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process. Two catalysts were prepared under comparable conditions except that the oxy-ccimpound, a silicate in one instance, contained possibly as much as 5 % of 20+ micron particles, and in the other the same material was subjected to comminution such ,that the particles were essentially all in the range 1-10 microns. In the prepa› ration of the catalyst the components were present in the proportions of 1 gram atom of potassium, 13.4 cc. of the silicate, and 5.4 Xl0- 3 mols of oleic acid. Each cata› lyst was tested as in Example 2 and then inspected. The catalyst prepared from the 1-10 micron sized silicate was especially suited for use in a continuous reactor; the other had agglomerated to • a hard unreactive solid. These and similar data indicate that for the preparation of sta:ble superfinely divided alkali metal containing ally! alkylation catalysts, not only must an unreactive solid compound be used, but it must ,be of a particle size com› parable to that of the active component. 

In the preferred manner, a series of catalysts was pre› pared and tested, as in Example 2, using 10 parts solid (alkali metal plus oxy-compound, Ca, Mg, Al silicate), 90 parts of refined paraffin white oil, and oleic acid in the proportions listed in Table V following. 

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These data indicate that while at least about 8-10 cc. of a mixed crystalline metamorphic silicate is required to yield a stable catalyst, as much as 41 cc. of the super› finely divided solid is an excess. No particular disad› vantage was noted by reason of the excess in this test. In a continuous unit, however, unneeded oxy-compound detracts from the reactor unit volume• production effi› ciency. When other unreactive superfinely divided oxy› compounds are used, similar results obtained, although minor variations in relative amounts may be desirabie. On the other hand, when the oxy-compound used has a particle size less than about 0.1 micron, i.e., a material having a size ‰o and less of the alkali metal particles normally attainable, no stable complex results. Thus, when for each gram atom of alkali metal about 13.4 cc. of calcium phosphate ha:ving an estimated particle size of 0.03 micron was substituted, the potassium agglomerated and no allyl alkylation catalyst complex was obtained. 

Catalyst preparation (A).-In a typical catalyst prepa› ration, an oxy-compound, for example, sodium metasili› cate, having a particle sizing in the range 1~10 microns and practically freed of adsorbed extraneous matter, is dispersed in an aprotic hydrocarbon medium, such as an alkane, cycloalkane, and a paraffinic petroleum fraction practically freed • of aromatic hydrocarbon and partially oxidized hydrocarbon impurities. Even where 1-10 microns presized solid particles are used, it is frequently desirable to subject the solid admixed with the paraffinic hydrocarbon (weight ratio hydrocarbon to solid about 85-15) to a period of ball-milling or the equivalent. Where presized particles of the desired . solid oxy› compound are not available, the powdered solid may be subjected as above to milling in the presence of the par~ affinic hydrocarbon in a ball, paint, or colloid mill until 

## EXAMPLE 6 

## EXAMPLE 7 

inspection under high powered microscope indicates the particles are properly sized. 

The weight ratio of dispersed solid in paraffin is ad› justed in accordance with the catalyst concentration desired by adding adq.itional hydrocarbon after transfer of ,the solid-oil dispersion to a suitable vessel fitted with an efficient dispersing means such as an ultra high speed (10,000-15,000 r.p.m.) high shear blade fitted stirring mechanical element, an ultrasonic vibrator or the equiva- lent. 

The dispersion is th.en heated to a temperature above the melting point of the alkali metal to be used and pref› erably to 100-120° C. and the alkali metal and the polar organic compound are introduced into the slurry and con- tacted, while high speed stirring or the like is continued. For the preparation of the more concentrated catalyst3 incremental addition is usually made. The dispersing action is continued at temperature for a period sufficient to facilitate even distribution of the catalyst components and some conditioning of the associated complex. A pe› riod of about 0.5 to 1 hour usually is adequate; however, a positive determination is possible by inspection of a sample under the microscope. Particle sizes should be less than about 15 microns. 

Ally! alkylation catalysts prepared in this manner are highly reproducible, are stable to temperature fluctua› tions under ally! alkylation conditions, and consistently have reactivities at least 50 to 100% higher than the ally! alkylation catalysts known in the art. Representative catalysts thus prepared have produced from 1500-2000 kilograms of propene dimer per kilogram of potassium used to prepare the catalyst up to the termination of the experimental run for reasons other than catalyst deactiva› tion. 

(B) In a second ally! alkylation catalyst preparation, 232 grams of crystalline metamorphic magnesium, cal› cium, and aluminum silicate were ball-milled in the presence of 1,318 grams of refined white oil until micro› scopic inspections of samples indicated the particle sizing was in the 1-10 micron range. The mixture was then transferred to a 5 liter stainless steel flask equipped with a high speed stirrer and the mixture diluted to 3.3 liters by the addition of white oil. Under an atmosphere of nitrogen the mixture was •heated to 120° C. for one half- hour, at which time while • stirring at• high. speeds 225 grams of potassium were added in three increments with about 5 minute intervals between the additions and with a 30 minute continuation after the last addition. One› half liter of white oil containing 4.6 grams of oleic acid was then added in two increments into the slurry and the mixture was stirred for an additional 30 minutes. The particles were found to be in the 2-15 micron size range. A further addition of 5.3 grams of oleic acid in .25 liter of oil were made, and the maximum particle size found was 7 microns. A 200 gram aliquot of the slurry was transferred -to a 500 cc. three-necked flask fitted with a stirrer, and the flask and contents were heated to 210° C. under an atmosphere of nitrogen. The nitrogen atmosphere was replaced with hydrogen and the system was held at 210-220° C. for 35 minutes. The catalyst thus prepared was cooled to 130° C. under an atmosphere of hydrogen, and then to room tempera› ture under an atmosphere of nitrogen. The maximum particle size was 3 microns. Titration of the aliquot was 2-methoxy ethanol indicated 146% of the theoretical hydrogen expected for potassium, showing the presence of potassium hydride. This catalyst when tested in use, for example, to catalyze the dimerization of propene at 150° C. and a pressure of 1200 p.s.i.g. required no in- duction period and had an exceptional catalytic activity. Inspections of the used catalyst indicated the particle size to be less than 6 microns in size. When the hydride allyl alkylation catalyst was prepared in an analogous man› _ner, except that the oxy-compound and polar organic compound were omitted, inspection indicated that the 

