.5 Intensities are normalised to reflection at 20 = 29.8 being 10 TABLE 2 X-ray powder diffraction pattern of phase B' (or Y) d (A) spacings were obtained using CuKa radiation Only lines from spacings between 4.58 A and 2.96 A were measured. d ( ) Relative Intensity 4.58 3 4.02 10 3.66 2 3.12 6.5 2.96 Intensities are normalised to the intensity of d= 4.02 being 10.

Example 3 Vanadium pentoxide (60.6g) and concentrated aqueous hydrochloric acid (790 mls) were heated with stirring for about 2 hrs to give a dark blue solution. To this solution orthophosphoric acid (88%, 89.1g) was added and the resulting solution was refluxed for a further period of about two hours. The solution was then evaporated by disttillation to about 200 mls. 200 mls of concentrated aqueous hydrochloric acid were added, the resulting solution was refluxed for a further period of 1 hour and then the solution was evaporated to dryness and the resulting solid was dried in an air oven at 1100C. The P:V ratio of this catalyst precursor was 1.2:1. The resulting solid was then boiled with water (20 mls/g. solid) for about 1 hour and the resulting blue suspension was filtered hot, washed with a small amount of warm water and dried at 1500C. A portion of the dried solid was mixed with a pelletting agent sold under the trade name "Sterotex" (2% by weight) and pelletised under a pressure of 17 tons. The pellet was then crushed and sieved to give particles 500 - 71011 in size and a 5.0 ml portion was charged to a tubular fixed bed reactor. The catalyst was then calcined in situ by the procedure detailed in example 1. After calcination, the catalyst gave a molar pass yield of 58.5% at a butane conversion of 94% at a reactor temperature of 405"C and a GHSV of 642 hr~l of 1.5% n-butane by volume in air at atmospheric pressure.

At a reactor temperature of 385"C and GHSV of 615 hr~l the catalyst gave a 53% molar pass yield at a butane conversion of 796sic. At a reactor temperature of 420"C and a GHSV of 2000 hr~l of 1.5CHo n-butane in air at atmospheric pressure the catalyst gave 43% molar pass yield of maleic anhydride at a n-butane conversion of 72%. The surface area of the final catalyst was 10 m2/g. A sample of the final catalyst was examined by X-ray diffract ometry and the characteristic X-ray powder diffraction patterns of phase X and phase B' were observed in addition to the X-ray powder diffraction pattern of the beta phase. It was found that 52% phase X was present in the final catalyst.

Example 4 Part A A sample of phase E as described by Ladwig (Z.Chem. 1968 vol. 8 pages 307 & 308) was prepared by the following method. Vanadium oxydichloride (29g) and orthophosphoric acid (100%, 65.5g) were refluxed in aqueous ethanol for 1 hour. Part of the solvent was then removed by distillation and the blue-green precipitate was collected by filtration and dried at 1100C for 7 hours. The sample was examined by X-ray diffractometry and was found to exhibit the X-ray spectrum characteristic of phase E as given in Table 3. The sample was then examined by differential thermal analysis (D.T.A.) and was found to exhibit one endothermic transition between 365"C and 425"C.

Part B A sample of a vanadium phosphorus catalyst precursor was prepared as described in Example 1 and this was examined by X-ray diffractometry and was found to contain the X-ray spectrum characteristic of phase E as given in table 1. It was determined by this means that 10% by weight of phase E was present in the catalyst precursor. The catalyst precursor was examined by D.T.A. and was found to exhibit two endothermic transitions, one between 365"C and 420"C and one between 425"C and 485"C. This catalyst precursor gave on pretreatment a final catalyst with a poor performance typical of that exemplified in Example 1.

TABLE 3 d (Angstrom) 20 (degrees) Relative* (d Angstrom) 20 (degrees) Relative* Intensity Intensity 6.34 14.0 100 2.37 37.9 5 4.49 19.8 5 2.10 43.1 34 3.98 22.3 58 2.00 45.3 12 3.58 24.9 64 1.90 47.9 6 3.37 26.4 28 1.87 48.8 6 3.17 28.2 87 1.76 52.0 8 2.98 30.0 17 1.69 54.4 5 2.83 31.6 59 1.68 54.5 7 2.48 36.2 21 1.58 58.2 12 1.54 60.1 8 Relative intensities less than 5 are not quoted.

Treatment of the catalyst precursor with boiling water as described in Example 2 resulted in a catalyst precursor which on analysis by X-ray diffractometry showed that the X-ray spectrum of phase E was essentially absent ( < 1% by wt. phase E present) and on D.T.A. it was found that the endothermic transition at 365"C to 420"C was also absent. This catalyst precursor gave on pretreatment a final catalyst with a greatly improved performance typical of that exemplified in Examples 2 and 3.

On evaporation of the extractant water a solid comprising phase E was recovered.

Example 5 Part A A catalyst precursor was prepared as described in example 1 and was extracted with DMSO )20 mls/lg solid) at 700C for 24 hours. The resulting slurry was filtered hot, washed with a small amount of DMSO and dried at 1 100C in an air oven. A portion of the resulting solid was mixed with "Sterotex" (3% w/w) and pelleted at 17 tons. The pellet was sieved and crushed to give particles 500 - 710 ffi in size and a 5 ml portion was charged to a tubular fixed bed reactor. The catalyst was then calcined in situ by heating to 3850C at a rate of 3"C/min whilst 1.5% n-butane by volume in air flowed through the bed. After 11 hours the temperature was raised stepwise to 450"C for 2 hours. After calcination at a reactor temperature of 385"C, at atmospheric pressure and GHSV of 1000 h(1 the catalyst gave a 120/0 molar pass yield of maleic anhydride at a butane conversion of 15%. A sample of the final catalyst was examined by X-ray powder diffractometry and was found to exhibit the X-ray powder diffraction patterns characteristic of phase X and phase Y in addition to that of the beta phase. The catalyst was found to contain 23% phase X.

Part B The catalyst precursor prepared as described in example 1 was examined by X-ray diffractometry and D.T.A. and was found to contain phase E. Treatment of the catalyst precursor with DMSO as described in example 5 part A resulted in a precursor which on analysis by X-ray diffractometry showed that the X-ray diffraction spectrum of phase E was essentially absent. Also on D.T.A. it was found that the endothermic transition at 365 420"C, characteristic of phase E, was absent.

Example 6 A series of final catalysts were prepared by the methods described in examples 1, 2 and 3.

The specific activity of these catalysts was then determined for the oxidation of 1.5% n-butane in air to give maleic anhydride at a reactor temperature of 385"C and a GHSV of 1000 h(1 at atmospheric pressure. The results are given in Table 4 and these show that the specific activity for the production of maleic anhydride increases with increasing phase X content.

TABLE 4 Method of Surface % phase X Specific activity Preparation area m-/g in final moles maleic catalyst anhvdride producedl"21hour Example 1 3 None 1.3 x 10-5 Example 2 11 37 1.43 x 10-5 Example 2 10 42.5 2.10 x 10-5 Example 3 10 52.4 3.19 x 10-5 Example 7 Vanadium pentoxide (183 g.) and orthophosphoric acid (88%, 414.9 g) were suspended in methanol 2,400 ml). The suspension was refluxed for 5 hours and was then cooled to room temperature and left to stand for 24 hours. The yellow solid prepared was collected by filtration and dried at 115"C in an air oven. A portion of the solid (81 g) was then slurried with concentrated aqueous hydrochloric acid (100 mls) and was refluxed for 24 hours after which time the slurry had become blue in colour. The slurry was then evaporated to dryness and the solid was dried at 115"C in an air oven. The resulting solid was then boiled with water (20 mls/g solid) for about 2 hours and the resulting blue suspension was filtered hot and the solid was washed with a little warm water and dried at 1500C. A portion of the dried solid was mixed with a pelleting agent sold under the trade name "Sterotex" (2% by weight) and pelletised under pressure at 17 tons. The pellet was then crushed and sieved to give particles 500 - 710 ilin size and a 5.0 ml portion was charged to a tubular fixed bed reactor. The catalyst was then calcined in situ by the procedure detailed in example 1. After calcination, the catalyst gave a molar pass yield of 47% at a butane conversion of 87% at a reactor temperature of 420"C and a GHSV of 1000 hil of 1.5% n-butane in air at atmospheric pressure. At a reactor temperature of 385"C and a GHSV of 1000 hil of 1.5% n-butane in air at atmospheric pressure the catalyst gave a molar pass yield of 44% at an n-butane conversion of 68%. The surface area of the final catalyst was 12 m2/g. The final catalyst was examined by X-ray diffractometry and was found to contain in excess of 20% phase X.

Example 8 A catalyst precursor was prepared, extracted with water, dried, pelleted and sieved to give 500 - 710 > particles as described in example 2. The particles were then heated in a muffle furnace to 400"C for 12 hours (nitrogen was fed). A sample of the heat treated catalyst was examined by X-ray powder diffractometry and was found to contain the X-ray powder diffraction patterns characteristic of phase X and phase B' with only a small proportion of the beta phase being present. The heat treated catalyst was found to contain about 40% phase X. A 5 ml portion of the heat treated catalyst was loaded to a fixed bed tubular reactor. At a reactor temperature of 420"C and a GHSV of 1000 hil of 1.6% n-butane in air at atmospheric pressure the catalyst gave a 34% molar pass yield of maleic anhydride at a butane conversion of 50%. The surface area of the final catalyst was 7 m2/g.

Examples 9 - 14 show that the catalytic performance of catalysts containing phase X can be greatly improved by the addition of trace amounts of promoters.

Example 9 A catalyst precursor was prepared. extracted with boiling water, dried, pelleted and sieved to give particles 500 - 710 y in size as described in example 3. The particles were then dried at 1500C for 16 hours and were then impregnated with an aqueous solution containing 8g. per 100 ml of cobalt chloride (as Cowl2 6H2O) to give a catalyst with a Co:V atomic ratio of 0.04:1. After drying a 5.0 ml portion was charged to a tubular fixed bed reactor and the catalyst was calcined in situ by the procedure detailed in example 1. After calcination the catalyst gave a molar pass yield of 60% at a butane conversion of 88% at a reactor temperature of 430"C and a GHSV of 1000 h(1 of 1.5% n-butane by volume in air at atmospheric pressure. The surface area of the final catalyst was 13 m2/g and on analysis by X-ray powder diffraction the final catalyst was found to contain 44% phase X.

Example 10 A catalyst was prepared as described in example 9 except that a solution of cobalt chloride (4-5g as CoCI2 6H2O) in isobutanol (25 ml) was used to impregnate the catalyst particles. The Co:V ratio of the catalyst was 0.034:1. After drying a 5.0 ml portion was charged to a tubular fixed bed reactor and the catalyst was calcined in situ by the method detailed in example 1. After calcination the catalyst gave a molar pass yield of 56% at a butane conversion of 87% at a reactor temperature of 420"C and a GHSV of 1000 h(1 of 1.5% n-butane in air at atmospheric pressure. The surface area of the final catalyst was 10 m2/g and on analysis by X-ray powder diffraction the catalyst was found to contain 46% phase X.

Example 11 A catalyst precursor was prepared, extracted with water, dried, pelleted and sieved to give particles 500 - 71011 in size as described in example 3. A series of cobalt promoted catalysts were then prepared using the method given in example 9 and using aqueous cobalt chloride solutions of different concentration to vary the Co:V atomic ratio. 5 ml portions of the catalyst were then loaded to the reactor and calcined in situ by the method described in example 1. The catalysts were then used to oxidise 1.5% n-butane in air to maleic anhydride and the results are given in Table 5.

TABLE 5 V:Co Reactor n Butane Maleic atomic Temper- conversion Anhydride Surface ratio GHSV ature Molar Pass Area Phase OC C % Yield % m21g X 0.053:1 2000 420 85 58.9 15.8 35 2500 430 86 57.0 0.065:1 2000 420 94.5 59.3 14 40 0.075:1 1600 420 86.6 58.5 10 41 Example 12 This example shows the use of lanthanum as a promoter.

A catalyst precursor was prepared, extracted with boiling water, pelleted and sieved to give particles 500 - 710 in size as described in example 3. The particles were then dried at 1500C in air for 16 hours and were then impregnated with a solution of lanthanum nitrate (2.7 g. La(NO3)3 6H20) in isobutanol (25 ml) to give a catalyst with a V:La atomic ratio of 1:0.009. By using a different concentration of lanthanum nitrate in isobutanol (4.6g/25 ml) at catalyst was prepared with a V:La atomic ratio of 1:0.027. 5 ml portions of these catalysts were then loaded to a fixed bed tubular reactor and calcined as described in example 1. The catalysts were then used to oxidise 1.5% n-butane in air to maleic anhydride and the results are given in Table 6.

TABLE 6 V:La Reactor n Butane Maleic atomic GHSV Temper- conversion Anhvdride Surface ratio hK1 ature % Molar Pass Area Phase OC Yield % m/g X 1:0.009 2000 420 83 60 15 32 1:0.027 2500 420 88 60 18 33 Example 13 A catalyst precursor was prepared, extracted with boiling water, dried, pelleted and sieved to particles 500 - 7101l in size as described in example 3. The particles were then dried at 1500C in air for 16 hours. A series of promoted catalysts were then prepared using a range of promoters by impregnating the catalyst particles with solutions of suitable promoter compounds in isobutanol. 5 ml portions of the promoted catalysts were then loaded to a fixed bed tubular reactor and were then calcined in situ by the method described in example 1. The promoted catalysts were then used to oxidise 1.5% n-butane in air to maleic anhydride and the results are given in Table 7.

Promoter V:Promoter Promoter Reactor Maleic Atomic Compound Temper- GHSV n Butane Anhydride Surface % Ratio used for ature hr-1 conversion Molar Pass Area Phase Impreg- C % Yield % m/g X nation CHROMIUM 1:0.004 Cr(NO3)39H2O 385 500 90 57 10 50 420 1000 93 50 COPPER 1:0.01 Cu(NO3)23H2O 420 1000 91 54 12 35 CERIUM 1:0.0125 Ce(NO3)36H2O 440 1000 95 50 11 50 NICKEL 1:0.008 Ni(NO3)26H2O 420 1000 80 49 12 17 ZINC 1:0.03 ZnCl2 420 400 90 60 8.6 30 450 1000 91 59 Example 14 This example demonstrates the use of molybdenum as a promoter.

Vanadium pentoxide (60.6g) and molybdenum trioxide (8g) and concentrated aqueous hydrochloric acid (760 mls) were heated under reflux with stirring for about 2 hours to give a dark blue solution. To this solution orthophosphoric acid (89.3g, 88%) was added and the resulting solution was refluxed for a further period of about 2 hours. This solution was then evaporated to dryness and the resulting solid was dried in an air oven at 1100C. The resulting solid was then boiled with water (20 mls/g solid) for about 2 hours and the resulting suspension was filtered hot, washed with a small amount of warm water and dried at 110 C. The V:Mo atomic ratio of this dried solid was 1:0.043. A portion of the dried solid was mixed with a pelleting agent sold under the trade name "Sterotex" (3% by weight) and was then pelleted under a pressure of 17 tons. The pellet was then crushed and sieved to give particles 500 - 710cm in size and a 5 ml portion was loaded to a fixed bed tubular reactor.

The catalyst was calcined in situ by the method described in example 1. After calcination, at a reactor temperature of 420"C and a GHSV of 1000 hr1 of 1.5% n-butane in air at atmospheric pressure the catalyst gave a 55% molar pass yield of maleic anhydride at a n-butane conversion of 75%. The surface area of the final catalyst was 9 m4g and on analysis by X-ray powder diffraction the final catalyst was found to contain 43% phase X.

Example 15 The catalyst used in Example 3 was fed at 3700C with a gas stream containing 1% o-xylene in air at atmospheric pressure at a GHSV of 1000 h(1. The exit gas was scrubbed with acetone. The conversion of o-xylene was 53% and substantial quantities of phthalic anhydride were produced.

GHSV = gas hourly space velocity measured at room temperature (20"C) and atmospheric pressure.

All reactions were carried out at atmospheric pressure.

DMSO = dimethyl sulphoxide Gas compositions are given as molar % The pressures applied in pelletting were applied to an area of 1.1 sq.inches.

Claims

WHAT WE CLAIM IS:

1. A process of producing a catalyst for the production of acid anhydrides which comprises reacting a vanadium compound with phosphoric acid, producing a solid vanadium/phosphorus mixed oxide catalyst precursor, contacting the solid precursor with an acid stronger than phsophoric acid (judged in terms of its first dissociation constant in water) at a concentration of at least 3N, recovering the precursor and extracting it with water or with another solvent for phase E until substantially only material insoluble in water or the said solvent is left. separating the precursor and producing a phase transition to a catalytically active form by heating it.

2. A process as claimed in claim 1 in which the acid stronger than phosphoric acid is hydrochloric acid.

3. A process as claimed in claim 1 or 2 in which the concentration of the acid stronger than phosphoric acid is at least SN.

4. A process as claimed in claim 1, 2 or 3 in which the acid stronger than phosphoric acid is in an aqueous solution.

5. A process as claimed in any preceding claim in which the vanadium compound is reacted with phosphoric acid in the presence of the acid stronger than phosphoric acid and a solvent, and the vanadium/phosphorus mixed oxide catalyst prcecursor is precipitated by removing solvent thus leaving the precursor in contact with the acid stronger than phosphoric acid at a concentration of at least 3N.

6. A process as claimed in claim 5 in which the solvent is water.

7. A process as claimed in claim 5 or 6 in which at least 90% of the solvent is removed.

8. A process as claimed in claim 5, 6 or 7 in which the precursor is left substantially dry.

9. A process as claimed in any preceding claim in which the phase transition is carried out before the catalyst is used by heating the precursor to a temperature of 340 to 500"C.

10. A catalyst for the oxidation of hydrocarbons to acid anhydrides which comprises vanadium/phosphorus mixed oxides of which at least 40% by weight is phase X and which has a surface area of at least 7m2/g.

11. A catalyst as claimed in claim 10 which comprises vanadium/phosphorus mixed oxides of which at least 50% by weight is phase X.

12. A catalyst as claimed in claim 10 or 11 which has a surface area of at least 10m2/g.

13. A catalyst produced by a process according to any of claims 1 to 9 or a catalyst according to any of claims 10 to 13 which contains less than 15% by weight of amorphous vanadium/phosphorus mixed oxides and in which if the catalyst contains vanadium/ phosphorus mixed oxides other than phase X they are at least partly present as phase B or B.

14. A catalyst produced by a process according to any of claims 1 to 9 or a catalyst as claimed in any of claims 10 to 13 which comprises a promoter.

15. A catalyst as claimed in claim 14 in which the promoter is tungsten, nickel, cadmium, zinc, bismuth, lithium, copper, uranium, zirconium, hafnium, chromium, iron, manganese, molybdenum, cobalt and/or a rare earth metal.

16. A catalyst as claimed in claim 14 or 15 in which the atomic ratio of the promoter to vanadium is in the range 0.0015:1 to 1:1.

17. A catalyst for the oxidation of hydrocarbons to acid anhydrides which comprises a vanadium/phosphorus mixed oxide having a surface area greater than 10m2/g which is promoted with a rare earth metal promoter.

18. A catalyst as claimed in claim 18 in which the surface area is greater than 15m2/g.

19. A catalyst as claimed in claim 18 or 19 in which the promoter is lanthanum.

20. A catalyst as claimed in any of claims 10 to 20 or prepared by a process as claimed in any of claims 1 to 9 which has a surface area of 10 - 50m2/g.

21. A catalyst as claimed in any of claims 10 to 21 or prepared by a process as claimed in any of claims 1 to 9 which comprises an alumina, silicon carbide, kieselguhr, pumice or silica support.

22. Catalysts whenever prepared by a process as claimed in any of claims 1 to 9

23. A process of oxidising a hydrocarbon to maleic or phthalic anhydride by contacting the hydrocarbon in the presence of oxygen with a catalyst as claimed in any of claims 10 to 23.

24. Catalysts for the production of acid anhydrides as claimed in any of claims 10 to 22 substantially as described in any one of the Examples.

25. A process for the production of a catalyst for the production of acid anhydrides as claimed in any of claims 1 to 9 whenever carried out substantially in accordance with any one of the Examples.

26. Acid anhydrides whenever produced by a process as claimed in claim 23.

27. Acid anhhydrides whenever produced by a process as claimed in claim 23 and substantially as described in any one of the Examples.