The invention relates to a process for oxidizing organic substrates by means of singlet oxygen using a modified molybdate LDH catalyst, and also the modified molybdate LDH catalyst itself.

The sole singlet oxygen oxidation ( ¹ θ ₂ -Ox) which is currently performed industrially is the photochemical ¹ θ ₂ -Ox in which the ¹ O ₂ is generated by a photochemical route. The disadvantage of this process results from the high costs of the photochemical devices required, and also restricted lifetime. The lamps required are degenerated relatively rapidly during the oxidation as a result of soiling of the glass surface. This process is also unsuitable for colored substrates. The process is actually only suitable for fine chemicals which are prepared on a relatively small scale (La Chimica e rindustria, 1982, Vol. 64, page 156).

For this reason, attempts have been made to find other process variants for the ¹ O ₂ - Ox which are suitable for the ¹ θ ₂ -Ox of water-insoluble hydrophobic organic substrates.

J. Am. Chem. Soc, 1968, 90, 975 describes, for example, the classical "dark" ¹ O ₂ -Ox in which ¹ O ₂ is generated not photochemically but rather chemically. In this case, hydrophobic substrates are oxidized by means of a hypochlorite/H2θ2 system in a solvent mixture composed of water and organic solvent. However, this process has found only a few synthetic applications, since many substrates are only sparingly soluble in the medium required. Moreover, the usability is quite restricted owing to side reactions between hypochlorite and substrate or solvent. Also, a large portion of the ¹ O ₂ is deactivated in the gas phase. Furthermore, this process is unsuitable for the industrial scale, since there is addition of the hypochlorite to H ₂ O ₂ in the organic medium and a large excess of H ₂ O ₂ is required to suppress the side reaction of sub-

strate with hypochlorite. An additional disadvantage arises by virtue of the occurrence of stoichiometric amounts of salt.

One variant of the "dark" ¹ O ₂ -Ox, which is not based on hypochlorite and is thus intended to partly avoid the above disadvantages, is known, for example, from J. Org. Chem., 1989, 54, 726 or J. MoI. Cat., 1997, 117, 439, according to which some water-soluble organic substrates are oxidized with H ₂ O ₂ and a molybdate catalyst in water as a solvent. According to Membrane Lipid Oxid. Vol. II, 1991 , 65 the ¹ θ ₂ -Ox of water-insoluble organic substrates with the molybdate/H ₂ θ ₂ system is difficult, since it was assumed that none of the customary solvents is suitable for maintaining the molybdate-catalyzed disproportionation of H ₂ O ₂ in water and ¹ O ₂ . However, the use of molybdenum catalysts also entails other disadvantages, for instance difficulty of recycling or environmental pollution.

Various literature sources, for example Adv. Synth. Catal. 2004, 346, 152-164, Chem. Commun., 1998, 267 or Chem. Eur. J. 2001 , 7, 2547, disclose the use of molybdate LDH catalysts for singlet oxygen oxidation, but these do not have satisfactory selectivity and do not afford satisfactory yields.

A further means of chemically generating ¹ O ₂ is, for example, the heating of triphenyl phosphite ozonide which is obtained from triphenyl phosphite and ozone. However, this method is, as described, for instance, in J. Org. Chem., Vol. 67, No 8, 2002, page 2418, employed only for mechanistic studies, since triphenyl phosphite is an expensive and additionally dangerous chemical.

In the base-catalyzed disproportionation of peracids, not only ¹ O ₂ but also further reactive compounds are formed, which lead to by-products.

It is accordingly an object of the present invention to enable the oxidation of organic substrates by means of singlet oxygen ( ¹ O ₂ ) with avoidance of molybdenum- containing wastewaters, and also to find a catalytic system with high activity and selectivity therefor.

Unexpectedly, this object is achieved by the use of a modified, heterogeneous mo- lybdate LDH catalyst.

The present invention accordingly provides for the oxidation of organic substrates by means of singlet oxygen, which comprises admixing organic substrates which react with ¹ θ2 with 10-70% H ₂ O ₂ in an organic solvent in the presence of a molybdate LDH catalyst modified by ethylene glycol, polyethylene glycol or polyols, and the catalytic decomposition of H ₂ O ₂ to water and ¹ θ ₂ then being followed by the oxidation to the corresponding oxidation products.

In the process according to the invention, organic substrates are oxidized by means of singlet oxygen.

The organic substrates used which react with ¹ θ2 may be the following compounds: olefins which contain one or more, i.e. up to 10, preferably up to 6, more preferably up to 4 C=C double bonds; electron-rich aromatics such as C ₆ -C ₅₀ , preferably up to

C ₃ O ₁ more preferably up to C2 ₀ phenols, polyalkylbenzenes, polyalkoxybenzenes; polycyclic aromatics having from 2 to 10, preferably up to 6, more preferably up to 4 aromatic rings; sulfides, for instance alkyl sulfides, alkenyl sulfides, aryl sulfides, which are either mono- or disubstituted on the sulfur atom, and also heterocycles having an oxygen, nitrogen or sulfur atom in the ring, for example C ₄ -C ₅ O, preferably up to 03O ₁ more preferably up to C20 furans, C4-C50, preferably up to C30, more preferably up to C ₂₀ pyrroles, C ₄ -CeO ₁ preferably up to C30, more preferably up to C ₂ othio- phenes.

The substrates may have one or more substituents, such as halogen (F, Cl, Br, I), cyanide, carbonyl groups, hydroxyl groups, C ₁ -CsO, preferably up to C30, more preferably up to C _2O alkoxy groups, CrC ₅₀ , preferably up to C ₃₀ , more preferably up to C ₂ O alkyl groups, C ₆ -C _5O , preferably up to C30, more preferably up to C ₂ o aryl groups, C ₂ -C ₅ O, preferably up to C30, more preferably up to C ₂ o alkenyl groups, C ₂ -C ₅ O, preferably up to C ₃₀ , more preferably up to C ₂₀ alkynyl groups, carboxylic acid groups,

ester groups, amide groups, amino groups, nitro groups, silyl groups, silyloxy groups, sulfone groups, sulfoxide groups, etc. The substrates may also be substituted by one or more NR1 R2 radicals in which R1 and R2 may be the same or different and are each H; Ci-C ₅ o, preferably up to C ₃ o, more preferably up to C ₂₀ alkyl; formyl; C ₂ -C5 ₀ , preferably up to C3 ₀₎ more preferably up to C ₂₀ acyl; C ₇ -C ₅₀ , preferably up to C3 ₀ , more preferably up to C ₂ o benzoyl, where R1 and R2 may also together form a ring, for example in a phthalimido group.

Examples of suitable substrates are: 2-butene; isobutene; 2-methy!-1-butene; 2-hexene; 1 ,3-butadiene; 2,3-dimethylbutene; Δ ^9|10 -octalin,

2-phthalimido-4-methyl-3-pentene; 2,3-dimethyl-1 ,3-butadiene; 2,4-hexadiene; 2-chloro-4-methyl-3-pentene; 2-bromo-4-methyl-3-pentene;

1-trimethylsilylcyclohexene; 2,3-dimethyl-2-butenyl-para-tolylsulfone;

2,3-dimethyl-2-butenyl-para-tolyl sulfoxide; Λ/-cyclohexenylmorpholine;

2-methyl-2-norbornene; terpinolene; α-pinene; β-pinene; β-citronellol; ocimene; citro- nellol; geraniol; famesol; terpinene; limonene; trans-2,3-dimethylacrylic acid; α-terpinene; isoprene; cyclopentadiene; 1 ,4-diphenylbutadiene; 2-ethoxybutadiene; 1 ,1'-dicyclohexenyl; cholesterol; ergosterol acetate; 5-chloro-1 ,3-cyclohexadiene; 3-methyl-2-buten-1-ol; 3,5,5-trimethylcyclohex-2-en-1-ol; phenol,

1 ,2,4-trimethoxybenzene, 2,3,6-trimethylphenol, 2,4,6-trimethylphenol,

1 ,4-dimethylnaphthalene, furan, furfuryl alcohol, furfural, 2,5-dimethylfuran, isobenzo- furan, dibenzyl sulfide, 2-methyl-5-tert-butylphenyl sulfide, etc.

The corresponding oxidation product is obtained from the substrates by the inventive oxidation. From alkenes, (polycyclic) aromatics or heteroaromatics, especially hydroperoxides or peroxides are obtained and can react further under the reaction conditions to give alcohols, epoxides, acetals or carbonyl compounds such as ketones, aldehydes, carboxylic acids or esters when the hydroperoxide or the peroxide is unstable.

The inventive oxidation is effected in an organic solvent.

Suitable solvents are CrCs alcohols such as methanol, ethanol, propanol, i-propanol, butanol, i-butanol, n-butanol, tert-butanol, ethylene glycol, propylene glycol, acetone, 1 ,4-dioxane, tetrahydrofuran, formamide, N-methylformamide, dimethylformamide, sulfolane, propylene carbonate and mixtures thereof. Preference is given to using methanol, ethanol, propanol, i-propanol, ethylene glycol, propylene glycol, acetone, formamide, N-methylformamide or dimethylformamide, particular preference to using methanol, ethanol, ethylene glycol, propylene glycol, formamide or dimethyl formamide as solvents.

If appropriate, up to 25% of water may be added to the organic solvent. However, the addition of water does not bring any advantages for the reaction. Preference is therefore given to not adding any water.

According to the invention, the heterogeneous catalyst added to the solvent- substrate mixture is a molybdate LDH catalyst modified by ethylene glycol, polyethylene glycol or by polyols (e.g. glycerol).

Unmodified molybdate(Mo) LDH catalysts (LDH layered double hydroxides) are already prior art and are described, for example, in Adv. Synth. Catal. 2004, 346, 152 - 164.

The unmodified Mo LDH catalysts are prepared, for example, according to the prior art (for example Chem. Eur. J. 2001 , 7, No. 12, P.2556) by reacting magnesium nitrate hydrates and aluminum nitrate hydrates in the presence of NaOH and subsequent addition of Na ₂ MoO ₄ ^H ₂ O.

In the case of these catalysts, the reaction product from the magnesium nitrate hydrates and aluminum nitrate hydrates forms the support material which, on completion of reaction, can first be isolated or can be treated directly with the molybdenum compound to exchange the nitrate groups for the (MoO ₄ ) ^2' .

The molar Mg/AI ratio in these catalysts may vary from 10 to 2. Preference is given to an Mg/AI ratio of 2:1.

The amount of molybdate compound used depends upon the desired loading of the support with molybdenum and may vary from 0.002 mmol Mo/g of catalyst to 2 mol Mo/g of catalyst.

In the modified Mo LDH catalysts used in accordance with the invention, an Mo LDH catalyst obtained according to the prior art is suspended in ethylene glycol, polyethylene glycol or polyol and kept in suspension for from a few hours up to several days at elevated temperature, preferably at from 60 to 100 ⁰ C, more preferably at from 75 to 85°C.

After the treatment with EG, PEG or polyol, the now modified Mo LDH catalyst is isolated from the suspension, dried under reduced pressure and can then be used in accordance with the invention.

These Mo LDH catalysts modified by EG, PEG or polyol are novel and therefore likewise form part of the subject matter of the present invention.

The amount of catalyst used depends upon the substrate used and is between 0.001 and 50 mol%, preferably between 0.1 and 10 mol%.

Subsequently, 10-70%, preferably 40-50% H ₂ O ₂ , is added. H ₂ O ₂ is preferably added slowly or in portions to the reaction mixture composed of solvent, substrate and catalyst, in the course of which the reaction mixture is preferably stirred. The consumption of H ₂ O ₂ in the process according to the invention is dependent upon the substrate used. For reactive substrates, preferably from 2 to 3 equivalents of H ₂ O ₂ are required, while less reactive substrates are preferably reacted with from 3 to 10 equivalents of H ₂ O ₂ .

The reaction temperature is between -20 and +8O ⁰ C, preferably between 15 and

6O ⁰ C.

The reaction progress can be monitored by means of UV spectroscopy or by means of HPLC.

After the reaction has ended, the reaction mixture is worked up. After filtering off the catalyst, the reaction solution which comprises the oxidation product is worked up by customary methods, for instance extraction, drying and isolation of the oxidation product, for example by column chromatography. The catalyst filtered off in accordance with the invention can then be used without further purification or drying for further oxidations.

The process according to the invention generates ¹ θ ₂ in a simple and efficient manner.

The process according to the invention affords the desired end products in high yields of up to 100% with high purity.

The process according to the invention is notable for the simple process which is ideally suited to the industrial scale, since it can be effected in simple multipurpose plants and with simple workup steps, and can be employed for a broad spectrum of substrates. A further advantage is the repeated reusability of the inventive catalyst.

Example 1 :

Synthesis and characterization of molybdate LDH (LDH = layered double hydroxide) catalysts

a) Preparation of the support material

A 1 I three-neck flask was charged with 100 ml of distilled water and the pH was adjusted to 10 with 1 M sodium hydroxide solution under a nitrogen atmosphere. 120 ml of a 0.333 M AI(NO ₃ ) ₃ -6H ₂ O solution and 120 ml of a 0.667 M Mg(NO ₃ ) ₂ -6H ₂ O solution were then introduced simultaneously into the flask with good stirring (metering rate 100 ml/h). During the metered addition of the two salt solutions, the pH was kept constant at 10 (by means of metering in a 1 M NaOH solution by means of a peristaltic pump). Once the salt solutions had been metered in, the suspension was stirred at room temperature for a further 22 hours. Thereafter, the precipitate formed was cen- trifuged, washed and centrifuged again. The washings were carried out three times (washing water required 3 x 400 ml).

The precipitate thus obtained was then dried by means of freeze-drying. Yield (dry): 10 g of {[Mg/AI]LDH ²⁺ (NO ₃ ) ^2' } catalyst support, white powder

b) Application of (MoO ₄ ) ^2" to the catalyst surface by exchange of (NO?) ^2"

10 g of [Mg/AI]LDH(NO ₃ ) ^" catalyst support (Mg/AI = 2) were added to a 2 mM Na ₂ MoO ₄ ^H ₂ O solution in water (volume 1 liter). The suspension was stirred at room temperature under inert gas atmosphere for a further 12 hours. The precipitate was centrifuged and washed twice with deionized water (400 ml per washing operation). The precipitate thus obtained was then dried by means of freeze-drying.

The Mo content was determined by means of ICP-AES which gave 0.02 mmol of Mo per gram of catalyst support.

Yield (dry): 9.8 g of {[Mg/AI]LDH ²⁺ (Mo0 ₄ ) ^2" } catalyst, white powder

c) Catalyst preparation without isolation of the support material

A 1 I three-neck flask was charged with 100 ml of distilled water and the pH was adjusted to 10 with 1 M sodium hydroxide solution under a nitrogen atmosphere. 120 ml of a 0.333 M AI(NO ₃ ) ₃ -6H ₂ O solution and 120 ml of a 0.667 M Mg(NO ₃ ) ₂ -6H ₂ O solution were then introduced simultaneously into the flask with good stirring (metering rate 100 ml/h). During the metered addition of the two salt solutions, the pH was kept constant at 10 (by means of metering in a 1 M NaOH solution by means of a peristaltic pump). Once the salt solutions had been metered in, the suspension was stirred at room temperature for a further 22 hours.

Thereafter, a 2 mM Na ₂ MoO ₄ -2H ₂ O solution in water (volume 1 liter) was added to the catalyst support suspension. The suspension was stirred at room temperature under an inert gas atmosphere for a further 12 hours. The precipitate was filtered off and dried at 60 ⁰ C under reduced pressure. Yield (dry): 11 g of {[Mg/AI]LDH ²⁺ (MoO ₄ ) ^2" } catalyst, white powder The Mo content was determined by means of ICP-AES which gave 0.02 mmol of Mo per gram of catalyst support.

Example 2:

Preparation of an Mo LDH catalyst modified by ethylene glycol

An Mo LDH catalyst prepared according to example 1 was suspended in 10 times the amount of ethylene glycol and kept in suspension at 80 ⁰ C for 12 hours. Subsequently, the mixture is filtered and the catalyst is dried under reduced pressure.

The Mo content was determined by means of ICP-AES which gave 0.02 mmol of Mo per gram of catalyst support. The catalyst was characterized by means of FTIR.

Examples 3-12:

Use examples of the catalyst

A general procedure for the oxidation of olefinic compounds was as follows:

In a 25 ml round-bottom flask, 0.25 g of Mo LDH EG (Mg/AI = 2; 0.2 mmol of Mo/g), 5 mmol of olefin and 5 ml of N,N-dimethylformamide were mixed at 25°C with good stirring, and H ₂ O ₂ (50% by weight) was added in portions of 2.5 mmol per portion. In the course of this, the color of the initially white suspension became yellowish to orange. The reaction progress was observed by means of GC.

The results for the oxidation of olefins are compiled in the table which follows.

ectivity

92 82

56 44

53 47

42 15 43

49 51 96

99

10 44 56 99 99

42 58 99 99

11

12 50 50

^[a] Limited peroxide formation of the 2,3 double bond was observed.

Examples 13-18:

Use examples of the catalyst

A general procedure for the oxidation of allylic alcohols was as follows:

In a 25 ml round-bottom flask, 0.1 g of Mo LDH EG (Mg/AI = 2; 0.2 mmol of Mo/g), 2 mmol of allyl alcohol and 2 ml of N,N-dimethylformamide were mixed at 25 ⁰ C with good stirring and H ₂ θ ₂ (50% by weight) was added in portions of 0.5 mmol per portion. The reaction progress was observed by means of GC.

Results for the oxidation of allylic alcohols are shown in the next table.

Substrate Product Distribution Conversion Selectivity

Example [%] [%] [%]

64 36

13

14 34 26 40

88 98

18 59 41

^[b] GC-incomplete separation of the diastereomers.

Example 19:

Examples of the use of other solvents.

Other solvents were also used instead of N,N-dimethylformamide for the peroxide generation. The results are shown in the graph which follows.

The model substrate used was citronellol.

Reaction conditions: 0.5 g of Mo LDH EG (Mg/AI = 2; 0.2 mmol of Mo/g, treated with

EG for 5 days at 80 ⁰ C), 10 mmol of citronellol, 40 mmol of H ₂ O ₂ (50% by wt.) added in 5 mmol portions, 10 ml of solvent, 25 ⁰ C

1 ,4-Dioxane Acetone Methanol DMF

Figure 1. Influence of the solvent on the Mo LDH EG catalyzed peroxidation of citro- nellol, showing: total time in hours (h) for hydrogen peroxide disproportionation.

Example 20:

Comparative experiment:

Advantage of the Mo LDH EG catalyst over the unmodified Mo LDH catalyst

The effect of the EG modification of the Mo LDH catalyst surface on the peroxidation of citronellol is shown in figure 2. The data show the total time for hydrogen peroxide disproportionation.

Reaction conditions: 0.5 g of Mo LDH or Mo LDH EG (Mg/AI = 2, 0.2 mmol of Mo/g, ethylene glycol for 12 h at 80 ⁰ C), 10 mmol of citronellol, 40 mmol of H ₂ O ₂

(50% by wt.) added in 5 mmol portions, 10 ml DMF, 25°C. Selectivity > 99% in both cases.

Figure 2

Mo LDH Mo LDH EG

Example 21 :

Comparative example

Advantage of the Mo LDH EG catalyst over sodium molybdate catalyst and MO

LDH catalyst at a reaction temperature of 60 ⁰ C

Oxidation of citronellol at a reaction temperature of 60 ⁰ C is shown in figure 3. The catalysts used were MoO ₄ ^2' (■), Mo LDH (o) and Mo LDH EG (•) in 1 ,4-dioxane. Reaction conditions: Mo LDH and Mo LDH EG: 0.1 g of Mo LDH or Mo LDH EG (Mg/AI = 2, 0.2 mmol of Mo/g, treated with EG for 5 days at 80 ⁰ C), 10 mmol of citronellol, H ₂ O ₂ (50% by wt.) added in 5 mmol portions, 20 ml of 1 ,4-dioxane, 60 ⁰ C. MoO ₄ ^2" : Same conditions except 0.1 mmol of Na ₂ MoO ₄ and 0.5 mmol of NaOH were added.

Figure 3

2 4 6 8 10

H ₂ OzI citronellol [mol / mol]

Example 22: Oxidation of citronellol with catalyst recycling.

In a 500 ml jacketed vessel with thermostat control, 50 g of β-citronellol (94%; remainder impurities) were dissolved in 180 ml of methanol and 5.0 g of Mo LDH EG catalyst were added. 50% H ₂ O ₂ was then metered in slowly with good stirring by means of a perfusor pump (9.2 ml/h corresponded to 0.5 mol.equiv./h). The temperature was kept constant at 25 ⁰ C. The progress of the reaction was observed by means of gas chromatography.

On completion of reaction (99% conversion), the catalyst was filtered off and used for the next batch without further purification or drying.

The reaction was repeated several times in this way. It was found that the catalyst did not lose activity and selectivity to a significant degree when it is used repeatedly. The results are reproduced below in the figure.

Mo LDH EG-catalyzed Oxidation of Citroneflol

3

Reaction number

Example 23: Oxidation of linalool

A 2000 liter jacketed vessel was charged with 1400 ml of methanol, and 1 mol% of catalyst (based on linalool) and 200 g (240 ml) of linalool were added. With good stirring, 358.8 g (300 ml) of 50% hydrogen peroxide were added at 25°C within 8 hours. The reaction progress was monitored by means of GC.

Conversion: >95% (Table)