A process includes periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system, oligomerizing the olefin monomer within the reaction mixture to form an oligomer product, and periodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system. The reaction system includes a total reaction mixture volume and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect contact between the reaction mixture and a heat exchange medium. A ratio of the total heat exchanged surface area to the total reaction mixture volume within the reaction system is in a range from 0.75 in.sup.1 to 5 in.sup.1, and an oligomer product discharge rate from the reaction system is between 1.0 (lb)(hr.sup.1)(gal.sup.1) to 6.0 (lb)(hr.sup.1)(gal.sup.1).

Herein disclosed is a system for producing an organic, the system including at least one high shear mixing device having at least one rotor and at least one stator separated by a shear gap, wherein the shear gap is the minimum distance between the at least one rotor and the at least one stator; a pump configured for delivering a fluid stream comprising liquid medium and light gas to the at least one high shear mixing device, wherein the at least one high shear mixing device is configured to form a dispersion of the light gas in the liquid medium; and a reactor comprising at least one inlet and at least one outlet, wherein the at least one inlet of the reactor is fluidly connected to the at least one high shear mixing device, and wherein the at least one outlet is configured for extracting the organic therefrom.

An apparatus for halogenation of a polymer is disclosed. The apparatus includes a reactor, at least one light source, a stirrer and a heater. The reactor contains a slurry of the polymer. The light source is disposed outside of the reactor at a distance ranging from 0.5 centimeter to 2 centimeters for facilitating irradiance of the slurry. The light source radiates a light of wavelength in the range of 250 nm to 355 nm. The stirrer is adapted to agitate the slurry. The heater is adapted to heat the slurry of the polymer. The blades on the stirrer and light source are arranged in such a way that slurry is maintained in uniform motion and reacted homogeneously to achieve desired conversion efficiently.

When producing lithium sulfide by a reaction between a lithium raw material and hydrogen sulfide, the reaction is performed under relatively mild conditions compared to the conventional technology, so frequent repairs or replacements due to corrosion and breakdown of reactors and piping are not required, thereby improving the economic efficiency of the process. Since unreacted hydrogen sulfide and a solvent from which moisture has been removed are reused, process costs are reduced so that economic feasibility in mass production is ensured. Furthermore, moisture and water vapor generated in a lithium sulfide production reaction are effectively removed to prevent a reverse reaction into lithium hydroxide and promote a forward reaction so that high-quality lithium sulfide can be produced with high purity and high yield. In addition, particle size may be controlled in the micrometer range without a separate crushing space or crushing stage, thereby providing excellent convenience and mass production.