Abstract: A process for the removal of sulfur compounds from FCC catalytic naphtha which is simple to implement and is economical in operation operates by selectively hydrofining the cracked naphtha to remove sulfur without sacrificing octane (hydrodesulfurization typically around 85%) followed by a downstream alkylation which will remove residual sulfur from the gasoline boiling range. The alkylation is carried out using a solid, acidic molecular sieve catalyst under mild conditions to shift sulfur species from the lighter, olefin-rich portions of the naphtha to the heavy, olefin-poor gasoline. Separation of the heavy portion of the treated product followed by catalytic hydrodesulfurization or some other means (e.g. sorption) removes the sulfur from the heavy portion without losing significant octane value.

Abstract: Solid phosphoric acid (SPA) olefin oligomerization process units may be converted to operation with a more environmentally favorable solid catalyst. The SPA units in which a light olefin feed is oligomerized to form gasoline boiling range hydrocarbon product, is converted unit to operation with a molecular sieve based olefin oligomerization catalyst comprising an MWW zeolite material. Besides being more environmentally favorable in use, the MWW based zeolites offer advantages in catalyst cycle life, selectivity. After loading of the catalyst, the converted unit is operated as a fixed-bed unit by passing a C2- C4 olefinic feed and a light aromatic co-feed containing benzene to a fixed bed of the MWW zeolite catalyst to effect alkylation of the benzene with the aromatic co-feed, typically at a temperature from 150 to 350° C., a pressure not greater than 7000 kpa, usually less than 4000 kPa and an olefin space velocity up to 10 WHSV.

Abstract: A fixed-bed catalytic reformer unit is converted to moving bed reactor/cyclic regenerator operation by re-using the fixed bed reactors of the original unit as regenerator vessels operated in cyclic regeneration mode in a new catalyst regeneration section. A flow connection, suitably a liftpipe, is provided to convey spent catalyst from the spent catalyst outlet of a new moving bed reactor section to the converted regenerator section, together with a flow connection for regenerated catalyst from the regenerator section to the regenerated catalyst inlet of the new moving bed reactor section. A flow control distributor directs spent catalyst sequentially to each of the regenerator vessels to carry out the regeneration with regeneration gas. Each regenerator vessel is cycled through a fill, regeneration, discharge sequence to maintain a continuous flow of catalyst to and from the reactor section.