Process for producing epsilon-caprolactam

Abstract: ε-caprolactam is produced by gas phase reaction of cyclohexanone oxime using a solid acid as a catalyst in the presence of a compound represented by the formula (I): R¹-O-R² (wherein R¹ represents a lower alkyl group which may be substituted with fluorine and R² represents a hydrogen atom, a lower alkyl group or a phenyl group) such as a lower alcohol or an ether compound. The solid acid includes a crystalline metallosilicate or a crystalline silicate.

Description: The present invention relates to a process for producing ε-caprolactam from cyclohexanone oxime using a solid acid as a catalyst under conditions of gas phase reaction. ε-caprolactam is an important raw material for nylon and the like. One of the processes for producing caprolactam is liquid phase rearrangement of cyclohexanone oxime using fuming sulfuric acid or concentrated sulfuric acid as a catalyst. However, the above process has problems in that a large amount of fuming sulfuric acid is required and besides ammonium sulfate is produced in large amounts as a byproduct. As an approach to solve these problems, various processes have been proposed according to which cyclohexanone oxime is rearranged in the gas phase using a solid acid as a catalyst. For example, there has been proposed use of boric acid catalyst (Japanese Published Unexamined Patent Application No. 37686/78 and Japanese Published Examined Application No. 12125/71), silica alumina catalysts (British Patent No. 831,927), solid phosphoric acid catalyst (British Patent No. 881,926), mixed metal oxide catalysts (Journal of the Chemical Society of Japan, No. 1, 77, 1977), and zeolite catalysts (Journal of Catalysis, 6 , 247, 1966 and U.S. Patent No. 4,359,421). However, the above processes have problems in reaction selectivity of the objective ε-caprolactam, life of catalysts, productivity per catalyst and quality of the product ε-caprolactam. For example, U.S. Patent No. 4,359, 421 discloses an example of using a crystalline zeolite such as ZSM-5 having an atomic ratio of Si/Al of 40-60 and mentions that conversion of cyclohexanone oxime is quantitative, but is silent about selectivity of ε-caprolactam. Besides, it shows a short catalyst life of 15-20 hours. The present inventors have also studied use of ZSM-5 zeolite having the Si/Al atomic ratio as mentioned in the above patent and have found that not only the life of catalyst, but the selectivity of ε-caprolactam are not enough. U.S. Patent Nos. 4,709,024 and 4,717,769 show use of a crystalline aluminosilicate having an Si/Al atomic ratio of at least 500 and an acid amount on external surface of less than a specific value and a crystalline metallosilicate having an Si/metal atomic ratio of at least 500. Selectivity of these catalysts has been considerably improved as compared with conventional silica catalysts. Furthermore, U.S. Patent No. 4,717,770 discloses that when crystalline zeolite catalysts are surface treated with an organometallic compound, selectivity can be improved. DE-A-1955559 and DE-A-2059703 are both concerned with the same technical problem DE-A-2059703 being a patent of addition to DE-A-1955559. The problem with which they are concerned results from the catalyst which both cases use, namely acid catalyst containing boric acid. The problem is that an incrustation consisting of boric acid, catalyst dust and reaction products of the oximes occurs under the rearrangement conditions in certain parts of the apparatus used to carry out the reaction. DE 1955559 is a method for continuous production of lactams by rearrangement of cycloalkanonoximes at 210 to 450°C with carrier catalysts in a fluidized bed, and it advocates the introduction of 0.01 to 1kg of water vapour per kg of delivered cycloalkanonoxime into the reaction chamber above the fluidized bed to overcome the said problem. DE 2059703 states that deposits are avoided but the boric acid is extracted and condensed together with the raw lactam. DE 2059703 accordingly advocates replacing the water with oxy compounds interalia exemplified by C₁ - C₄ alkanols or 0-formic acid ester. According to the present invention a process for producing ε-caprolactam comprises carrying out gas phase reaction of cyclohexanone oxime using a solid acid as a catalyst characterised in that the reaction is carried out in the presence of a compound represented by the formula (I): R¹-O-R² (I) wherein R¹ represents a C₁-C₆ alkyl group which may be substituted with fluorine and R² represents a hydrogen atom, a C₁-C₆ alkyl group or a phenyl group, the compound of the formula (I) being present in an amount of 0.1-20 times as much as the weight of cyclohexanone oxime, and in that the solid acid catalyst is crystalline metallosilicate or crystalline silicate and in that the reaction is carried out at a temperature of 250-500°C. The present invention will be explained in detail. When a crystalline metallosilicate is used it preferably has an Si/Me atomic ratio (wherein Me preferably represents at least one metallic element selected from Al, Ga, Fe, B, Zn, Cr, Be, Co, La, Ge, Ti, Zr, Hf, V, Ni, Sb, Bi, Cu, Nb, and the like) of at least 5, e.g. at least 50 or 90 or 100, or 360 or preferably at least 1400, or at least 7000 or at least 9000 or as high as 147000, or more. When a crystalline silicate is used it preferably comprises silicon dioxide containing substantially no Me component. The Si/Me ratio can be obtained by usual analytical means such as atomic absorption spectrometry and X-ray fluorescence analysis. These catalysts are prepared by known processes. These crystalline metallosilicates and crystalline silicates are known to have various crystal forms and especially preferred are those which belong to so-called pentasil type structure. In the present invention, a compound represented by the formula R¹-O-R² (I) (wherein R¹ represents a C₁-C₆ alkyl group (hereafter lower alkyl) which may be substituted with fluorine and R² represents a hydrogen atom, a lower alkyl group or a phenyl group) is present in the reaction system. As example of R¹ in the formula, mention may be made of such as methyl, ethyl, propyl, butyl, amyl, hexyl, monofluoroethyl, difluoroethyl, trifluorethyl, and hexafluoroisopropyl. Examples of R² in the formula include a hydrogen atom, and groups such as methyl, ethyl, propyl, butyl, amyl and hexyl, and a phenyl group. As examples of the compounds represented by the formula (I), mention may be made of lower alcohols having a hydrogen atom as R² and ether compounds having a lower alkyl group or phenyl group as R². As the lower alcohols, there may be used, for example, one or more of methanol, ethanol, n-propanol, isopropanol, n-butanol, sec-butanol, isobutanol, n-amyl alcohol, n-hexanol, and 2,2,2-trifluoroethanol. Especially, use of one or more of methanol, ethanol, n-propanol, isopropanol, and n-butanol results in remarkable improvement of the selectivity of ε-caprolactam and the life of catalyst and thus these are more preferred. Methanol and ethanol are especially preferred because of their remarkable effect and from the industrial viewpoint. As the ether compounds, there may be used, for example, one or more of dimethyl ether, methyl ethyl ether, diethyl ether, methyl n-propyl ether, methyl isopropyl ether, methyl tert-butyl ether and anisole. Especially, use of one or more of the ether compounds having methyl group as R¹ results in remarkable improvement of selectivity of ε-caprolactam and the life of the catalyst and thus these are more preferred. Usually, the process of the present invention is carried out under atmospheric pressure or reduced pressure lower than atmospheric pressure. The method for reaction preferred for use in the practice of the present invention will now be explained. The reaction is preferably carried out by a gas phase catalytic method in a fixed-bed or fluidized bed. The starting material cyclohexanone oxime is brought in the gas form into contact with the catalyst bed. The formula (I) compound, e.g. the lower alcohol or ether compound can be previously mixed in the gas phase with the cyclohexanone oxime or can be fed to a reactor separately from the cyclohexanone oxime. In case of a fixed-bed, it is preferred to pass the cyclohexanone oxime and lower alcohol or ether compound which are well mixed with each other through the catalyst bed. In case of a fluidized bed, the cyclohexanone oxime and lower alcohol or ether compound are not always necessarily previously mixed and can be separately fed from each other and besides, the lower alcohol or ether compound can be divisionally added e.g. in portions. Furthermore, in the case of a fluidized bed, the lower alcohol or ether compound may be added at a position upstream of the position of addition of the cyclohexanone oxime. The amount of lower alcohol to be present in the reaction system is preferably 0.1-20 times, preferably 10 times or less, more preferably 0.3-8 times as much as the weight of the cyclohexanone oxime. The amount of the ether compound to be present in the reaction system is preferably 0.1-20 times, more preferably 0.3-15 times as much as the weight of the cyclohexanone oxime. In the present invention, vapour of a compound inert to the reaction such as benzene, cyclohexane or toluene or an inert gas such as nitrogen or carbon dioxide may be present as a diluent gas in the reaction system. The reaction temperature is in the range of 250-500°C. If the reaction temperature is lower than 250°C, the reaction rate tends to be less and the selectivity of ε-caprolactam tends to decrease. If it is higher than 500°C, the selectivity of ε-caprolactam tends to decrease since thermal decomposition of cyclohexanone oxime cannot be ignored. An especially preferred range is 300-450°C, and most preferred is 300-400°C. The preferred space velocity (WHSV) of the starting material cyclohexanone oxime is 0.1-40 hr ⁻¹ (i.e. feeding speed of cyclohexanone oxime per 1 kg of catalyst is 0.1-40 kg/hr). It is preferably 0.2-20 hr ⁻¹, more preferably 0.5-10 hr ⁻¹. Isolation of ε-caprolactam from the reaction mixture can be carried out by customary methods. For example, ε-caprolactam can be obtained by cooling and condensing the reaction mixture gas and then purifying it by extraction , distillation, crystallization or the like. The lower alcohol or ether compound added to the rearrangement reaction system can be recovered from the reaction mixture and reused. Catalyst which has become reduced in activity due to long-term use thereof can be easily activated to the original activity by calcining it in a gas stream containing oxygen gas and thus can be repeatedly used. As explained in detail above, according to the present invention, ε-caprolactam can be produced with very high selectivity even under the conditions where the conversion of cyclohexanone oxime is substantially about 100% and in addition the life of catalyst can be markedly improved as compared to conventional processes. Besides, alcohol or ether compound added to the reaction system can be recovered and used repeatedly. The following examples are given for the purpose of illustration only. Reference Example 1 (Preparation of catalyst A) Tetraethylorthosilicate (Si(OC₂H₅)₄, 100g, Al content ≦10 ppm), 224.0g of 10% aqueous solution of tetra-n-propylammonium hydroxide and 214g of ethanol were charged into a 1.5 litre stainless steel autoclave and vigorously stirred for 30 minutes. The mixed solution had a pH of 13. The autoclave was tightly sealed and then dipped in an oil bath to keep the internal temperature at 105°C. Hydrothermal synthesis was carried out for 120 hours with stirring at at least 400 r.p.m. Pressure in the autoclave reached 2-3 kg/cm². pH at completion of the hydrothermal synthesis was 11.8. A white solid product was filtered off and washed continuously with distilled water until the pH of the filtrate reached about 7. The white solid was dried and then was calcined at 500-530°C for 4 hours in an air stream to obtain 27g of powdery white crystals. The crystals were identified to be pentasil type zeolite by powder X-ray diffraction. Si/Al atomic ratio was 147000 according to atomic absorption spectroscopy assay. To 10g of the crystals was added 100g of 5% aqueous ammonium chloride solution and ion exchange treatment was carried out at 50-60°C for 1 hour and then the crystals were filtered off. This ion exchange treatment was carried out four times and then the crystals were washed with distilled water until no Cl⁻ was detected and the crystals subsequently dried at 120°C for 16 hours. The thus obtained crystals of NH₄ form were pressed to the form of tablets, crushed and sieved to particles of 24-48 mesh (Tyler Series) (which have openings 710 to 297 microns across) and then calcined at 500°C for 1 hour in a nitrogen gas stream to obtain a catalyst which will be referred to as catalyst A. Reference Example 2 (Preparation of catalyst B) Tetraethylorthosilicate (Si(OC₂H₅)₄, 100g), 224g of 10% aqueous solution of tetra-n-propylammonium hydroxide and 60g of ethanol were charged into a 1.5 litre stainless steel autoclave and sufficiently stirred. To this mixed solution was added 48g of previously prepared aqueous aluminium sulfate solution [Al₂(SO₄)₃.18H₂O(20 mg)/water 48g], followed by vigorous stirring for 30 minutes. The mixed solution had a pH of 13. The autoclave was tightly sealed and then dipped in an oil bath to keep the internal temperature at 105°C. Hydrothermal synthesis was carried out for 120 hours with stirring at at least 400 r.p.m. Pressure in the autoclave reached 2-3 kg/cm². pH at completion of the hydrothermal synthesis was 11.8. A white solid product was calcined in the same manner as in Reference Example 1 to obtain powdery white crystals. The crystals were identified to be pentasil type zeolite by powder X-ray diffraction. Si/Al atomic ratio was 7000 according to atomic absorption spectroscopy assay. Thereafter, the crystals were subjected to ion exchange treatment and calcined in the same manner as in Reference Example 1 to obtain catalyst B. Reference Example 3 (Preparation of catalyst C) Solutions of raw materials having the following compositions were prepared. Solution A: Distilled water: 162g; Sulfuric acid: 16.7g; Al₂(SO₄)₃.18H₂O: 2.92g; (n-Pr)₄NBr: 20.8g. Solution B: Distilled water: 119.7g; Sodium silicate: 186.3g. Solution C: Distilled water: 281.7g; Sodium chloride: 70.7g. Solutions A and B were simultaneously added dropwise to solution C with vigorous stirring and were mixed. pH at completion of the mixing was 9.6. The mixture was charged into a 1.5 litre stainless steel autoclave. Hydrothermal synthesis was carried out for 20 hours at 160°C with stirring at at least 400 r.p.m. After cooling and filtration, sufficient repeated washing (with about 7 litre of distilled water) was carried out until no Cl⁻ ion was detected. The resulting white solids were dried at 120°C for 16 hours. Then, the crystals were calcined at 500-550°C for 4 hours in an air stream to obtain white powdery crystals. The crystals were identified to be pentasil type zeolite by powder x-ray diffraction. Si/Al atomic ratio was 50 according to atomic absorption spectroscopy assay. Thereafter, the crystals were subjected to ion exchange treatment and calcined in the same manner as in Reference Example 1 to obtain catalyst C. Reference Example 4 (Preparation of catalyst D) Solutions of raw materials having the following compositions were prepared. Solution A: Distilled water: 443g; Sulfuric acid: 45g; (n-Pr)₄NBR: 55.8g. Solution B: Distilled water: 320g; Sodium silicate: 453g. Solution C: Distilled water: 754g; Sodium chloride: 189g. Solutions A and B were simultaneously added dropwise to solution C with vigorous stirring and were mixed. pH at completion of the mixing was 9.5. The mixture was charged into a 3 litre stainless steel autoclave. Hydrothermal synthesis was carried out for 20 hours at 160°C with stirring at least 350 r.p.m. After cooling and filtration, sufficient repeated washing (with about 15 litre of distilled water) was carried out until no Cl⁻ ion was detected. The resulting white solids were calcined in the same manner as in Reference Example 1 to obtain white powdery crystals. The crystals were identified to be pentasil type zeolite by powder X-ray diffraction. Si/Al atomic ratio was 100 according to atomic absorption spectroscopy assay. Thereafter, the crystals were subjected to ion exchange treatment and calcination in the same manner as in Reference Example 1 to obtain catalyst D. Reference Example 5 (Preparation of catalyst E) Solutions of raw materials having the following compositions were prepared. Solution A: Distilled water: 150g; (n-Pr)₄NBr: 81g; Colloidal silica (SI-30): 118.8g. Solution B: Distilled water: 150g; Sodium hydroxide: 76.5g. Solution B was added dropwise to solution A and mixed. The mixture was charged into a 1 litre stainless steel autoclave and hydrothermal synthesis was carried out for 24 hours at 160°C with stirring. After cooling, the product was filtered off and continuously washed with distilled water until the pH of the filtrate became neutral. The resulting white solids were calcined in the same manner as in Reference Example 1 to obtain powdery crystals. The crystals were identified to be pentasil type zeolite by pwoder x-ray diffraction. Si/Ai atomic ratio was 1400 according to atomic absorption spectroscopy assay. Thereafter, the crystals were subjected to ion exchange treatment and calcination in the same manner as in Reference Example 1 to obtain catalyst E. Reference Example 6 (Preparation of catalyst F) In a 1.5 litre stainless steel autoclave were charged 217.5g of 10% aqueous solution of tetra-n-propyl-ammonium hydroxide, 214g of ethanol, 2 ml of aqueous solution containing 64.2 mg of zirconium oxynitrate and 100g of high purity tetraethylorthosilicate (Si(OC₂H₅)₄) in this order, followed by sufficient stirring for 1 hour. The internal temperature was kept at 105°C and hydrothermal synthesis was carried out for 48 hours with stirring at at least 400 r.p.m. The resulting white solid product was filtered off and washed continuously with distilled water until the pH of the filtrate became neutral. The crystals were dried at 120°C for 16 hours. The dried crystals were calcined at 500-550°C for 4 hours in an air stream to obtain 27g of powdery white crystals. The crystals were identified to be zirconosilicate having structure similar to pentasil type zeolite by powder X-ray diffraction. Si/Zr atomic ratio was 2400 according to atomic absorption spectroscopy assay. Thereafter, the crystals were subjected to ion exchange treatment and calcination in the same manner as in Reference Example 1 to obtain catalyst F. Reference Example 7 (Preparation of catalyst G) White crystals were obtained by hydrothermal synthesis, filtration and calcination in the same manner as in Reference Example 6 except that 1.414g of titanium tetraisopropoxide was used in place of the zirconium oxynitrate. The crystals were identified to be crystalline silicate having the structure similar to that of pentasil type zeolite by powder x-ray diffraction. Si/Ti atomic ratio was 90 according to atomic absorption spectroscopy assay. Subsequently, the crystals were subjected to ion exchange treatment and calcination in the same manner as in Reference Example 1 to obtain catalyst G. Reference Example 8 (Preparation of catalyst H) White crystals were obtained by hydrothermal synthesis, filtration and calcination in the same manner as in Reference Example 6 except that 30.2 mg of vanadium trichloride was used in place of the zirconium oxynitrate. The crystals were identified to be crystalline silicate having structure similar to that of pentasil type zeolite by powder X-ray diffraction. Si/V atomic ratio was 2300 according to atomic absorption spectroscopy assay. Then, the crystals were subjected to the same ion exchange treatment and calcination as in Reference Example 1 to obtain catalyst H. Reference Example 9 (Preparation of catalyst I) Aerosil (amorphous silica of high purity, 45.0g), 45.73g of tetra-n-propylammonium bromide, 10.8g of sodium hydroxide and 375.81g of distilled water were charged into a 1.5 litre stainless steel autoclave. The autoclave was tightly sealed, followed by vigorous stirring at 20°C for 120 hours. The mixed solution had a pH of 12.8. The internal temperature was kept at 105°C and hydrothermal synthesis was carried out for 96 hours with stirring at at least 400 r.p.m. A white solid product was filtered off and washed continuously with distilled water until the pH of the filtrate became neutral. The white solid product was calcined in the same manner as in Reference Example 1 to obtain white powdery crystals. The crystals were identified to be pentasil type zeolite by powder X-ray diffraction. Si/Al atomic ratio was 360 according to atomic absorption spectroscopy assay. Thereafter, the crystals were subjected to ion exchange treatment and calcination in the same manner as in Reference Example 1 to obtain catalyst I. Reference Example 10 (Preparation of catalyst J) Tetraethylorthosilicate (Si(OC₂H₅)₄, 104.17g), 232.85g of 10% aqueous solution of tetra-n-propylammonium hydroxide, 62.33g of ethanol, and 50.44g of distilled water were charged into a 1.5 litre stainless steel autoclave and vigorously stirred for 30 minutes. The mixed solution had a pH of 12.5. The autoclave was tightly sealed and then dipped in an oil bath to keep the internal temperature at 105°C. Hydrothermal synthesis was carried out for 96 hours with stirring at at least 400 r.p.m. Pressure in the autoclave reached 2-3 kg/cm². pH at completion of the hydrothermal synthesis was 11.7. A white solid product was calcined in the same manner as in Reference Example 1 to obtain white powdery crystals. The crystals were identified to be pentasil type zeolite by powder X-ray diffraction. Si/Al atomic ratio was 9000 according to atomic absorption spectroscopy assay. The crystals were subjected to ion exchange treatment and calcination in the same manner as in Reference Example 1 to obtain catalyst J. EXAMPLE 1 Catalyst A (0.3g, 0.5 ml) was packed in a quartz glass reaction tube of 1 cm inner diameter and was preheated in a nitrogen stream at 350°C for 1 hour. Then, a mixed solution of cyclohexanone oxime/methanol/benzene = 1/2.3/11.5 (weight ratio) was fed to the reaction tube at a feeding rate of 11.5g/hr to carry out reaction. Space velocity WHSV was 2.6 hr⁻¹ and the temperature of the catalyst bed (reaction temperature) was 350°C. Reaction product was trapped and collected under water-cooling every hour and analyzed by gas chromatography. Methanol was recovered at at least 98% in all analyses. The results are shown in Table 1. Time lapsed (hr) Conversion (%) Selectivity (%) 1.25 99.4 89.2 3.25 99.0 92.3 6.25 98.7 91.2 The space velocity WHSV is the value calculated by the following formula and conversion of cyclohexanone oxime and selectivty of ε-caprolactam are calculated by the following formulas, respectively. WHSV (hr⁻¹) = feeding rate of cyclohexanone oxime (kg/hr) / weight of catalyst (kg) Conversion (%) of cyclohexanone oxime = {(X-Y)/X} x 100 Selectivity (%) of ε-caprolactam = {Z/(X-Y)} x 100 In the above formulas, X, Y and Z are as follows: X = Mols of the starting cyclohexanone oxime fed. Y = Mols of unaltered cyclohexanone oxime recovered. Z = Mols of -caprolactam in the product. EXAMPLES 2 to 8 The catalysts obtained in the reference examples were respectively subjected to preheating treatment in the same manner as in Example 1 and reactions were carried out using 0.3g (0.5 ml) of each of the preheated catalysts at the same weight ratio of cyclohexanone oxime/methanol/benzene, feeding rate of the mixed solution and reaction temperature as in Example 1. The results of the reactions are shown in Table 2. Example Catalyst WHSV (hr⁻¹) Time lapsed (hr) Conversion (%) Selectivity (%) 2 B 2.7 2.25 99.4 87.4 6.25 98.0 87.8 3 C 2.6 2.25 80.9 78.2 6.25 44.8 75.0 4 D 2.6 1.25 97.5 81.6 6.25 73.2 79.5 5 E 2.6 1.25 97.8 84.6 6.25 90.6 84.5 6 F 2.8 1.25 99.8 95.5 3.25 99.8 95.4 7 G 2.7 1.25 98.2 83.3 6.25 91.7 84.8 8 H 2.6 3.25 91.1 89.0 6.25 88.4 92.2 Comparative Examples 1 to 8 Example 1 was repeated except that methanol was not present in the reaction system and a mixed solution of cyclohexanone oxime/benzene = 1/11.5 (weight ratio) was fed to the reaction tube at a feeding rate of 11.5g/hr and reaction was carried out at 350°C. The results are shown in Table 3. Comparative Example Catalyst WHSV (hr⁻¹) Time lapsed (hr) Conversion (%) Selectivity (%) 1 A 3.1 3.25 100 79.6 6.25 97.8 81.3 2 B 3.1 1.25 99.8 78.1 6.25 89.7 81.8 3 C 3.3 2.25 16.8 55.8 6.25 8.0 43.9 4 D 3.1 1.25 96.4 62.6 6.25 39.1 72.4 5 E 3.1 1.25 89.5 70.2 5.25 67.9 70.1 6 F 3.1 1.25 100 82.9 6.25 98.3 88.2 7 G 3.1 1.25 100 74.6 6.25 87.7 81.5 8 H 3.1 3.25 100 83.9 6.25 96.9 84.8 EXAMPLE 9 In order to confirm reproducibility of catalyst preparation and rearrangement reaction of cyclohexanone oxime, a catalyst was prepared in the same manner as in preparation of catalyst A in Reference Example 1. (The obtained catalyst was referred to as "catalyst A*" hereinafter. Si/Al atomic ratio was 147000.). Using 0.3g (0.5 ml) of catalyst A*, reaction was carried out under the same conditions as in Example 1. The results are shown in Table 4. Time lapsed (hr) Conversion (%) Selectivity (%) 1.25 99.1 90.4 4.25 98.4 90.7 6.25 97.8 89.5 Comparative Example 9 Reaction was carried out under the same conditions as in Comparative Example 1 in the absence of methanol in the reaction system using catalyst A* in the same amount as in Example 9. The results are shown in Table 5. Time lapsed (hr) Conversion (%) Selectivity (%) 1.25 100 75.6 4.25 99.5 78.0 6.25 98.6 77.4 EXAMPLE 10 Reaction was carried out under the same conditions as in Example 1 except that benzene was not present in the reaction system, using the same amount of catalyst A* as in Example 9 by feeding a mixed solution of cyclohexanone oxime/methanol = 1/2 (weight ratio) to the reaction tube at a feeding rate of 3.0g/hr. WHSV was 3.3 hr⁻¹ and reaction temperature was 350°C. The results are shown in Table 6. Time lapsed (hr) Conversion (%) Selectivity (%) 1.25 99.7 87.7 3.25 99.6 85.5 6.25 99.7 86.3 EXAMPLE 11 As in Example 10, in the absence of benzene, reaction was carried out, using the same amount of catalyst A* as in Example 9 by feeding a mixed solution of cyclohexanone oxime/methanol = 1/13 (weight ratio) to a reaction tube at a feeding rate of 11.7 g/hr. WHSV was 2.8 hr⁻¹ and reaction temperature was 350°C. The results are shown in Table 7. Time lapsed (hr) Conversion (%) Selectivity (%) 1.25 63.3 84.2 6.25 36.5 86.3 EXAMPLES 12 to 16 Reaction was carried out at the same feeding rate and reaction temperature as in Example 1 except that catalyst A* was used in the same amount as in Example 9 and alcohols as shown in Table 8 were used in place of the methanol. The results are shown in Table 8. Example Alcohol Feeding ratio WHSV (hr⁻¹) Time lapsed (hr) Conversion (%) Selectivity (%) 12 Ethanol 1/1.6/909 3.1 2.25 99.0 91.8 6.25 99.0 91.2 13 n-Propanol 1/2.0/9.5 2.9 1.25 96.6 90.4 6.25 92.6 91.9 14 Isopropanol 1/2.0/9.5 2.9 1.25 99.8 87.9 4.25 99.5 91.8 15 n-Hexanol 1/7.3/6.5 2.6 1.25 59.8 87.2 3.25 40.2 82.1 16 2,2,2-Trifluoro ethanol 1/7.1/6.7 2.6 1.25 99.8 86.4 3.25 99.3 87.4 EXAMPLES 17 to 18 Reaction was carried out at the same feeding rate and reaction temperature as in Example 1, using catalyst A* in the same amount as in Example 9 with changing the feed ratio of cyclohexanone oxime/methanol/benzene (weight). The results are shown in Table 9. Example Feeding ratio WHSV (hr⁻¹) Time lapsed (hr) Conversion (%) Selectivity (%) 17 1/0.5/11.0 3.1 1.25 99.8 83.4 6.25 99.0 86.6 18 1/1.1/12.6 2.6 1.25 100 90.9 6.25 99.6 90.9 EXAMPLE 19 Catalyst A* (0.5g, 0.8 ml) was packed in a quartz glass reaction tube of 1 cm inner diameter and was preheated as in Example 1. Then, a mixed solution of cyclohexanone oxime/methanol/benzene = 1/1.1/10.4 (weight ratio) was fed to the reaction tube at a feeding ratio of 5.8 g/hr to carry out reaction. WHSV was 0.9 hr⁻¹ and reaction temperature was 350°C. The results are shown in Table 10. Time lapsed (hr) Conversion (%) Selectivity (%) 6.25 99.4 89.0 21.25 98.4 90.8 31.25 97.6 89.0 EXAMPLE 20 Catalyst I (0.348g, 0.58 ml) was packed in a quartz glass reaction tube of 1 cm inner diameter and preheated in nitrogen stream at 350°C for 1 hour. Then, a mixed solution of cyclohexanone oxime/methanol (weight ratio) = 1/1.86 was fed to the reaction tube in nitrogen stream (4.2 l/hr) at a feeding rate of 8.0 g/hr to carry out reaction. WHSV was 8.0 hr⁻¹ and reaction temperature was 350°C. Reaction product was trapped and collected by cooling with dry ice-methanol solution every hour and analyzed by gas chromatography. The results are shown in Table 11. Time lapsed (hr) Conversion (%) Selectivity (%) 1.25 100 94.3 3.25 100 91.1 6.25 100 93.6 Comparative Example 10 Reaction was carried out in the same manner as in Example 20 except that toluene was used in place of the methanol and a mixed solution of cyclohexanone oxime/toluene = 1/1.86 (weight ratio) was fed to the reaction tube at a feeding rate of 8.0 g/hr and the reaction temperature was 350°C. WHSV was 8.0 hr⁻¹. The results are shown in Table 12. Time lapsed (hr) Conversion (%) Selectivity (%) 1.25 98.8 75.7 3.25 94.8 84.8 6.25 86.7 87.1 EXAMPLE 21 Catalyst I (0.9g, 1.5 ml) was packed in a quartz glass reaction tube of 1 cm inner diameter and was preheated at 350°C under reduced pressure (30 Torr). Then, the pressure was adjusted to 80 Torr and a mixed solution of cyclohexanone oxime/methanol = 1/5 (weight ratio) was fed to the reaction tube at a feeding rate of 4.8 g/hr to carry out the reaction. WHSV was 0.9 hr⁻¹ and reaction temperature was 350°C. The reaction product was trapped and collected by ice-cooling every hour and analyzed by gas chromatography. The results are shown in Table 13. Time lapsed (hr) Conversion (%) Selectivity (%) 1.25 98.8 95.1 3.25 98.8 95.6 6.25 96.7 95.3 Comparative Example 11 Reaction was carried out in the same manner as in Example 21 except that toluene was used in place of the methanol and a mixed solution of cyclohexanone oxime/toluene = 1/5 (weight ratio) was fed to the reaction tube at a feeding rate of 4.8 g/hr and reaction temperature was 350°C. The results are shown in Table 14. Time lapsed (hr) Conversion (%) Selectivity (%) 1.25 100.0 78.5 3.25 99.8 84.4 6.25 95.0 88.6 EXAMPLE 22 Reaction was carried out in the same manner as in Example 21 except that catalyst J was used in place of the catalyst I. The results are shown in Table 15. Time lapsed (hr) Conversion (%) Selectivity (%) 1.25 99.6 95.4 3.25 98.8 95.9 6.25 97.6 96.2 Comparative Example 12 Reaction was carried out in the same manner as in Comparative Example 11 except that catalyst J was used in place of the catalyst I. The results are shown in Table 16. Time lapsed (hr) Conversion (%) Selectivity (%) 1.25 99.9 86.9 3.25 99.6 88.7 6.25 97.8 90.4 EXAMPLE 23 Catalyst B (0.3g, 0.5 ml) was packed in a quartz glass reaction tube of 1 cm inner diameter and preheated in a nitrogen stream at 350°C for 1 hour. Then, a mixed solution of cyclohexanone oxime/methyl tert-butyl ether/benzene = 1/3.1/10.6 (weight ratio) was fed to the reaction tube at a feeding rate of 11.5 g/hr to carry out reaction. WHSV was 2.7 hr⁻¹ and reaction temperature was 350°C. The reaction product was trapped and collected by water-cooling every hour and analyzed by gas chromatography. The results are shown in Table 17. Time lapsed (hr) Conversion (%) Selectivity (%) Yield (%) 1.25 98.7 82.1 81.0 3.25 98.3 84.6 83.2 6.25 90.6 88.6 80.3 Comparative Example 13 Reaction was carried out in the same manner as in Example 23 except that ether compound was not present in the reaction system and a mixed solution of cyclohexanone oxime/benzene = 1/11.5 (weight ratio) was fed to the reaction tube at a feeding rate of 11.5g/hr (WHSV = 3.1). The results are shown in Table 18. Time lapsed (hr) Conversion (%) Selectivity (%) Yield (%) 1.25 99.8 78.1 77.9 3.25 98.6 79.8 78.7 6.25 89.7 81.8 73.4 EXAMPLES 24 to 26 Reaction was carried out using the same catalyst as used in Example 23 in the same manner as in Example 23 except that ether compounds as shown in Table 19 were used in place of the methyl tert-butyl ether and feeding rate and feed ratio of raw materials as shown in Table 19 were employed. Reaction temperature was 350°C. The results are shown in Table 19. Example Ether compound Feeding ratio WHSV (hr⁻¹) Time lapsed (hr) Conversion (%) Selectivity (%) Yield (%) 24 Methyl n-propyl ether 1/2.6/11.1 1.6 1.25 99.7 80.0 79.8 3.25 95.3 88.1 84.0 25 Diethyl ether 1/2.6/11.1 2.6 1.25 100 79.5 79.5 6.25 97.3 82.6 80.4 26 Anisole 1/7.7/6.1 2.8 2.25 98.5 81.7 80.5 6.25 91.9 84.1 77.3

Claims: A process for producing ε-caprolactam which comprises carrying out gas phase reaction of cyclohexanone oxime using a solid acid as a catalyst characterised in that the reaction is carried out in the presence of a compound represented by the formula (I): R¹-O-R² (I) wherein R¹ represents a C₁-C₆ alkyl group which may be substituted with fluorine and R² represents a hydrogen atom, a C₁-C₆ alkyl group or a phenyl group, the compound of the formula (I) being present in an amount of 0.1-20 times as much as the weight of cyclohexanone oxime, and in that the solid acid catalyst is crystalline metallosilicate or crystalline silicate and in that the reaction is carried out at a temperature of 250-500°C. A process as claimed in claim 1 characterised in that the compound of the formula (I) is a C₁-C₆ alcohol in which R² represents a hydrogen atom. A process as claimed in claim 2 characterised in that the C₁-C₆ alcohol is methanol, ethanol, n-propanol, isopropanol or a mixture thereof. A process as claimed in claim 1, 2 or 3 characterised in that the compound of formula (I) is a C₁-C₆ alcohol and is present in an amount of 0.3-8 times the weight of the cyclohexanone oxime. A process as claimed in claim 1 characterised in that the compound of formula (I) is an ether compound in which R² represents a C₁-C₆ alkyl group or a phenyl group. A process as claimed in claim 5 characterised in that the ether compound if dimethyl ether, diethyl ether, methyl n-propyl ether, methyl tert-butyl ether, anisole or a mixture thereof. A process as claimed in claim 5 or claim 6 characterised in the ether compound is present in an amount of 0.3-15 times the weight of cyclohexanone oxime. A process as claimed in anyone of claims 1 to 7 characterised in that the solid acid catalyst is a crystalline metallosilicate which has an Si/Me atomic ratio of at least 5. A process as claimed in anyone of claims 1 to 8 characterised in that the crystalline metallosilicate or crystalline silicate has a pentasil type structure. A process as claimed in anyone of claims 1 to 9 characterised in that the solid acid catalyst is a metallosilicate and the metal is at least one metallic element selected from the group consisting of Al, Ga, Fe, B, Zn, Cr, Be, Co, La, Ge, Ti, Zr, Hf, V, Ni, Sb, Bi, Cu and Nb.

Inventors: ICHIHASHI HIROSHI, KITAMURA MASARU, NAKAMURA YASUO, SUZUKAMO GOHFU, ICHIHASHI, HIROSHI, KITAMURA, MASARU, NAKAMURA, YASUO, SUZUKAMO, GOHFU
Applicants: SUMITOMO CHEMICAL CO, SUMITOMO CHEMICAL COMPANY, LIMITED
Application year: 1990
Main classification: C07D201
IPC codes: C07D201