CATALYTIC PROCESS FOR PREPARING CYCLOHEXANONE-OXIME

Abstract: A catalytic process for preparing cyclohexanone-oxime by reacting cyclohexanone with NH₃ and H₂O₂ in the liquid phase, wherein the catalyst substantially consists of a highly crystalline substance containing SiO₂ and having a zeolitic structure.

Description: EP-A-4676 describes a direct process for the production of oximes, among others cyclohexanone-oxime, wherein a mixture of ketone, ammonia and oxygen is contacted, at a temperature of from 50° to 500°C, with a solid catalyst having a certain surface area. Preferred catalysts are, among many others, ca­ talysts comprising silica and/or zirconia and/or an oxide of a transition metal of Group 3-8 of the Periodic Table. DE-C-1 245 371 teaches the preparation of cyclohexanone-­ oxime by catalytic reaction, in the liquid phase, of cyclo­ hexanone with ammonia and hydrogen peroxide at 5 to 40°C, in the presence of a catalyst consisting of phospho-tungstic acid or of similar compounds. A drawback of this method is, however, that this type of catalyst is difficult to handle, particularly, during the separation of the product from the catalyst. It has now been found that it is possible to obtain the same high yields by using a completely different catalyst that is easier to handle and simplifies the process in all its steps. Thus, the present invention relates to a catalytic process for preparing cyclohexanone-oxime by reacting cyclohexanone with NH₃ and H₂O₂ in the liquid phase at a temperature of from 25 to 100°C and at a pressure equal to or higher than atmos­ pheric pressure, which process is characterized in that the catalyst substantially consists of a highly crystalline, SiO₂-containing substance having a zeolitic structure and, in particular, of a titanium-silicalite, optionally in admix­ ture with an inert binder. Titanium-silicalites are known com­ pounds which, for example, are described in GB-A-2 024 790 and 2 071 071. The reaction temperature preferably is in the range of from 40 to 90°C. Tests carried out at 15°C have provided results that are not completely satisfactory. A pressure above atmospheric pressure is preferred since it promotes the development of the reaction. Other substances of zeolitic nature which catalyse the reaction are, first of all, the various types of silicalite, such as silicalite I (see, e.g., US-A-4 061 724), silicalite II, zirconium-silicalites and hafnium-silicalites. Another class of analogous catalysts are the metal­ silicalites, e.g., borosilicates (boralites), beryllo­ silicates, chromo-silicates, vanadium-silicates, zirconium­ silicates, gallium-silicates and ferro-silicates which are, in part, described in GB-A-2 024 790. A third class of catalysts of analogous type consists of the known aluminium-silicates, generally known as "zeolites", particularly the zeolites of type Y, the zeolites ZSM5, the zeolites ZSM 11 and the other zeolites ZSM described in EP-A-129 239, 141 514 and 143 642, as well as the zeolites MB 28 described in EP-A-21 445. Some of these zeolites have already been successfully utilized in the aminoximation of cyclohexanone in the gas phase with NH3 and air. According to another preferred embodiment of the process of the present invention the titanium-silicalite mentioned above is replaced, at least in part, by a zirconium-silicalite or a boralite. The process according to the present invention can be carried out either continuously or discontinuously, provided that reactors with surfaces that are resistant to hydrogen peroxide are used. When the reaction is carried out in batch , it is advisable that 0.1 to 50 parts by weight (preferably from 1 to 20 parts by weight) of pure catalyst (excluding binder) for 100 parts by weight of cyclohexanone be used. If the reaction is performed in a continuous manner, it is preferred to employ a space velocity of from 0.1 to 100 kg/h of cyclohexanone (C₆H 10 O) per kg of catalyst. The molar ratio of H₂O₂:C₆H 10 O is, generally, in the range of from 0.5 to 2.5 and, preferably, from 1 to 1.5, whereby H₂O₂ means 100% pure hydrogen peroxide (i.e., dilution water excluded). Water (H₂O) is the most suitable liquid vehicle for the reaction. However, it is also possible to use or­ ganic water-soluble solvents capable of dissolving both pure ammonia and its aqueous solutions such as, e.g., methanol, ethanol, propanol, isopropanol, butanol, isobutanol, tertiary butanol and mixtures thereof. Solvents with car­ bonyl functions such as aldehydes and ketones should be excluded. The reaction water, which is formed according to the equation: gradually increases the amount of liquid vehicle as the con­ version to oxime proceeds. During the reaction conside­ rable amounts of peroxy-di-cyclohexyl-amine of the formula are also formed. Ammonia should always be added before the hydrogen peroxide and in excess (NH₃: C₆H 10 O≧1, preferably ≧1.5 moles/mol). Otherwise, undesired side-reactions occur. At the end of the reaction, the cyclohexanone-oxime can be separated by different methods, for example, through extrac­ tion with suitable solvents such as benzene, toluene and the cyclohexanone as used for the synthesis, whereby a hydropho­ bic organic phase and an aqueous phase are formed. Cyclo­ hexanone-oxime and unreacted cyclohexanone form the organic layer. The aqueous layer which contains the excess NH₃ as well as traces of cyclohexanone and oxime can be re­ cycled to the reaction zone (ammoximation zone). The following examples illustrate the invention without, however, limiting it. EXAMPLE 1 A glass reactor, equipped with a stirrer and a heating jacket, was first blanketed with an inert gas (nitrogen). Subse­ quently, 1.5 g of a catalyst consisting of a finely ground powder of titanium-silicalite containing 3.85% by weight of highly crystalline titanium oxide (average diameter of the particles ≦5 µm) was charged. 50 ml of a 32% by weight aqueous solution of ammonia were added to the catalyst. The mixture was stirred and 9.5 g of cyclohexanone were charged. The three-phase system (solid-aqueous-organic) formed was kept homogenous by stirring vigorously. Heating was started by conveying a liquid at 60°C into the jacket. Simulta­ neously, a 32% by weight aqueous solution of hydrogen per­ oxide was fed to the reactor by means of a metering pump. After 15 minutes, the temperature in the reactor reached 60°C while the pressure rose to a value of from 80 to 93 KPa (600 to 700 mm Hg) above atmospheric pressure. The addition of H₂O₂ was performed within 3.5 hours, during which time the pressure decreased. The temperature was maintained at 60°C and stir­ ring was continued for a further 1.5 hours, whereafter the test was stopped and the mixture was cooled. 50 ml of toluene were added to the resulting suspension and, after stirring for a few minutes, the aqueous phase and the organic phase were separated from the catalyst by filtration. The liquid phases were separated in a separation funnel and the aqueous phase was extracted with two portions of toluene of 30 ml each. The toluene solutions were com­ bined and analysed. The analysis revealed a cyclohexanone conversion of 95% and a selectivity to cyclohexanone-oxime , of 79.45%; the selectivity of hydrogen peroxide to oxime was 68.7%. At the end, about 15% of the starting cyclo­ hexanone was found to be in the form of peroxy-dicyclohexyl­ amine (see formula II above). EXAMPLES 2 (Comparative Test) and 3 Example 1 was repeated, varying temperature and pressure. The data and results given in table 1 prove that the selec­ tivity of the conversion H₂O₂ → oxime is very ad­ versely affected when operating under vacuum. EXAMPLE 4 (Comparative Test) Example 1 was repeated, bringing the pressure (gauge) to zero and considerably lowering the temperature (down to 15°C). The unsatisfactory results shown in table 1 prove that it is disadvantageous to excessively reduce the thermal level of the ammoximation. EXAMPLE 5 Example 1 was repeated, replacing titanium silicalite by a zirconite (zirconium-silicalite). Analogous results were obtained. EXAMPLE 6 Example 1 was repeated, replacing titanium-silicalite by a boralite (boron-silicate). Analogous results were obtained.

Claims: 1. A catalytic process for preparing cyclohexanone-oxime by reacting cyclohexanone with ammonia and hydrogen peroxide in the liquid phase at a temperature of from 25 to 100°C and at a pressure equal to or higher than atmospheric pres­ sure, characterized in that the catalyst substantially con­ sists of a highly crystalline substance containing SiO₂ and having a zeolitic structure. 2. The process of claim 1, wherein the catalyst is a titanium­ silicalite, optionally in admixture with an inert binder. 3. The process of claim 1 and/or claim 2, wherein a zirconium­ silicalite replaces, at least in part, titanium-silicalite. 4. The process of claim 1 and/or claim 2, wherein a boralite replaces, at least in part, titanium-silicalite. 5. The process of any one of claims 1 to 4, wherein the reac­ tion temperature ranges from 40 to 90°C. 6. The process of any one of claims 1 to 5, wherein the space velocity of cyclohexanone ranges from 0.1 to 100 kg/h per kg of pure catalyst (binder excluded). 7. The process of any one of claims 1 to 6, wherein the H₂O₂: C₆H 10 O molar ratio ranges from 0.5 to 2.5, where H₂O₂ means pure hydrogen peroxide (dilution water excluded). 8. The process of any one of claims 1 to 7, wherein NH₃ is added prior to H₂O₂, the NH₃: C₆H 10 O molar ratio being ≧1, preferably ≧1.5.

Inventors: DE ALBERTI, GIORDANO, MORETTI, ENRICO, PADOVAN, MARIO, ROFFIA, PAOLO
Applicants: MONTEDIPE S.R.L.
Application year: 1986
Main classification: C07C249
IPC codes: C07C251, C07B61, C07D271, B01J21, C07C249, C07C67, C07C239, B01J29