Process for Preparing Alpha, Beta Unsaturated Acids by Catalytic Oxidation of Corresponding Saturated Acids in the Gas Phase
Abstract
Alpha, beta-unsaturated acids are obtained by gas-phase catalytic oxidation of saturated acids containing from 3 to 8 carbon atoms. The catalyst used has the empirical composition in which in which The catalytic dehydrogenation of lower aliphatic acids is known and has been described previously. According to one known process, for example, a metal oxide is used as a catalyst and reagent, and dehydrogenation is conducted in the absence of molecular oxygen. In that method, however, the catalyst is rapidly reduced and deactivated and requires frequent re-activations, while the degree of conversion of the saturated acid at every pass on the catalytic bed is very low, which results in considerable complications in carrying out the process and requires use of large apparatuses. In this connection, reference is made to U.S. Pat. No. 2,945,057 and to Ind. Eng. Chem. Prod. Res. and Development, volume II, page 287 (1963). According to another known process, a metal sulphide is employed as dehydrogenating agent, in the absence of molecular oxygen, to dehydrogenate lower aliphatic acids and the esters thereof. In this process too, since the metal sulphide acting as dehydrogenating agent is converted as the reaction proceeds, frequent regenerations of the metal sulphide become necessary: see U.S. Pat. No. 3,370,087. Furthermore, it is known since long how to prepare methacrylic acid by dehydrogenation of isobutyric acid in the presence of a catalyst consisting of iodine or hydrogen iodide. However, even using a large amount of iodine or hydrogen iodide, the selectivity in methacrylic acid remains limited: see in this connection Japanese Pat. No. 26,484/68. Also, processes employing sulphur vapours as a reagent are known: see Japanese Pat. No. 8,208/69 and German Pat. No. 2,129,320. More recently, alpha, beta-unsaturated aliphatic acids have been otained starting from the corresponding saturated acids by dehydrogenation conducted in the presence of molecular oxygen on solid catalysts. The catalysts employed, according to Belgian Pat. No. 766,404, consist of mixed phosphates of iron and bismuth, optionally also of lead. One object of this invention is to provide new process for preparing alpha, beta-unsaturated acids from corresponding saturated acids containing 3 to 8 carbon atoms which is free of the disadvantages associated with known processes. This and other objects are accomplished by the invention in accordance with which alpha, beta-unsaturated acids are obtained by the catalytic oxidative dehydrogenation of carboxylic, aliphatic saturated acids having the general formula ##EQU1## wherein R.sub.1, R.sub.2, R.sub.3 represent a hydrogen atom or an alkyl radical containing from 1 to 5 carbon atoms, the maximum limit as to carbon atoms in the molecule being 8. The process of the invention is characterized in that the reaction is conducted in the presence of a catalyst containing, in combination with oxygen, iron, phosphorus and one or more of the elements lithium, sodium, potassium, rubidium, cesium, calcium, strontium, barium, magnesium. The saturated aliphatic acid is introduced into the catalytic reactor in a gaseous admixture with oxygen (air) and with one or more diluents such as nitrogen, steam, CO.sub.2 etc. The amount of aliphatic acid contained in the reacting mixture is comprised between 1% and 40% by volume, the oxygen/saturated acid molar ratio ranging from 0.1/1 to 10/1, preferably from 0.4/1 to 4/1. The reaction temperature is comprised between 300.degree. and 500.degree.C. In the process of this invention, it is possible to employ -- with particularly favorable results -- isobutyric acid and propionic acid as starting saturated acids in order to obtain methacrylic acid and acrylic acid respectively. In the catalyst composition the above-mentioned elements are present in such amounts that the relative atomic ratios can be defined by the following empirical formula: It is conventional, in this art, to identify the catalyst by empirical formula and to consider the elements as existing as oxides. However, as is understood by those skilled in the art, to assign a value to a symbol such as z in the foregoing formula for the catalyst is not to say that all of the elenents making up the catalyst do exist as oxides, wholly or partially, since the actual oxidation state of the elements as they exist in the catalyst has not been established. The catalytic composition used in the practice of this invention can be employed without a support and as such it exhibits excellent catalytic activity. Should it be preferable to employ the catalyst composition in combination with a support, it is possible to use as the support any suitable inorganic material such as silica, alumina, silicium carbide, silica-alumina, silicates, borates, carbonates, provided they are stable under the reaction conditions to which they will be subjected in the oxidative dehydrogenation of the starting saturated acids to the alpha, beta-unsaturated acids. The amount of active catalyst composition by weight with respect to the support weight may vary within a wide range depending upon the characteristics of the support and the method of preparing the supported catalyst. In the process of this invention, the catalyst may be used in the form of fixed or fluidized bed. In the latter case, both the character of the support and the method used to prepare the supported catalyst are of particular importance to the preparation of a microspheriodal catalyst having a suitable granulometirc distribution. A microspheroidal catalyst can be prepared according to different techniques: for instance by spray-drying a solution or suspension of the support and of the components of the active catalyst composition, or by impregnating a pre-formed microspheroidal support with a solution of the components of the catalytically active composition. As starting compounds for the preparation of the catalytic composition, according to this invention, the following compounds of alkaline metals, for example, may be used: nitrates, oxides, hydroxides, carbonates, bicarbonates, nitrites, phosphates, silicates, and oxyacid salts or salts of monocarboxylic or polycarboxylic organic acids such as formates, oxalates, citrates, tartrates, etc. Starting iron compounds may be chosen, according to the method employed for the preparation of the catalyst, from nitrates, chlorides, sulphates, carbonates, monocarboxylic or polycarboxylic organic acid salts and chelates. As for alkaline-earth metals, chlorides, sulphates, carbonates, salts of monocarboxylic or polycarboxylic organic acids, etc., can be used. For phosphorus, alkaline phosphates may be used, ammonium phosphates, phosphoric or phosphorous acids, etc. All methods of preparation involve a final activation phase of the catalytic combination which consists of heating it, in the presence of air or of a mixture of air and steam, at a temperature between 350.degree. and 850.degree.C, preferably between 400.degree. and 700.degree.C. The preparation of the catalyst may be accomplished in accordance with known techniques. The following methods have been found useful in the preparation of the catalyst: 1. In an aqueous solution of phosphoric acid are dissolved predetermined quantities of iron salts and of alkaline or alkaline-earth metals salts. To this is then added ammonia up to pH 7. The suspension obtained in this way is then evaporated to dryness under stirring, with the residue being dried further at 130.degree.C for one night and then activated in air at 540.degree.C for 2 hours. The calcined mass is then ground and sifted. The portion which passes through a mesh of 20-35 is suitable for use in a fixed bed reactor. 2. A suitable mixture of the components was digested with water and gradually evaporated to dryness under stirring. The residue was finely ground and then dried overnight at 130.degree.C. The resulting mass was then activated in air for 2 hours at 130.degree.C to 600.degree.C. 3. The residue dried at 130.degree.C, as per method 1, was treated in air at 300.degree.C. The mass so obtained was ground to a size which passed through a 25-mesh screen; 10% of stearic acid powder was added and the mixture was pressed to 4 .times. 4 mm pastils. The pastils so obtained were activated for 2 hours in air at 540.degree.C. 4. A solution of the catalyst components having a volume corresponding to that of the support was used to impregnate a microspheroidal silica of the commercial type. The resulting slurry was allowed to stand for 2 - 3 hours, after which it was evaporated to dryness under stirring and further dried overnight at 130.degree.C. The product obtained was activated in a fluidized bed in air for 2 hours at 550.degree.C. This preparation method is useful in preparing catalyst for fixed bed using a proper support. Using the catalysts disclosed herein, high yields of unsaturated acid are obtained with very high conversions, in some cases up to 100%, of the corresponding saturated acid. Such result is attributable to the fact that the catalysts according to this invention promote an oxidative dehydrogenation process having a regular trend and which is easily controllable as regards reaction temperature and contact times. The reagents may be fed onto the catalyst preheated to a temperature close to the reaction temperature or at least to a temperature slightly higher than the mixture dew point, in which case they rapidly heat on contacting the catalytic bed, either of the fixed or fluidized type. The reagents may be fed to the catalyst already premixed either thoroughly or in part or individually. Feeding of the reagents partially premixed or individually is best applied in general to a fluidized bed reactor. It is also possible to introduce a part of the air or, optionally, all of the saturated acid or a part thereof, into the reactor bottom and successively to feed the remaining amounts of reagents to one or more upper points inside the catalytic bed. When the reaction is conducted according to the catalytic fixed bed technique, such bed may be prepared, according to the art, by arranging the catalyst inside the tubes of a tube bundle reactor and by removing the reaction heat by proper fluids circulating outside the tubes and, for example, more generally, by means of molten salts mixtures. It is also possible to operate in a reactor consisting of several adiabatic reaction stages alternated with zones for cooling the reacted mixture. The reaction is conducted at a temperature ranging from 300.degree. to 500.degree.C, preferably from 340.degree. to 440.degree.C. The contact time, expressed in seconds as the ratio between the catalytic bed volume and the volumes of the reagents gaseous mixture fed per second, measured under the average conditions of temperature and pressure existing in the catalytic bed, may vary depending upon the nature of the catalyst, the nature of the catalytic bed, i.e. fixed or fluidized, and upon the catalyst size; generally it may be comprised between 0.1 and 20 seconds, a preferred range being from 0.3 to 15 seconds, as corresponding to the most usual practical operating conditions. The total pressure at which the reaction is conducted is not particularly important, and may vary within a wide range. It is selected, in part, for reasons of economy but generally, pressures of about atmospheric or pressures slightly higher than atmospheric pressure are used. Me is one or more of the elements Li, Na, K, Rb, Cs, Mg, Ca, Sr and Ba; x is 0.2 to 3; y is 0.01 to 2; and z is a value corresponding to the average valences of the elements in the oxidation states in which they exist in the catalyst. Me is one or more of the elements Li, Na, K, Rb, Cs, Mg, Ca, Sr, Ba, x is 0.2 to 3, Y is 0.01 to 2, and z is a value corresponding to the average valences of the elements in the oxidation states in which they exist in the catalyst.
Metadata
Assignee
- Montedison S.p.A.
Inventors
- Enrico Cavaterra
- Guido Petrini
- Romano Covini
- Luciano Moreschini
Application Information
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Description
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Claims
Patent Citations (5)
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| US3781336 | 1973-12-01 | Chono et al. | |
| US3855279 | 1974-12-01 | Watkins |