BIMETALLIC GOLD - PALLADIUM CATALYST

This invention relates to a process for the oxidation of cycloalkanes utilising a supported gold and palladium catalyst and the use of the supported gold and palladium catalyst for the oxidation of cycloalkanes. Also described is a process for the preparation of the catalyst.

The oxidation of cyclohexane, particularly under mild reaction conditions, is of key importance to industry because the products, in particular cyclohexanol and cyclohexanone, are precursors for the production of adipic acid which is a key intermediate in the production of polyamides, polyurethanes, polyesters and plasticizers. Typically, adipic acid is prepared by oxidising a mixture of cyclohexanol and cyclohexanone (KA oil) with nitric acid. KA oil is the primary product of cyclohexane oxidation. Cyclohexanone is also used as a starting material for caprolactam.

Currently, commercial cyclohexane oxidation is conducted by using homogeneous cobalt and manganese salts, at temperatures above 423K. The process provides cyclohexanol and cyclohexanone as products with selectivity of 85%. Significant amounts of cyclohexyl hydrogen peroxide (CHHP) and trace amounts of carboxylic acid by-products are also produced. However, the high selectivity for cyclohexanol and cyclohexanone products is only obtained at low conversion levels, typically less than 10%, and most typically less than 5% conversion. While manipulation of the reaction conditions can provide greater conversion, this is normally accompanied by deterioration in the selectivity to cyclohexanol and cyclohexanone.

It has been found that catalytic performance above 5% conversion can be achieved in the oxidation of cyclohexane using hydrogen peroxide or ierf-butyl hydrogen peroxide (TBHP). However, it is commercially attractive to employ oxygen or air in any industrial process due the cheapness and feasibility in large scale operations. For similar reasons, and from an environmental perspective, it is also desirable to employ a process which does not use solvent.

Environmental issues are also relevant when considering the suitability of catalysts for large- scale production. Higher turn-over-frequency can be obtained by using low concentration of homogeneous catalysts. However, recycling of homogeneous catalysts and disposal of waste liquid are problematic and have significant impacts on the environment. Most conventional heterogeneous catalysts are typically inactive under mild reaction conditions due to relatively low mobility of lattice oxygen.

The catalyst and processes of the invention address the above problems associated with current commercial catalysts and processes for the oxidation of cycloalkanes. Thus, it is an object of this invention to provide a process for cycloalkane (particularly cyclohexane) oxidation which yields cycloalkanol and cycloalkanone (particularly cyclohexanol and cyclohexanone) products with high selectivity (at least 85%, and preferably at least 90%) and at conversion levels above 5% (particularly above 10%). which would be a significant development over current industrial processes. It is a further object of the invention to provide a heterogeneous catalyst which can be recycled and which may be used in a process for oxidising cycloalkanes, which is suitable for industrial scale-up and which yields cycloalkanol and/or cycloalkanone with favourable selectivity and conversion. It is a particular object of the invention to provide a heterogeneous catalyst which can selectively decompose CHHP in a single unit operation, in order to increase conversion and maintain or improve the reaction selectivity to cyclohexanol and cyclohexanone in the oxidation of cyclohexane. It is a further particular object of the invention to provide a more efficient and economical process for the production of adipic acid from the oxidation of cyclohexane. A key element of the overall cost for the current industrial production of adipic acid is steam usage and the alternative catalyst system provided by the present invention significantly reduces this element.

In a first aspect, the invention provides a process for oxidising cycloalkane(s) comprising contacting one or more cycloalkane(s) with an oxidant in the presence of a supported catalyst, wherein the supported catalyst comprises a catalyst comprising gold-palladium particles and a support selected from carbides, nitrides and oxides, wherein the oxides are selected from magnesium, aluminium and zinc oxides.

There is also described a process for the preparation of a supported catalyst comprising the steps of:

(a) preparing an aqueous solution of gold and palladium salts; and

(b) adding a support thereto, wherein the support is selected from carbides, nitrides and oxides, wherein the oxides are selected from magnesium, aluminium and zinc oxides, and wherein said process further comprises the step of reducing the gold and palladium ions.

The reduction step typically comprises the addition of a suitable reducing agent, either before or after the addition of the support, and in a preferred embodiment the reducing agent is added before the addition of the support. Alternatively, the reduction step may be effected by calcination. The reduction step reduces the gold and palladium ions to the gold-palladium alloy of the catalyst of the present invention. In a second aspect, the invention provides an oxidation process for preparing cycloalkanol(s) and/or cycloalkanone(s) comprising contacting one or more cycloalkane(s) with an oxidant in the presence of a supported catalyst, wherein the supported catalyst comprises a catalyst comprising gold-palladium particles and a support selected from carbides, nitrides and oxides, wherein the oxides are selected from magnesium, aluminium and zinc oxides.

In a third aspect, the invention provides the use of a supported catalyst, wherein the supported catalyst comprises a catalyst comprising gold-palladium particles and a support selected from carbides, nitrides and oxides, wherein the oxides are selected from magnesium, aluminium and zinc oxides, as a catalyst for the oxidation of cycloalkanes. The Catalyst

The gold-palladium particles of the catalyst are a gold-palladium (AuPd) alloy, and preferably in the form of nanoparticles. The mean longest diameter of a nanoparticle is preferably no more than about 200nm, more preferably no more than about 50nm, more preferably no more than about 30nm, and more preferably no more about 20nm, and most preferably in the range of from about 5nm to about 15 nm. The mean size and size distribution of the nanoparticles is suitably measured by STEM (Scanning Transmission Electron Microscopy), where visual inspection of a typical section of the supported catalyst sample is used to count particles of different sizes within a given cross sectional area.

The composition of the gold-palladium alloy influences the catalytic activity and the inventors have found that optimum conversion and selectivity in the oxidation of cycloalkanes is obtained when the molar ratio of gold to palladium in the alloy is in the range from about 1 :18 to about 18:1 , more preferably from about 1 :15 to about 15:1 , more preferably from about 1 :12 to about 12:1 , more preferably from about 1 :10 to about 10:1 , and most preferably from about 1 :9 to about 9:1. The support has a very significant effect upon the catalytic performance of the gold-palladium particles in the oxidation of cycloalkanes. For example, a silica-supported AuPd catalyst was found to be inactive in the cyclohexane oxidation reaction, whereas replacement of the silica with silicon nitride (Si ₃ N ₄ ) as the support provided good catalytic activity for the AuPd catalyst in cyclohexane oxidation. Thus, the interaction between support, particularly surface oxygen species, and active species is a key factor for catalytic activity. Surprisingly, the inventors observed that, using some supports, additional amounts of catalysts did not improve the catalytic performance, but quenched the whole reaction. This phenomenon would appear contradictory to conventional catalyst performance since a greater amount of catalyst would normally be expected to improve the concentration of active oxygen species, facilitating the oxidation of the reactant. The phenomenon is not, however, unknown. The so-called catalyst- inhibitor transition was identified by J. F. Black (JACS, 1978, 100, 527-535) who observed sharp changes in catalytic performance dependent on the concentration of a cobalt/manganese salt in a metal-catalysed autoxidation. The catalyst-inhibitor transition is of particular importance in an industrial process. Catalyst systems associated with a catalyst-inhibitor transition which is very sensitive to catalyst amount requires the presence of precise amounts of catalysts for industrial production. Such catalyst systems are inflexible and prone to negative effects on productivity, and hence unattractive for an industrial process. The catalyst system of the invention utilises a support selected from the group consisting of carbides, nitrides and certain oxides. Preferably, the carbide supports are selected from B ₄ C ₃ , Mo ₂ C, ZrC, WC, SiC and TiC, more preferably from B ₄ C ₃ and SiC, and more preferably the carbide is SiC. Preferably, the nitrides are selected from BN, C ₃ N ₄ , AIN and Si ₃ N ₄ , and preferably from BN and Si ₃ N ₄ . The oxides of magnesium, zinc and aluminium may be single metal oxides or mixed metal oxides, for instance selected from MgO, Al ₂ 0 ₃ , ZnO, and MgAI ₂ 0 ₄ . Preferably, the catalyst system of the invention utilises a carbide or nitride support, more preferably a carbide support. The carbide supports exhibit high stability and chemical inactivity in cycloalkane oxidation, even at higher temperature, and were found to be superior in these respects to, for instance, the nitride supports. Thus, the carbide support is effectively inert for cycloalkane oxidation, and is neither catalyst nor inhibitor. A particular advantage of the present invention is that the preferred supports (most notably the carbide supports) modify catalyst performance in a way which greatly improves the resistance of the catalyst system to catalyst amount, and are therefore particularly suitable for an industrial process.

The loading of the AuPd catalyst is preferably in the range of from about 0.1 to about 10 wt% based on the total weight of the support and catalyst, preferably from about 0.5 to about 5 wt%, preferably from about 0.5 to about 2 wt.%.

The inventors also found that modification of the AuPd catalyst by doping further improves catalytic performance. Such a modification combines the improved resistance of the catalyst system to catalyst amount with increased conversion and/or selectivity. Furthermore, the doping modification inhibits the production of ring-opened carboxylic acid species, such as adipic acid in the oxidation of cyclohexane. This is advantageous because adipic acid and other byproducts would otherwise have to be separated from the reaction mixture.

The introduction of the dopant is typically effected by surface modification of the supported AuPd catalyst, using methods as described herein, for instance by coating the surface of the supported AuPd catalyst. Preferred dopants are the basic metal oxides and hydroxides, and in particular MgO, Al ₂ 0 ₃ , ZnO, CaO, Mg(OH) ₂ , AI(OH) ₃ , Zn(OH) ₂ , and Ca(OH) ₂ . Particularly effective dopants are selected from Mg(OH) ₂ and AI(OH) ₃ , preferably AI(OH) ₃ . As used herein, the term "dopant" refers to a material which is different to the materials of the support and the catalyst. Thus, a basic metal oxide or hydroxide in the list hereinabove is used as a "dopant" in a supported catalyst which does not contain that species as the support. The basic metal oxides and hydroxides in the list hereinabove are of particular utility in supported AuPd catalysts wherein the support is selected from the carbides and nitrides described herein.

The amount of dopant introduced into the supported AuPd catalyst is preferably quantified as a function of the amount of dopant used during the catalyst preparation, and defined as the weight percent of dopant relative to the total weight of the initial aqueous solution of gold and palladium salts used in the preparation. Thus, the amount of dopant used during the catalyst preparation is preferably in the range of from about 1.25x10 ^"3 wt% to about 2x10 ^"2 wt%, preferably from about 1.5x10 ^"3 wt% to about 1 10 ^_2 wt%,and in one embodiment about 5x10 ^"3 wt%, relative to the total weight of the initial aqueous solution of gold and palladium salts used in the preparation.

The supported catalyst is suitable for use as a heterogeneous catalyst in the process for oxidising cycloalkane. The heterogeneous nature of the catalyst is advantageous, allowing the catalyst to be more easily separated from the reaction products and recycled. For example, when the cycloalkane is cyclohexane, the reactant is in the liquid phase and the catalyst is in the solid thereby allowing the catalyst to be extracted from the reaction mixture by filtration.

Thus, in a fourth aspect, the present invention provides the use of the supported catalyst defined herein as a catalyst, suitably a heterogeneous catalyst, in a process for oxidising cycloalkane(s), particularly for preparing cycloalkanol(s) and/or cycloalkanone(s).

Preparation of the supported AuPd catalyst The gold-palladium particles of the catalyst are preferably prepared according to the sol- immobilisation method defined hereinafter, in which a water-soluble polymer is added to a solution of gold and palladium salts, with the subsequent addition of a reducing agent. The resulting gold-palladium particles are obtained as a sol and then supported on a support. The supports are usually added to the sol, as a solid, under vigorous stirring conditions for up to about 3 hours. The supported catalyst can be extracted by filtration, washed with water, and then dried. Typical drying temperatures are around 120°C, and drying may be conducted for 8- 12 hours. Accordingly, the sol-immobilisation method for preparing the catalyst of the invention preferably comprises the following steps: (a) preparing an aqueous solution of gold and palladium salts;

(b) adding a water-soluble polymer to the solution obtained in step (a);

(c) adding a reducing agent to the solution obtained in step (b) to form a sol; and

(d) adding a support to the sol solution obtained in step (c) to form a slurry. The process for preparing the supported catalyst of the invention may further comprise, additionally to steps (a) to (d) above, the following steps:

(e) filtering the resulting slurry obtained in step (d);

(f) washing the product of step (e) with water; and

(e) drying the washed product of step (f). Any suitable palladium salt may be used, and preferably the palladium salt is a palladium (II) salt, for instance PdCI ₂ , which is commonly used for the production of palladium catalysts. Any suitable gold salt may be used, and preferably the gold salt is a gold (III) salt, for instance gold (III) chloride, KAuCU or chloroauric acid (HAuCU), used herein in the form of its trihydrate HAuCI ₄ .3H ₂ 0. Any suitable reducing agent may be used, and in a preferred embodiment the reducing agent is NaBH ₄ . The reducing agent is preferably provided in a molar excess with respect to the amount of gold, and in one embodiment in a molar ratio of at least about 2:1 , and in a further embodiment in a molar ratio of 5:1 . The reducing agent is normally provided in the form of an aqueous solution, and in one embodiment it is provided as a 0.1 M aqueous solution. The water-soluble polymer is preferably polyvinylalcohol (PVA). The PVA may be provided in partially or fully hydrolysed form, and in one embodiment is partially hydrolysed. The PVA suitably exhibits a degree of hydrolysis of at least about 70%, and in one embodiment a degree of hydrolysis in the range of from about 70 to about 90 %. In a preferred embodiment, the water- soluble polymer has a molecular weight of from about 5000 to about 20,000, and preferably from about 8,000 to about 12,000. The water-soluble polymer is normally provided in the form of an aqueous solution, and in one embodiment it is provided as a 1 wt% aqueous solution. The water-soluble polymer is preferably provided in weight excess relative to the amount of gold, and in one embodiment it is provided in a weight ratio of 1 .2:1 with respect to the amount of gold. The ratio of PVA to the metallic species of the catalyst (AuPd) is preferably from about 0.01 :1 to about 0.1 :1.

The doped supported gold-palladium catalysts of the invention are preferably prepared using the sol-immobilisation method described herein process, comprising the additional step of introducing into the process a solution (normally aqueous) of a salt comprising the metal ion of the dopant, typically after production of the sol (step (c)) and before addition of the support (step (d)). Metal nitrate salts are particularly suitable, and magnesium nitrate and aluminium nitrate were used herein to generate the magnesium hydroxide and aluminium hydroxide dopants, respectively. Subsequently, the support is added as described herein and the pH value of the solution adjusting to a value between 8 and 12 using any suitable base, for instance ammonia. After vigorous stirring, the supported catalyst is filtered, washed and dried as described above.

In one embodiment, the supported catalysts may be calcined after drying. Calcination can be conducted under an atmosphere of air, nitrogen, hydrogen, helium or the like, and is typically conducted under an atmosphere of air. Calcination temperatures may range from 200 to 1000°C, typically 200 to 700°C. The calcination time may be from about 1 to about 40 hours, more typically from about 2 to about 15 hours. In a preferred embodiment, however, the supported catalysts (particularly the doped supported catalysts) of the present invention are not calcined, since while selectivity may increase, conversion tends to decrease.

Alternative methods for preparation of the supported catalyst include impregnation methods, precipitation methods and seed-mediated growth, and these methods may use the reactants described hereinabove.

In an impregnation method, an aqueous solution of gold and palladium salts is prepared, and the support added thereto in the desired weight ratios. The suspension is then stirred, filtered and washed. The supported catalyst is then dried, as described above for the sol-immobilisation method, and consecutively calcined, as described above. The aerobic calcination process reduces the impregnated gold and palladium salt precursors to provide gold-palladium particles.

In a precipitation method, an aqueous solution of gold and palladium salts is prepared, to which is added a suitable base (for instance, sodium carbonate) with stirring until a pH of from about 9 to about and 1 1 is attained. The support is added with continuous stirring for up to about 3 hours, maintaining the pH between 9 and 1 1. The mixture is heated from room temperature to around 70°C, and a suitable reducing agent (for instance formaldehyde) is then added. The solid is filtered, washed and dried, as described above.

Oxidation of Cycloalkanes

The supported catalysts described herein are particularly suitable for oxidising cycloalkanes to the corresponding cycloalkanol and/or cycloalkanone.

Examples of the cycloalkane as the raw material include monocyclic cycloalkanes having no substituent on the ring, such as cyclopropane, cyclobutane, cyclopentane, cyclohexane, cycloheptane, cyclooctane, cyclodecane, cyclododecane and cyclooctadecane; polycyclic cycloalkanes such as decalin and adamantane; and cycloalkanes having a substituent on the ring, such as methylcyclopentane and methylcyclohexane. Mixtures of cycloalkanes may be used, although it is preferable to limit the reaction to a single substrate, wherever possible, in order to avoid cross-reactions and to facilitate isolation of the target compounds. The present invention is of particular commercial utility for the oxidation of cyclohexane or cyclododecane, particularly cyclohexane.

An oxygen-containing gas is usually used as the oxygen source. This oxygen-containing gas may be, for example, air, pure oxygen, or air or pure oxygen diluted with an inert gas such as nitrogen, argon or helium. Oxygen-enriched air may also be used.

The amount of the supported catalyst to be used is usually in the range from about 0.01 to about 50 parts by weight, and preferably from about 0.1 to about 10 parts by weight, based on 100 parts by weight of cycloalkane.

The reaction temperature is usually no more than about 200°C, preferably no more than 180°C, and typically from about 50°C to about 150°C, and preferably form about 100°C to about 150°C. The reaction pressure is usually from about 0.01 to about 10MPa, and preferably from about 0.1 to about 2 MPa. The duration of the reaction is typically no more than 24 hours, and typically in the range of from about 1 to about 20 hours, preferably 1 to 5 hours. A solvent may be used for the reaction, and suitable solvents include nitrile solvents such as acetonitrile and benzonitrile, and carboxylic acid solvents such as acetic acid and propionic acid. In a preferred embodiment, the reaction is carried out in the absence of solvent.

The oxidation reaction in the presence of the supported AuPd catalyst can also be operated in the presence of a radical initiator. Examples of the radical initiator include azonitrile compounds such as 2,2'-azobis(isobutyronitrile), 2,2'-azobis(2,4-dimethylvarelonitrile), and 2,2'-azobis(4- methoxy-2,4-dimethylvarelonitrile); and peroxides such as TBHP, peroxydibenzoyl, peroxydilauroyi, t-butylperoxy 2-ethylhexanoate, and bis(2-ethylhexyl)peroxydicarbonate. Other examples of initiators include cyclohexanone, N-hydroxyphthalimide, and 2-butanone. Two or more kinds of these radical initiators may be used in combination, or a single radical initiator may be used. When the radical initiator is used, the amount is usually from 0.1 mole or less per mole of cycloalkane. However, a commercial process (particularly a continuous process) preferably does not use such a radical initiator, the exception being the use of an initiator which corresponds to the target cycloalkanone. Thus, in one embodiment, the oxidation process of the present invention is operated in the presence of an initiator which is the target cycloalkanone of the oxidation of the cycloalkane feedstock; for example, where the feedstock is cyclohexane, then cyclohexanone may be added into the reaction mixture as a radical initiator. The addition of the target cycloalkanone as initiator is typically effected by recycle of a portion of the target cycloalkanone product back to the reactor.

Once the oxidation reaction is completed, conventional post-treatment steps may be conducted. Thus, the reaction mixture is typically filtered to separate the catalyst, followed by washing with water and further distillation.

In a continuous commercial process, the oxidation reaction may be carried out using conventional oxidation reactors known in the art. For example, those described in US- 3,957,876; US-3,510,526 and US-3,530,185. The invention is further illustrated by the following examples. The examples are not intended to limit the invention as described above. Modification of detail may be made without departing from the scope of the invention.

Examples

The following general methods were used to synthesise the catalysts listed in Table 1. Preparation of supported Au/Pd catalysts (sol-immobilization method)

An aqueous solution of PdC^ (Johnson Matthey) and/or HAuCl ₄ -3H ₂ 0 of the desired concentration was prepared. Polyvinylalcohol (PVA) (1 wt% solution; Aldrich; MW = 10 000; 80% hydrolyzed) was added (PVA Au (by wt) = 1.2), and a 0.1 M freshly prepared solution of NaBH ₄ (Aldrich, NaBH ₄ /Au (mol/mol) = 5) was then added to form a dark-brown sol. 30 minutes after sol generation, the colloid was immobilized by adding the desired amount of support under vigorous stirring conditions. After 2 h the slurry was filtered, the catalyst washed thoroughly with distilled water (neutral mother liquors) and dried at 120°C overnight.

Surface modification of supported Au/Pd catalysts by doping with Mq(OH)? or AI(OH)3

The modified catalysts were prepared by using a modified sol-immobilization method. After formation of the Au-Pd nanoparticles in the sol, the desired amount (herein 10, 40, 80 or 160mg) of magnesium nitrate or aluminium nitrate was added into the solution. Afterwards, the desired amount of support was added and the pH value of the solution was adjusted to 1 1 by adding ammonia. After two hours stirring, the filtrate was washed and dried at 120°C overnight.

Oxidation of cyclohexane

The catalytic activity of the prepared catalysts in the oxidation of cyclohexane oxidation was studied on a laboratory scale by the method described below. Catalytic oxidation tests were performed using a glass bench reactor, which was connected to a cylinder of 0 ₂ gas. After the addition of cyclohexane (10 ml_) and desired amount of catalyst had been added to the unit, reactants were magnetically stirred at 140°C and 3 bar C^for 17 hours. After reaction was complete, the desired amount of chlorobenzene was added into the product as an external standard. The liquid products were then injected into a Gas Chromatograph (Varian 3200) with a CP-Wax 42 column and FID detector for ketone, alcohol, peroxide, ether and ester quantification. Any solid products of the reaction present in the final mixture were collected by filtration, washed with cyclohexane and subsequently dissolved in a known weight of methanol. Subsequently, 300 μΙ_ of sample out of the 10 ml_ product solution was mixed with 2 ml of 14% boron tri-fluoride (BF ₃ ) in methanol, which was subsequently heated at 70°C and magnetically stirred for half hour. After complete conversion of the acid products to corresponding methyl esters, the reaction was stopped by adding 2 ml_ water. Finally, the esters formed were extracted from the mixture using a known volume of dichloromethane and injected into GC for quantification. The results are described below. I: Effects of different supports on the activity of AuPd catalyst

The catalytic performance in the oxidation of cyclohexane of Au-based catalysts on different supports was tested in accordance with the procedure above, using 6mg of the catalyst. The results presented in Table 2 below demonstrate that the AuPd nano-alloys can display significant catalytic activity, but that this is highly dependent on the support. The best performance of 1 1% conversion and 97% selectivity was obtained by using MgO supported AuPd, which is even better than that of the commercial catalyst, cobalt naphthenate. Some of the supports, for instance, silica or zeolite, quenched the whole reaction. In this series of experiments, the performance of the MgO-supported AuPd catalyst was compared with AuAg and AuPt nano-alloys, which displayed inferior catalytic performance.

Table 2

Ket. = cyclohexanone; Ale. = cyclohexanol; CHHP = cyclohexyl hydrogen peroxide;

AA = adipic acid II: Effect of Au:Pd ratio

A series of experiments was conducted to determine the optimum molar ratios of gold and palladium in the catalyst, using MgO as the support. The results are shown in Figure 1 , and demonstrate that the preferred Au:Pd molar ratio is in the range from about 1 :9 to about 9:1.

Ill: Effect of catalyst amount

In experiments designed to optimise the reaction conditions with the MgO supported catalyst (1 %AuPd/MgO), it was observed that increasing the catalyst amount from 0 to 6mg resulted in high selectivity with increasing conversion levels. Surprisingly, however, further amount of catalyst did not improve the catalytic performance but instead quenched the whole reaction. Thus, when Experiment No.1 in Table 2 was re-run using 8mg of catalyst, no cyclohexane oxidation was observed (0% conversion).

IV: Effects of different supports on the resistance of AuPd catalysts to catalyst dose

The influence of the support on the resistance of the AuPd catalyst to catalyst amount was investigated using oxide, nitride and carbide supports. The oxidation reactions were run in accordance with the procedure describe above, with variable amounts of the supported catalyst. The results, which are presented in Table 3 below, demonstrate that the carbide-supported catalysts display superior resistance to high dose of catalyst.

Table 3

Expt Catalyst Amt. Conversion Selectivity (%)

No.

Ket. Ale. CHHP AA total (mg) (%)

12a 1 %AuPd/ZnO 6 7.8 44 36 5 86

12b 10 9 41 32 7 82

12c 20 5.4 42 30 14 86

12d 30 0

13a 1 %AuPd/AI ₂ 0 ₃ 6 7 43 33 6 83

13b 10 1 1 31 44 6 82

13c 20 0

14a 1 %AuPd/MgAI ₂ 0 ₄ 3 8.3 28 41 16 85

14b 6 6 46 35 5 88

14c 10 6 36 36 6 80

14d 20 0

15a 1 %AuPd/Si ₃ N ₄ 6 9 37 31 12 82

15b 10 6.5 37 31 22 91

15c 20 6.5 35 29 24 89

15d 30 5 34 41 18 19

15e 40 0 Table 3 (cont.)

V: Catalytic performance of carbide-supported AuPd doped with Mg(OH)? and AKOI-Qa

The catalytic performance of the carbide-supported AuPd catalysts was improved by the introduction of magnesium or aluminium oxides into the supported catalysts. The results of cyclohexane oxidation performed as described herein, using varying amounts of catalyst, are presented in Table 4.

Table 4

The designations M40, A10, A40, A80 and A160 refer to the identity and amount of base dopant used (A=AI(OH) ₃ ; M=Mg(OH) ₂ ; and the number is the total weight of base dopant present during the preparation method.

VI: Effect of Au:Pd ratio of carbide-supported AuPd catalysts doped with Mq(OH)? and AKOhQa

Further oxidation reactions were run to determine the effect of the Au:Pd ratio on the doped carbide-supported AuPd catalysts. The results are presented in Table 5 below.

Table 5