Process for producing propylene

Abstract: A process for the production of lower olefins by dehydrating lower alcohols having 2 to 4 carbon atoms which comprises using a γ-alumina catalyst containing 0.3% by weight or less of impurities in total excluding SiO₂, the impurities including 0.2% by weight or less of sulfur content calculated in terms of SO₄⁻⁻ and 0.05% by weight or less of sodium content calculated in terms of Na₂O, and/or a process for the production of lower olefins by dehydrating lower alcohols having 2 to 4 carbon atoms that comprises using a γ-alumina catalyst which contains 0.5 to 5% by weight of SiO₂. According to the process of the present invention, lower olefins can be produced from lower alcohols with high yield and high selectivity for a prolonged period of time without reducing the catalytic activity.

Description: This invention relates to a process for the production of propylene from propanol by dehydrating the alcohol using specified catalysts. Various processes have been proposed for the production of high purity olefins by means of dehydration of alcohols, for example, a process in which ethylene is produced by dehydrating ethanol in the presence of solid acid catalysts such as alumina, silica, silica-alumina, zeolites and solid phosphoric acid (Japanese Patent Application Kokai No. 64-34929). When dehydration is carried out using a solid acid as a catalyst, it is necessary to keep the reaction temperature at 250 to 300°C or higher because of the greatly endothermic alcohol dehydration reaction. In addition, application of solid acid catalysts such as silica alumina, zeolites and solid phosphoric acid is not desirable, because their strongly acidic nature causes a decrease in the yield of olefins due to heavy materials formed by polymerization of the formed olefins. The heavy material thus formed adheres to the catalyst surface and decreases the catalytic activity. In such an instance, γ-alumina may be used advantageously, because its weakly acidic nature does not entail polymerization of the formed olefins. However, the catalytic activity of γ-alumina decreases greatly over a prolonged period of time. That is a significant drawback in using γ-alumina to produce olefins. It is generally known that γ-alumina is transformed into the α form under high pressure or at a high temperature of 1000°C or more and that such a transition can be prevented by the addition of a metal oxide as a secondary component, such as La 2 O 3 , MgO or SiO 2 . However, it is difficult to apply such a prior art means for the prevention of high temperature crystal phase transition to a reaction system at a low temperature or around 300°C under a low pressure, because nothing is known about the phenomenon or mechanism of crystal phase transition under such conditions. Though it is possible to effect the hydration reaction without pressurization, such an operation requires complex handling because or the necessity to set additional process steps and is disadvantageous also from the economic point of view. That is, being gaseous under ambient temperature and pressure, lower olefins having 2 to 4 carbon atoms formed by the reaction must be liquefied prior to their purification by, for example, distillation, which requires cooling using a refrigerating machine or pressurization using a compressor. EP-A-379,803 discloses a process for preparing propylene which comprises dehydrating isopropanol in the presence of a γ-alumina catalyst having a mean pore diameter of from 3 to 15 nm with a standard deviation of from 1 to 4 nm based on a statistical calculation from pore diameter and pore volume. The γ-alumina preferably comprises up to 0.5% by weight of an alkali metal oxide. DE-A-3,017,501 discloses an activated alumina catalyst containing alkali metal, sulfur, iron and silicon in an amount of 0.05 wt% or less, respectively, calculated as Na 2 O, SO 3 , Fe 2 O 3 and SiO 2 and having a purity of 99.6 wt% or more. This catalyst is stated to have superior activity and selectivity when dehydrating ethanol to ethylene. In view of the above, it is a primary object of the present invention to provide a process by which propylene can be produced from propanol with high yield and high selectivity for a prolonged period of time using simple equipment. The present invention provides a process for producing propylene by the catalytic dehydration of propanol using a γ-alumina catalyst (A), wherein: a) the dehydration is carried out at a temperature of from 150 to 500°C and under such pressure that the propylene produced liquifies at ambient temperature; b) the catalyst (A) contains 0.3% by weight or less of impurities in total excluding SiO 2 , said impurities including 0.2% by weight or less of sulfur content calculated in terms of SO 4 -- and 0.03% by weight or less of sodium content calculated in terms of Na 2 O. The present invention also provides a process for producing propylene by the catalytic dehydration of propanol using a γ-alumina catalyst (B), wherein: a) the dehydration is carried out at a temperature of from 150 to 500°C and under such pressure that the propylene produced liquifies at ambient temperature; and b) the catalyst (B) contains 0.5 to 3% by weight of SiO 2 . The propanol to be used as the starting material includes n-propanol and i-propanol and mixtures thereof with each other. It was found for the first time by the inventors of the present invention that the catalytic activity of γ-alumina decreases greatly because of the transition of a moiety of its crystal phase from the γ form to the α form when used in a reaction system for a long period of time under pressure even at a low temperature of from 300 to 350°C. Since such a tendency becomes significant as the pressure increases, it is difficult to use γ-alumina as a catalyst in an industrial process under pressure. The present invention uses a specific catalyst in the dehydration reaction. The catalyst (A) is a γ-alumina catalyst which contains 0.3% by weight or less of impurities in total excluding SiO 2 , preferably 0.1% by weight or less. The sulfur content in the impurities is 0.2% by weight or less, preferably 0.1 % by weight or less, more preferably 0.06% by weight or less, calculated in terms of SO 4 -- and the sodium content in the impurities is 0.03% by weight or less, calculated in terms of Na 2 O. When the sum total of impurities such as Na, Fe and SO 4 ions, excluding SiO 2 , and sulfur and sodium contents of the impurities in a γ-alumina catalyst are restricted to within the aforementioned ranges, the catalyst is hardly converted into the α-form. Therefore its catalytic activity does not decrease even after its use in the dehydration reaction for a prolonged period of time at a temperature of from 150 to 500°C under pressure. In addition, a γ-alumina catalyst with reduced sodium content improves the yield in the dehydration reaction. Catalyst (B) used in the present invention contains SiO 2 in an amount of from 0.5 to 3% by weight. When the SiO 2 content is restricted to within this range, crystal phase transition of the catalyst from the γ-form into the α-form can be prevented. Therefore its catalytic activity does not decrease even after its use in the dehydration reaction for a prolonged period of time at a temperature of from 150 to 500°C under pressure. The features of catalysts (A) and (B) described above may be effected in a combined manner. γ-Alumina may be produced by any known method, provided that its impurity and/or SiO 2 contents are within the aforementioned ranges. For example, it may be produced from an acidic aluminium salt by mixing aluminium sulfate with sodium aluminate or by mixing aluminium sulfate with calcium carbonate, from an organic aluminum compound by the hydrolysis thereof or from an alumina hydrate by Bayer's process. When produced from an aluminium salt or from an alumina hydrate by Bayer's process, it is necessary to wash the aluminium hydrate with a sufficient volume of water at the time of its filtration in order to attain the aforementioned range of impurities in the resulting γ-alumina to be used in the present invention. In that instance, it is desirable to add ammonia to the washing water in a concentration of 0.5 to 25%, for the purpose of keeping the crystal form of the hydrate. When γ-alumina is produced from an alumina hydrate obtained by Bayer's process, removal of the sodium content is not so easy. For this reason, γ-alumina once obtained by baking of the hydrate is washed with a dilute aqueous solution of, for example, hydrochloric acid or acetic acid and then with water to remove the sodium content. By carrying out such handling steps, the amounts of impurities are reduced to predetermined levels. In order to avoid contamination of impurities, it is desirable to operate drying and baking steps in an atmosphere of, for example, nitrogen, air (pure air not including reactive gases) or an inert gas. Preferably, γ-alumina may be produced by a process in which the amounts of contaminated impurities can be reduced at the time of using the starting material. Especially, it is preferable to employ a process in which γ-alumina is prepared from an organic aluminium compound, because such a starting material does not contain Na and SO 4 ions. Examples of organic aluminium compounds include aluminium isopropoxide, aluminium ethoxide, aluminium tributoxide, triethyl aluminium and triisobutyl aluminium. Since trialkyl aluminium compounds are difficult to handle and dangerous because of the necessity to carry out an oxidation reaction, it is preferable to use an aluminium alkoxide as the starting material. Particularly preferred is aluminium isopropoxide, because it can be purified by distillation easily due to its low boiling point and because it is easily available. When aluminium isopropoxide is used as the starting material, γ-alumina may be produced by hydrolyzing the starting material under reflux after mixing it with isopropanol and water, washing the resulting precipitate with aqueous ammonia and then subjecting the washed precipitate to baking. Baking may be effected at such a temperature that the product becomes the γ-form, preferably from 550 to 650°C. On the other hand, for the purpose of including a predetermined amount of SiO 2 in the γ-alumina, SiO 2 is added during the production process of the γ-alumina or at the time of its use as a catalyst. Addition of SiO 2 may be carried out during any one step or steps of the production process of the γ-alumina. For example, an SiO 2 source may be added to, for example, boehmite or pseudo-boehmite which is a starting material for the γ-alumina, or to, for example, aluminium sulfate or sodium aluminate at the time of material preparation. It may also be added to the γ-alumina powder as a final product. In order to satisfy the effect of its addition, it is necessary to disperse the SiO 2 in the γ-alumina to a certain degree of uniformity. Any source of SiO 2 may be used, provided that it finally becomes in the form of SiO 2 . For example, the SiO 2 source may be added as a hydrogel or hydrosol of SiO 2 or as an alkyl compound such as ethylsilicate. It is desirable to prevent γ-alumina from contamination of other metal oxides such as La 2 O 3 and MgO, because the presence of such compounds deteriorates the catalyst quickly, though they are known to have an effect to prevent transition into the α-form at a high temperature. With regard to other physical properties of the γ-alumina, though not particularly limited, it preferably has a mean pore size of from 50 to 150 Å and a specific surface area of from 100 to 350 m 2 /g. The catalyst may be made into a powder form or a granular form, or used as a fixed bed by making it into a pellet form by tablet molding. Though not particularly required, the catalyst may be subjected to a pretreatment such as baking treatment. The reaction temperature is 150 to 500°C, preferably from 250 to 400°C. The reaction progresses with high yield within this temperature range, thus rendering possible industrial scale production. The reaction may, for example, be carried out under reduced, normal or pressurized pressure conditions. However, taking the aforementioned purification-related problem into consideration, The reaction is carried out under such a pressurized condition that the formed olefins liquify at ambient temperature. Preferred dehydration reaction conditions according to the process of the invention are as follows. The starting material may be fed into a reaction vessel at a rate of from 0.1 to 20 hr -1 , preferably from 0.5 to 10 hr -1 , in terms of LHSV (liquid hourly space velocity). A feeding rate of less than this would result in low productivity, thus requiring large equipment, and a rate of higher than this would result in a low reaction yield, thus requiring additional energy for separation and recovery of the resulting product. Feeding rates outside this range, therefore, are not economic. According to the process of the present invention, a gaseous material inert to the dehydration reaction may be used in order to discharge olefins formed by the reaction quickly from the reaction system. Examples of such gaseous materials include nitrogen, helium, argon, methane, ethane, propane and butane. In this instance, it is preferable to avoid the presence of water because of a possibility of enhancing crystal phase transition due to the presence of water. Also useful as the gaseous materials are those which are liquid before their feeding in a reactor but which become gaseous under the reaction conditions inside the reactor. Examples of such materials include: aliphatic hydrocarbons such as pentane, hexane, heptane, cyclopentane and cyclohexane; and aromatic hydrocarbons such as benzene, toluene, xylene, ethylbenzene and cumene. When the gaseous material is fed into a reactor vessel by mixing it with an alcohol, it is preferably used in an amount of from 0.05 to 10 moles per 1 mole of the alcohol. When the gaseous material is used in larger amounts than this, it is necessary to recycle the gaseous material by separating it from a mixture of an olefin with water as the reaction products, thus entailing economic disadvantages such as a high production cost of olefins. According to the process of the present invention, the reaction is preferably carried out in a continuous manner. As to the type of the reactor, it is preferable to employ a fixed bed system in which a catalyst is used in granular form. EXAMPLES The following Inventive and Comparative Examples further illustrate the present invention. The crystal phase transition of the γ-alumina catalyst was checked by the following simple means. (Steam Resistance Test of Catalyst) A 1 to 50 g portion of a catalyst was wrapped in a 200 mesh SUS 316 net and charged in a 2,000 cc capacity autoclave together with a coil-shaped filler (HELIPAK industrially available from TOKYO TOKUSHU KANAAMI K.K.) of SUS 316. The catalyst was set in the central position. After heating to 400°C using an electric furnace, water was fed into the autoclave using a high pressure pump and the pressure in the vessel was increased to 80 kg/cm 2 G. After 6 hours of treatment, the catalyst was taken out and subjected to X ray analysis to examine its crystal phase. When required, the thus treated catalyst was checked for its specific surface area and its activity as a catalyst for olefin production. (Preparation of Catalyst 1 - Catalyst A) Commercially available reagent grade aluminium isopropoxide was mixed with isopropanol and water and subjected to hydrolysis under reflux. The precipitate thus formed was suspended in aqueous ammonia which had been adjusted to pH 13, and the suspension was stirred for a whole day and night. Thereafter, the thus treated precipitate was filtered, washed with water and then subjected to baking at 600°C for 5 hours in an electric furnace. When the thus obtained alumina was analyzed, its SiO 2 content was found to be 0.1% by weight or less, its SO 4 -- and Na 2 O contents were both 0.01% by weight or less and its purity (dry basis) was 99.9% by weight or more. When its crystal was analyzed by X-ray diffraction (XRD), no peaks other than a peak belonging to the γ-form were observed. The thus obtained alumina was molded into 3 mm x 3 mm tablets. (Preparation of Comparative Catalyst A) An aqueous solution of commercially available reagent grade aluminium sulfate was neutralized by mixing it with an aqueous solution of sodium aluminate to collect a precipitate. The precipitate thus collected was washed with aqueous ammonia which had been adjusted to pH 13. After repeating the washing step 7 times, the precipitate was stirred for a whole day and night in aqueous ammonia which had been adjusted to pH 13. Thereafter, the thus treated precipitate was filtered, washed with water and then subjected to baking at 600°C for 5 hours in an electric furnace. When the thus obtained alumina was analyzed, its SiO 2 content was found to be 0.1% by weight or less, its SO 4 -- content was 0.1% by weight, its Na 2 O content was 0.04% by weight and its purity (dry basis) was 99.8% by weight. When its crystal was analyzed by X-ray diffraction (XRD), no peaks other than a peak belonging to the γ-form were observed. The thus obtained alumina was molded into 3 mm x 3 mm tablets. (Preparation of Catalyst 3 - Catalyst A/B) Commercially available reagent grade aluminium isopropoxide and 2.6% by weight of ethyl silicate as a source of SiO 2 based on aluminium isopropoxide were dissolved in isopropanol. The thus prepared isopropanol solution was mixed with water and subjected to hydrolysis under reflux. The precipitate thus formed was suspended in aqueous ammonia which had been adjusted to pH 13, and the suspension was stirred for a whole day and night. Thereafter, the thus treated precipitate was filtered, washed with water and then subjected to baking at 600°C for 5 hours in an electric furnace. When the thus obtained alumina was analyzed, its SO 4 -- and Na 2 O contents as dry basis were both 0.01% by weight or less. Its SiO 2 content was found to be 3% by weight, with 0.1% by weight or less of impurities excluding SiO 2 , and its purity (dry basis) was 96.9% by weight. When its crystal was analyzed by X-ray diffraction (XRD), no peaks other than a peak belonging to the γ-form were observed. The thus obtained alumina was molded into 3 mm x 3 mm tablets. (Preparation of Comparative Catalyst 1) An aqueous solution of commercially available reagent grade aluminium sulfate was neutralized by mixing it with an aqueous solution of sodium aluminate to collect a precipitate. The precipitate thus collected was stirred for a whole day and night in aqueous ammonia which had been adjusted to pH 13. Thereafter, the thus treated precipitate was filtered, washed with water and then subjected to baking at 600°C for 5 hours in an electric furnace. When the thus obtained alumina was analyzed, its content of impurities excluding SiO 2 was found to be 0.9% by weight or less, with its SiO 2 , SO 4 -- and Na 2 O contents being 0.1% by weight or less, 0.6% by weight and 0.2% by weight, respectively, and its purity (dry basis) being 99.1% by weight or more. When its crystal was analyzed by X-ray diffraction (XRD), no peaks other than a peak belonging to the γ-form were observed. The thus obtained alumina was molded into 3 mm x 3 mm tablets. (Preparation of Catalyst 4 - Catalyst B) An aqueous solution of commercially available reagent grade aluminium sulfate was mixed with an aqueous solution of sodium aluminate to collect a precipitate. To the precipitate thus collected was added 3% by weight of silica sol (trade name, Snowtex) based on the precipitate, and the resulting mixture was stirred for a whole day and night in aqueous ammonia which had been adjusted to pH 13. Thereafter, the thus treated precipitate was filtered, washed with water and then subjected to baking at 600°C for 5 hours in an electric furnace. When the thus obtained alumina was analyzed, its content of impurities excluding SiO 2 was found to be 0.2% by weight or less, with its SiO 2 , SO 4 -- and Na 2 O contents being about 2% by weight, 0.09% by weight and 0.08% by weight, respectively. The thus obtained alumina was molded into 3 mm x 3 mm tablets. (Preparation of Comparative Catalyst 2) Comparative catalyst 2 was prepared by repeating the procedure for the preparation of catalyst 4 except that the silica sol was not used. When the thus obtained alumina was analyzed, its content of impurities excluding SiO 2 was found to be 0.2% by weight or less, with its SiO 2 , SO 4 -- and Na 2 O contents being 0.1% by weight or less, 0.08% by weight and 0.10% by weight, respectively. (Preparation of Comparative Catalyst 3) An aqueous solution of commercially available reagent grade aluminium sulfate was mixed with an aqueous solution of sodium aluminate to collect precipitate. To the precipitate thus collected was added 10% by weight of silica sol (trade name, Snowtex) based on the precipitate, and the resulting mixture was stirred for a whole day and night in aqueous ammonia which had been adjusted to pH 13. Thereafter, the thus treated precipitate was filtered, washed with water and then subjected to baking at 600°C for 5 hours in an electric furnace. When the thus obtained alumina was analyzed, its content of impurities excluding SiO 2 was found to be 0.2% by weight or less, with its SiO 2 , SO 4 -- and Na 2 O contents being about 7% by weight, 0.10% by weight and 0.09% by weight, respectively. The thus obtained alumina was molded into 3 mm x 3 mm tablets. (Preparation of Catalyst 5 - Catalyst B) A commercially available γ-alumina catalyst (trade name, KHO-24; manufactured by Sumitomo Chemical Co., Ltd.) was pulverized and then mixed with 3% by weight of a commercially available silica gel (Kanto Kagaku Co., Ltd.). By adding an appropriate amount of water, the thus prepared mixture was ground using a mortar and then molded into 3 mm x 3 mm tablets. When the thus obtained alumina was analyzed, its content of impurities excluding SiO 2 was found to be 1.1% by weight or less, with its SiO 2 , SO 4 -- and Na 2 O contents being about 2% by weight, 0.70% by weight and 0.30% by weight, respectively. (Example 1) A vertical type reaction tube made of SUS 316 (inside diameter, 25.4 mm; length, 50 cm) equipped with an external electric furnace was packed with 40 cc of the catalyst 1, and the temperature of the electric furnace was increased to 320°C. Isopropanol was fed from the top of the reaction tube at an LHSV of 1 hr -1 , and the reaction was effected by increasing the pressure in the reaction tube to 18 kg/cm 2 G. A gas/liquid mixture discharged from the bottom of the reaction tube was separated into gas and liquid phases. When examined 5 hours after the commencement of the reaction, conversion of isopropanol was found to be 73 mole % and selectivity of propylene was 92 mole %. Diisopropyl ether was found as a byproduct. Next, steam resistance of the catalyst 1 was evaluated in accordance with the procedure described above. Results of the X-ray analysis showed no transition into the α-form. A 40 cc portion of the catalyst 1 after its steam resistance test was packed in the same type of the reaction tube as used in the above experiment, and the reaction was carried out under the same conditions as described above. A gas/liquid mixture discharged from the bottom of the reaction tube was separated into gas and liquid phases. When examined 5 hours after the commencement of the reaction, conversion of isopropanol was found to be 73 mole % and selectivity of propylene was 92 mole %, thus showing no changes in the catalytic activity by the steam treatment. Diisopropyl ether was found as a byproduct. (Comparative Example 1) The same type of reaction tube as used in Example 1 was packed with 40 cc of the comparative catalyst 1 prepared above, and the reaction was carried out under the same conditions as in Example 1. A gas/liquid mixture discharged from the bottom of the reaction tube was separated into gas and liquid phases. When examined 5 hours after the commencement of the reaction, conversion of isopropanol was found to be 73 mole % and selectivity of propylene was 88 mole %. Diisopropyl ether was found as a byproduct. Next, the steam resistance of the comparative catalyst 1 was evaluated in accordance with the procedure described above. Results of the X-ray analysis of the comparative catalyst after its steam resistance test showed about 30% of transition into the α-form. A 40 cc portion of the comparative catalyst 1 after its steam resistance test was packed in the same type of reaction tube as used in Example 1, and the reaction was carried out under the same conditions as described in Example 1. A gas/liquid mixture discharged from the bottom of the reaction tube was separated into gas and liquid phases. When examined 5 hours after the commencement of the reaction, conversion of isopropanol was found to be 48 mole % and selectivity of propylene was 75 mole %, thus showing a sharp decrease in the catalytic activity by the steam treatment. Diisopropyl ether was found as a byproduct. (Example 2) A vertical type reaction tube made of SUS 316 (inside diameter, 38.1 mm; length, 4,300 mm) equipped with an external oil bath was packed with 4,550 cc of the catalyst 1, and the temperature of the oil bath was increased to 315°C. Isopropanol was fed from the top of the reaction tube at an LHSV of 1 hr -1 , and the reaction was effected by increasing the pressure in the reaction tube to 18 kg/cm 2 G. A gas/liquid mixture discharged from the bottom of the reaction tube was separated into gas and liquid phases. When examined 10 hours after the commencement of the reaction, conversion of isopropanol was found to be 81 mole % and selectivity of propylene was 95 mole %. Diisopropyl ether was found as a byproduct. In addition, when examined 3,000 hours after the commencement of the reaction, conversion of isopropanol was found to be 80 mole % and selectivity of propylene was 94 mole %. When the catalyst after completion of the reaction was examined by X-ray analysis, formation of the α-form was found in an amount of 1%. Thus, it was found that the transition into the α-form and the decrease in the catalytic activity were negligible even after a prolonged period of reaction time. (Comparative Example A and Example 4) The procedure of Example 2 was repeated using the same reaction tube under the same reaction conditions, except that the catalyst 1 was replaced by the comparative catalyst A and catalyst 3. The results are shown in Table 1. (Comparative Example 2) The procedure of Example 2 was repeated using the same reaction tube under the same reaction conditions, except that the catalyst 1 was replaced by the comparative catalyst 1. The results are shown in Table 1. (Comparative Example B) The reaction tube used in Example 1 was packed with 40 cc of the catalyst A, and the temperature of the electric furnace was increased to 400°C. Ethanol was fed from the top of the reaction tube at an LHSV of 0.5 hr -1 , and the reaction was effected by increasing the pressure in the reaction tube to 18 kg/cm 2 G. A gas/liquid mixture discharged from the bottom of the reaction tube was separated into gas and liquid phases. When examined 5 hours after the commencement of the reaction, conversion of ethanol was found to be 83 mole % and selectivity of ethylene was 94 mole %. Diethyl ether was found as a byproduct. Next, the steam resistance of the catalyst A was evaluated in accordance with the procedure described above. Results of the X-ray analysis of the thus treated catalyst showed about 5% transition into the α-form. A 40 cc portion of the catalyst A after its steam resistance test was packed in the same type of reaction tube as used in the above experiment, and the reaction was carried out under the same conditions as described above. A gas/liquid mixture discharged from the bottom of the reaction tube was separated into gas and liquid phases. When examined 5 hours after the commencement of the reaction, conversion of ethanol was found to be 78 mole % and selectivity of ethylene was 92 mole %. Diethyl ether was found as a byproduct. (Example 7) A vertical type reaction tube made of SUS 316 (inside diameter, 25.4 mm; length, 50 cm) equipped with an external electric furnace was packed with 40 cc of the catalyst 4, and the temperature of the electric furnace was increased to 320°C. Isopropanol was fed from the top of the reaction tube at an LHSV of 1 hr -1 , and the reaction was effected by increasing the pressure in the reaction tube to 18 kg/cm 2 G. A gas/liquid mixture discharged from the bottom of the reaction tube was separated into gas and liquid phases. When examined 5 hours after the commencement of the reaction, conversion or isopropanol was found to be 90 mole % and selectivity of propylene was 92 mole %. Diisopropyl ether was found as a byproduct. Next, the steam resistance of the catalyst 4 was evaluated in accordance with the procedure described above. Results of the X-ray analysis showed no transition into the α-form. A 40 cc portion of the catalyst 4 after its steam resistance test was packed in the same type of reaction tube as used in the above experiment, and the reaction was carried out under the same conditions as described in Example 7. A gas/liquid mixture discharged from the bottom of the reaction tube was separated into gas and liquid phases. When examined 5 hours after the commencement of the reaction, conversion of isopropanol was found to be 87 mole % and selectivity of propylene was 90 mole %. Diisopropyl ether was found as a byproduct. (Example 8) A vertical type reaction tube made of SUS 316 (inside diameter, 38.1 mm; length, 4,300 mm) equipped with an external oil bath was packed with 4,550 cc of the catalyst 4, and the temperature of the oil bath was increased to 315°C. Isopropanol was fed from the top of the reaction tube at an LHSV of 1 hr -1 , and the reaction was effected by increasing the pressure in the reaction tube to 18 kg/cm 2 G. A gas/liquid mixture discharged from the bottom of the reaction tube was separated into gas and liquid phases. When examined 10 hours after the commencement of the reaction, conversion of isopropanol was found to be 89 mole % and selectivity of propylene was 95 mole %. Diisopropyl ether was found as a byproduct. In addition, when examined 3,000 hours after the commencement of the reaction, conversion of isopropanol was found to be 85 mole % and selectivity of propylene was 92 mole %. When the catalyst after completion of the reaction was examined by X-ray analysis, the catalyst was found to be totally as the γ-form thus showing that transition of the catalyst into the α-form and decrease in the catalytic activity did not occur even after a prolonged reaction time. (Comparative Example 4) The reaction of Example 7 was repeated except that 40 cc of the comparative catalyst 2 was used. A gas/liquid mixture discharged from the bottom of the reaction tube was separated into gas and liquid phases. When examined 5 hours after the commencement of the reaction, conversion of isopropanol was found to be 73 mole % and selectivity of propylene was 88 mole %. Diisopropyl ether was found as a byproduct. Next, the steam resistance of the comparative catalyst 2 was evaluated in accordance with the procedure described above. Results of the X-ray analysis showed about 30% transition into the α-form. Using the comparative catalyst 2 after its steam resistance test, the reaction was carried out using the same type of reaction tube and under the same reaction conditions as described in Example 7. A gas/liquid mixture discharged from the bottom of the reaction tube was separated into gas and liquid phases. When examined 5 hours after the commencement of the reaction, conversion of isopropanol was found to be 48 mole % and selectivity of propylene was 75 mole %. Diisopropyl ether was found as a byproduct. Thus, it was found that the comparative catalyst was transformed into the α-form and its catalytic activity was reduced by the steam resistance test. (Comparative Example 5) The reaction of Example 7 was repeated except that 40 cc of the comparative catalyst 3 was used. A gas/liquid mixture discharged from the bottom of the reaction tube was separated into gas and liquid phases. When examined 5 hours after the commencement of the reaction, conversion of isopropanol was found to be 92 mole % and selectivity of propylene was 65 mole %. A heavy material was found as a byproduct. After 1,000 hours of the reaction, conversion of isopropanol was reduced to 43 mole %. The comparative catalyst after completion of the reaction showed no transition into the α-form, but its surface was covered with a large quantity of carbon. (Comparative Example 6) A vertical type reaction tube made of SUS 316 (inside diameter, 38.1 mm; length, 4,300 mm) equipped with an external oil bath was packed with 4,500 cc of the comparative catalyst 2, and the temperature of the oil bath was increased to 315°C. Isopropanol was fed from the top of the reaction tube at an LHSV of 1 hr -1 , and the reaction was effected by increasing the pressure in the reaction tube to 18 kg/cm 2 G. A gas/liquid mixture discharged from the bottom of the reaction tube was separated into gas and liquid phases. When examined 10 hours after the commencement of the reaction, conversion of isopropanol was found to be 84 mole % and selectivity of propylene was 90 mole %. Diisopropyl ether was found as a byproduct. In addition, when examined 3,000 hours after the commencement of the reaction, conversion of isopropanol was found to be 54 mole % and selectivity of propylene was 84 mole %. When the comparative catalyst after completion of the reaction was examined by X-ray analysis, about 20% of transition into the α-form was found. No. Comparative example B Inventive example 7 Inventive example 8 Comparative example 4 Material ethanol isopropanol isopropanol isopropanol Flow rate (hr -1 ) 0.5 1 1 1 Temp. (°C) 400 320 315 320 Pressure (kg/cm 2 G) 18 18 18 18 Reaction time (hr) 5 5 5 5 10 3000 5 5 Catalyst A after steam test 4 after steam test 4 continuous operation comparative catalyst 2 after steam test α-form (%) 5 0 0 30 By-product diethyl ether diisopropyl ether diisopropyl ether diisopropyl ether Alcohol conversion 83 78 90 87 89 85 73 48 Olefin slectivity 94 92 92 90 95 92 88 75 Olefin yield 78 72 83 78 85 78 64 36 No. Comparative example 5 Comparative example 6 Material isopropanol isopropanol Flow rate (hr -1 ) 1 1 Temp. (°C) 320 315 Pressure (kg/cm 2 G) 18 18 Reaction time (hr) 5 1000 10 3000 Catalyst comparative catalyst 3 continuous operation comparative catalyst 2 continuous operation α-form (%) 0 20 By-product heavy material diisopropyl ether Alcohol conversion 92 43 84 54 Olefin slectivity 65 - 90 84 Olefin yield 60 - 76 45 As has been described in the foregoing, according to the process of the present invention, propylene can be produced from propanol with higher yield and higher selectivity for longer period of time in comparison with the prior art processes. The high purity propylene produced by the inventive process is useful as a raw material for use in the synthesis of various organic compounds and polymers.

Claims: A process for producing propylene by the catalytic dehydration of propanol using a γ-alumina catalyst (A), wherein: a) the dehydration is carried out at a temperature of from 150 to 500°C and under such pressure that the propylene produced liquifies at ambient temperature; b) the catalyst (A) contains 0.3% by weight or less of impurities in total excluding SiO 2 , said impurities including 0.2% by weight or less of sulfur content calculated in terms of SO 4 -- and 0.03% by weight or less of sodium content calculated in terms of Na 2 O. A process according to claim 1 wherein the catalyst (A) comprises up to 1% α-alumina. A process according to claim 1 or 2 wherein said γ-alumina catalyst (A) has been prepared from an organic aluminium compound. A process for producing propylene by the catalytic dehydration of propanol using a γ-alumina catalyst (B), wherein: a) the dehydration is carried out at a temperature of from 150 to 500°C and under such pressure that the propylene produced liquifies at ambient temperature; and b) the catalyst (B) contains 0.5 to 3% by weight of SiO 2 . A process according to claim 4 wherein the catalyst (B) is free of α-alumina. A process according to claim 4 or 5 wherein said γ-alumina catalyst (B) has been prepared by adding an SiO 2 source which is then converted into SiO 2 . A process according to any one of the preceding claims wherein the γ-alumina catalyst has the features of both catalyst (A) as defined in claim 1 and catalyst (B) as defined in claim 4.

Inventors: ARAKI SHINTARO, ISAKA TOSHIYUKI, TANIGUCHI KATSUO, ARAKI, SHINTARO, ISAKA, TOSHIYUKI, TANIGUCHI, KATSUO, Araki, Shintaro, c/o MITSUI PETROCHEM. IND., LTD., Isaka, Toshiyuki, c/o MITSUI PETROCHEM. IND., LTD., Taniguchi, Katsuo, c/o MITSUI PETROCHEM. IND., LTD
Applicants: MITSUI PETROCHEMICAL IND, MITSUI PETROCHEMICAL INDUSTRIES, LTD.
Application year: 1992
Main classification: C07C1
IPC codes: B01J21, C07C1