Catalyst Composition for Producing Tertiary-Butylstyrene

Alkenyl-substituted aromatic compounds are important starting materials for the production of resins, plastics, rubbers, solvents, chemical intermediates, and the like.

Processes for the production of alkenyl-substituted aromatic compounds often are characterized by low conversion rates which necessitate the recycle of large quantities of unconverted charge. Many of the known processes require the presence of a large volume of steam or other gaseous diluent which is a cost disadvantage. In some processes the conversion efficiency to alkenyl-substituted aromatic product is diminished because of the formation of a relatively large proportion of carbon oxides and other byproducts.

In one well-known commercial process, C.sub.2 -C.sub.3 alkylaromatic hydrocarbons (e.g., ethylbenzene, ethyltoluene and isopropylbenzene) are converted to the corresponding styrene derivatives by passage of the alkylaromatic hydrocarbon feed and steam over a Fe.sub.2 O.sub.3 catalyst. The conversion per pass is in the 35-40% range, and comparatively high temperatures are needed for the oxidative dehydrogenation reaction.

Illustrative of other oxidative dehydrogenation processes, U.S. Pat. No. 3,299,155 describes a process for the production of alkenylbenzenes which involves contacting a mixture of an ethyl (or isopropyl) substituted benzene compound and sulfur dioxide in vapor phase with a metal phosphate catalyst such as calcium phosphate.

U.S. Pat. No. 3,409,696 describes a process which involves contacting an admixture of C.sub.2 -C.sub.4 alkylaromatic hydrocarbon and steam at a temperature of 500.degree.-650.degree. C. with a catalyst containing 20-60 weight percent of a bismuth compound (e.g., bismuth oxide) on a calcium phosphate support of which at least 90% of the total pore volume is contributed by pores having a diameter of 1000-6000 A.

U.S. Pat. No. 3,733,327 describes an oxydehydrogenation process for converting a C.sub.2 -C.sub.6 alkylaromatic compound to the corresponding C.sub.2 -C.sub.6 alkenylaromatic compound which comprises contacting an admixture of starting material and oxygen at 400.degree.-650.degree. C. with a cerium phosphate or cerium-zirconium phosphate catalyst.

U.S. Pat. No. 3,957,897 describes a process for oxydehydrogenation of C.sub.2 -C.sub.6 alkylaromatic compounds which involves the use of oxygen, a reaction zone temperature of 450.degree.-650.degree. C., a space velocity of 55-2500, and a catalyst which is at least one of calcium, magnesium and strontium pyrophosphate.

More recently, there has been increasing concern with respect to the potentially harmful environmental effects associated with the manufacture of synthetic resin products. In the molding of large shaped articles, for example, volatile components of polymerizable monomeric formulation sometimes tend to evaporate from freshly coated mold surfaces which are exposed.

Various means have been contemplated for reducing the level of fugitive vapors in a synthetic resin manufacturing plant. One method involves the replacement of volatile monomers of a formulation with monomers which have a lower vapor pressure. Thus, it is advantageous to substitute an alkenylaromatic compound such as tertiary-butylstyrene for styrene in a polymerizable formulation which contains the volatile styrene as a comonomer.

As a further consideration, it has been found that tertiary-butylstyrene is desirable as a comonomer in the preparation of copolymers or as a curing agent for fiber-reinforced plastics because it improves the moldability of polymerizable formulations and it lessens the mold shrinkage of molded plastic articles.

The advantages of tertiary-butylstyrene as a comonomer in resin systems has stimulated interest in improved processes for synthesizing this type of higher molecular weight alkenylaromatic compound.

U.S. Pat. No. 3,932,549 describes a process for preparing tertiary-butylstyrene which comprises reacting tertiary-butylbenzene with ethylene and oxygen at 50.degree.-300.degree. C. in the presence of a catalyst prepared by treating metallic palladium or a fatty acid salt thereof with pyridine.

Other known processes for producing tertiary-butylbenzene involve oxydehydrogenation of tertiary-butylethylbenzene. The type of patent processes described hereinabove for oxydehydrogenation of C.sub.2 -C.sub.6 alkylaromatic compounds are generally applicable for conversion of tertiary-butylethylbenzene to tertiary-butylstyrene.

However, the chemical reactivity of tertiary-butylethylbenzene under oxydehydrogenation conditions is more complex than that of simpler chemical structures such as ethylbenzene or ethyltoluene. The teritary-butyl substituent of tertiary-butylethylbenzene under oxydehydrogenation conditions is susceptible to cracking so as to yield methane and a residual isopropenyl substituent on the benzene nucleus. Consequently, one of the ultimate byproducts of tertiary-butylethylbenzene oxydehydrogenation is a dialkenylbenzene derivative such as isopropenylstyrene.

Because of the presence of two or more polymerizable alkenyl groups, a compound such as isopropenylstyrene tends to undergo crosslinking activity and form insoluble byproducts during the high temperature cycles of starting material conversion and product recovery in an oxydehydrogenation process. Heat exchangers and distillation columns can be rendered inoperative by the deposition of high molecular weight polymeric residues.

Further, the presence of an isopropenylstyrene type of contaminant, particularly a variable quantity of such material, in purified tertiary-butylstyrene can complicate or even prohibit the application of the contaminated tertiary-butylstyrene product as a comonomer in polymerizable formulations.

Accordingly, it is an object of the invention to provide a process for oxydehydrogenation of C.sub.2 -C.sub.6 alkyl-substituted aromatic compounds to the corresponding alkenyl-substituted aromatic derivatives.

It is another object of this invention to provide a process for converting tertiary-butylethylbenzene to tertiary-butylstyrene under moderate conditions with a high level of starting material conversion and product selectivity.

It is another object of this invention to provide a process for converting tertiary-butylethylbenzene to tertiary-butylstyrene with little or no production of dialkenylbenzene byproducts.

It is a further object of this invention to provide a novel catalyst adapted for oxydehydrogenation processes.

Other objects and advantages of the present invention shall become apparent from the accompanying description and examples.

One or more objects of the present invention are accomplished by the provision of a process which comprises contacting a feed stream containing tertiary-butylethylbenzene and oxygen in vapor phase with a catalyst comprising aluminum-calcium-cerium phospate.

In a more specific embodiment, this invention provides a process for the production of tertiary-butylstyrene under oxydehydrogenation conditions which comprises contacting a feed mixture of tertiary-butylethylbenzene and oxygen at a temperature in the range between about 350.degree. C. and 650.degree. C. with a coprecipitated aluminum-calcium-cerium phosphate catalyst, wherein the conversion selectivity to tertiary-butylstyrene is at least 80 mole percent, and the selectivity to dialkenylbenzene is essentially zero mole percent.

A preferred reaction temperature for the oxydehydrogenation reaction is one which is in the range between about 400.degree. C. and 600.degree. C.

The feed admixture of tertiary-butylethylbenzene and oxygen can contain quantities of other hydrocarbons which do not adversely affect the invention oxydehydrogenation reaction, e.g., compounds such as octane, decene, naphthene, benzene, toluene, pyridine, thiophene, and the like, which may be present in commercially available alkylbenzenes.

The molecular oxygen component of the feed admixture preferably is present in a quantity between about 0.2-5 moles per mole of tertiary-butylethylbenzene, and most preferably in a molar ratio of 0.8-2:1. The oxygen can be supplied as air, commercially pure oxygen, or air enriched with oxygen.

It is advantageous to include a gasiform diluent in the feed stream. Illustrative of suitable diluents are carbon dioxide, nitrogen, noble gases and steam, either individually or in admixture. The diluent is normally employed in a quantity between about 2-20 moles per mole of tertiary-butylethylbenzene in the feed stream.

The pressure utilized in the vapor phase oxydehydrogenation process can be subatmospheric, atmospheric or superatmospheric. A convenient pressure for the vapor phase process is one which is in the range between about 1 and 200 psi.

Suitable reactors for the vapor phase process include either fixed bed or fluid bed reactors which contain the invention aluminum-calcium-cerium catalyst composition. The process can be conducted continuously or noncontinuously, and the catalyst may be present in various forms such as a fixed bed or a fluidized system.

The residence time (i.e., catalyst contact time) of the feed stream in the vapor phase process will vary in the range of about 0.5-20 seconds, and preferably will average in the range between about 1-15 seconds. Residence time refers to the contact time adjusted to 25.degree. C. and atmospheric pressure. The contact time is calculated by dividing the volume of the catalyst bed (including voids) by the volume per unit time flow rate of the feed stream at NTP.

An important aspect of the present invention process is the use of a novel coprecipitated aluminum-calcium-cerium phosphate catalyst composition. The catalyst exhibits unique properties for the conversion of tertiary-butylethylbenzene to the tertiary-butylstyrene with a high conversion efficiency, and with little or no production of dialkenylbenzene type of byproducts.

The atomic ratio of metals in the catalyst composition can vary in the range of about 5-20:5-20:1 of aluminum:calcium:cerium. The phosphate component is present in a quantity at least sufficient to satisfy the valences of the metal elements in the catalyst.

The catalyst can be prepared by the addition to an aqueous solution of ammonium phosphate of an aqueous solution of water soluble compounds of aluminum, calcium and cerium metals, respectively. Illustrative of water-soluble or partially water-soluble compounds are the chlorides, nitrates and sulfates of aluminum, calcium and cerium.

In a preferred procedure, the pH of the resultant solution of aluminum, calcium, cerium and phospate compounds is adjusted to about 7 with an alkaline reagent such as ammonium hydroxide. The coprecipitate which forms is recovered, washed with water, and dried.

It has been found that the activity of the catalyst composition is enhanced if the coprecipitate preparation is calcined in an inert atmosphere at a temperature between about 300.degree. C. and 600.degree. C. for a period of about 1-24 hours.

The coprecipitated aluminum-calcium-cerium phosphate composition described above can be used as the catalyst per se, or the said composition can be combined with a suitable internal diluent or carrier substrate. The carrier substrate is preferably incorporated during the coprecipitate formation step of the catalyst preparation.

The carrier substrate should be relatively refractory to the conditions utilized in the invention process. Suitable carrier substrate materials include (1) silica or silica gel, silicon carbide, clays, and silicates including those synthetically prepared and naturally occurring, which may or may not be acid treated such as attapulgus clay, china clay, diatomaceous earth, Fuller's earth, kaolin, asbestos and kieselguhr; (2) ceramics, porcelain, crushed firebrick and bauxite; (3) refractory inorganic oxides such as alumina, titanium dioxide, zirconium dioxide, chromium oxide, beryllium oxide, vanadium oxide, cesium oxide, hafnium oxide, zinc oxide, molybdenum oxide, bismuth oxide, tungsten oxide, uranium oxide, magnesia, boria, thoria, silica-alumina, silica-magnesia, chromia-alumina, alumina-boria and silica-zirconia; (4) crystalline zeolitic alumino-silicates such as naturally occurring or synthetically prepared mordenite and/or faujasite, either in the hydrogen form or in a form which has been treated with multivalent cations; and (5) spinels such as MgAl.sub.2 O.sub.4, FeAl.sub.2 O.sub.4, ZnAl.sub.2 O.sub.4, CaAl.sub.2 O.sub.4, and other like compounds having the formula MO.Al.sub.2 O.sub.4 where M is a metal having a valence of 2.

The catalyst as employed in the invention process can be in the shape of granules, pellets, extrudate, powders, tablets, fibers, or other such convenient physical form.

A preferred catalyst composition of the present invention is one which corresponds to the formula:

wherein x is a number sufficient to satisfy the valences of the metal components.

The preferred catalyst composition of the present invention is adapted for oxydehydrogenation of hydrocarbon compounds such as C.sub.3 -C.sub.10 alkenes, C.sub.4 -C.sub.10 cycloalkenes and C.sub.2 -C.sub.6 alkylaromatic compounds, and has particular advantage for the oxydehydrogenation of tertiary-butylethylbenzene and ethyltoluene under mild oxidation conditions.

The presence of the cerium metal component in an invention aluminum-calcium-cerium phosphate catalyst composition appears to enhance the reactivity of the catalyst, and the presence of the aluminum metal component contributes attrition-resistance and extends the life of the catalyst under hydrocarbon oxyhydrogenation conditions.

The following examples are further illustrative of the present invention. The reactants and other specific ingredients are presented as being typical, and various modifications can be derived in view of the foregoing disclosure within the scope of the invention.

A solution is prepared by dissolving 25 grams of aluminum nitrate [0.07 M, Al(NO.sub.2).sub.3.9H.sub.2 O], 16 grams of calcium nitrate [0.07 M, Ca(NO.sub.3).sub.2.4H.sub.2 O] and 3 grams of cerium(III) nitrate [0.007 M, Ce(NO.sub.3).sub.3.6H.sub.2 O] in 150 milliliters of water. The solution is blended with 150 milliliters of an aqueous solution of dibasic ammonium phosphate [0.3 M, (NH.sub.4).sub.2 HPO.sub.4 ] having a pH of 7.6. The pH of the resultant blended solution is adjusted to a pH of 7 with ammonium hydroxide.

The solution is heated to the boiling point, maintained at that temperature for a period of about one hour, and then cooled to room temperature. The solid material which has precipitated is separated by filtration. The recovered precipitate is washed with water, and then dried in a vacuum oven at 120.degree. C. The dried solids are calcined at 550.degree. C. under a nitrogen atmosphere for a period of 5 hours.

A portion of the calcined solids is ground and sieved to a mesh size in the range of 10-20. A 1 cm.sup.3 quantity of the catalyst is charged to an electrically heated reactor, and the reactor is heated to a temperature of about 450.degree. C.

An air flow of 10 milliliters/minute and a tertiary-butylethylbenzene (meta:para ratio of 3:97) flow of 1 milliliter/hour are introduced into the inlet of the reactor. The effluent stream from the reactor is cooled, and the resultant liquid components are collected and analyzed by a gas chromatograph/mass spectrometer system.

The molar percent conversion of tertiary-butylethylbenzene is 45.6 and the mole percent selectivity to tertiary-butylstyrene is 86.4. The relative selectivity yield of dialkenylbenzene is less than about 0.03 mole percent.

When an aluminum-calcium-cerium phosphate catalyst contains Ce(IV) rather than Ce(III) metal component, the yield of dialkenylbenzene byproducts tends to increase.

An aluminum-calcium-cerium phosphate catalyst is prepared in the same manner as Example I, employing an eight-fold increase in the relative proportions of chemical components.

The atomic ratio of the metals in the catalyst composition are in a ratio of 9.8:9.6:1 of Al:Ca:Ce.

A 100 cm.sup.3 portion of the catalyst powder (10-20 mesh) is charged to a reactor which is a 0.5 inch stainless steel pipe of 24 inch length. The reactor and a part of the feed line are immersed in a molten salt bath.

Variable quantities of tertiary-butylethylbenzene between about 30-120 milliliters/hour are fed to the reactor, together with a gas stream consisting of about 400-800 milliliters/minute of air and about 500-1000 milliliters/minute of nitrogen. Assay of the liquid products and of the effluent gas from the condenser are employed to calculate the conversion and selectivity results. The reaction conditions and data calculations from 3 runs are summarized in the following Table.