A method (10) of synthesizing Fischer-Tropsch products (20) includes feeding a synthesis gas (30) to a moving-bed Fischer-Tropsch synthesis reactor (16) containing a Fischer-Tropsch catalyst in a moving catalyst bed and catalytically converting at least a portion of the synthesis gas (30) in the moving catalyst bed to Fischer-Tropsch products (20). The Fischer-Tropsch products (20) are removed from the moving-bed Fischer-Tropsch synthesis reactor (16). The method (10) further includes, while the moving-bed Fisher-Tropsch synthesis reactor (16) is on-line, withdrawing a portion (50) of the Fischer-Tropsch catalyst from the moving-bed Fischer-Tropsch synthesis reactor (16), adding a reactivated Fischer-Tropsch catalyst (57, 58) to the moving-bed Fischer-Tropsch synthesis reactor (16), and adding a fresh Fischer-Tropsch catalyst (60,58), in addition to the reactivated catalyst (57,58), to the moving-bed Fischer-Tropsch synthesis reactor (16).

A method (10) of synthesizing Fischer-Tropsch products (20) includes feeding a synthesis gas (30) to a moving-bed Fischer-Tropsch synthesis reactor (16) containing a Fischer-Tropsch catalyst in a moving catalyst bed and catalytically converting at least a portion of the synthesis gas (30) in the moving catalyst bed to Fischer-Tropsch products (20). The Fischer-Tropsch products (20) are removed from the moving-bed Fischer-Tropsch synthesis reactor (16). The method (10) further includes, while the moving-bed Fisher-Tropsch synthesis reactor (16) is on-line, withdrawing a portion (50) of the Fischer-Tropsch catalyst from the moving-bed Fischer-Tropsch synthesis reactor (16), adding a reactivated Fischer-Tropsch catalyst (57, 58) to the moving-bed Fischer-Tropsch synthesis reactor (16), and adding a fresh Fischer-Tropsch catalyst (60,58), in addition to the reactivated catalyst (57,58), to the moving-bed Fischer-Tropsch synthesis reactor (16).

Methods for producing propylene by the dehydrogenation of propane are provided. Methods can include introducing a first gas mixture including propane to a dehydrogenation catalyst at a temperature of at least about 570 C., introducing a second gas mixture including steam and air to the dehydrogenation catalyst at a temperature of at least about 550 C., and allowing the second gas mixture to subsist therewith for at least about one hour. Methods can further include introducing a third gas mixture including hydrogen to the dehydrogenation catalyst at a temperature of at least about 500 C.

Methods for producing propylene by the dehydrogenation of propane are provided. Methods can include introducing a first gas mixture including propane to a dehydrogenation catalyst at a temperature of at least about 570 C., introducing a second gas mixture including steam and air to the dehydrogenation catalyst at a temperature of at least about 550 C., and allowing the second gas mixture to subsist therewith for at least about one hour. Methods can further include introducing a third gas mixture including hydrogen to the dehydrogenation catalyst at a temperature of at least about 500 C.

A method for producing a dehydrogenated product and a coked catalyst, then introducing an oxygen-containing fluid, combusting at least a portion of the coke disposed on the catalyst in the presence of the oxygen-containing fluid to produce a decoked catalyst. An apparatus for introducing fluid into a reactor, comprising a first inlet conduit configured to convey a first gas, a second inlet conduit configured to convey a second gas, and an outlet conduit configured to convey the first gas and the second gas into a reactor, wherein there is an acute angle between a longitudinal axes of the first inlet conduit and a longitudinal axis of the second inlet conduit and an obtuse angle between a longitudinal axis of the outlet conduit and the longitudinal axis of the second inlet conduit and a pre-distributor disposed, in one embodiment on the inner surface, within the first inlet conduit is disclosed.

A method for producing a dehydrogenated product and a coked catalyst, then introducing an oxygen-containing fluid, combusting at least a portion of the coke disposed on the catalyst in the presence of the oxygen-containing fluid to produce a decoked catalyst. An apparatus for introducing fluid into a reactor, comprising a first inlet conduit configured to convey a first gas, a second inlet conduit configured to convey a second gas, and an outlet conduit configured to convey the first gas and the second gas into a reactor, wherein there is an acute angle between a longitudinal axes of the first inlet conduit and a longitudinal axis of the second inlet conduit and an obtuse angle between a longitudinal axis of the outlet conduit and the longitudinal axis of the second inlet conduit and a pre-distributor disposed, in one embodiment on the inner surface, within the first inlet conduit is disclosed.

Disclosed are processes for rejuvenating catalysts comprising at least one Group 10 metal and a microporous crystalline metallosilicate, and hydrocarbon conversion processes including such rejuvenation processes. In an aspect, the rejuvenation process comprises contacting a deactivated catalyst comprising at least one Group 10 metal and a microporous crystalline metallosilicate with an oxygen-containing gaseous stream under conditions comprising a temperature ranging from about 250 C. to about 375 C. and a pressure of up to about 100 bar. In a further aspect, the rejuvenation process comprises contacting a deactivated catalyst comprising at least one Group 10 metal, at least one rare earth metal, and a microporous crystalline metallosilicate with an oxygen-containing gaseous stream under conditions comprising a temperature ranging from about 250 C. to about 500 C. and a pressure of up to about 100 bar.

A process for regenerating catalyst particles is disclosed. The process includes the steps: (a) withdrawing a regeneration zone effluent comprising halogen from a regeneration zone, wherein the regeneration zone contains catalyst particles comprising halogen; (b) contacting a first portion of the regeneration zone effluent with adsorbent in a first adsorption zone, removing halogen from the first portion of the regeneration zone effluent, and withdrawing from the first adsorption zone a first adsorption zone effluent; (c) contacting the first adsorption zone effluent with a water removing material to create a first water-depleted stream; and (d) passing the first water-depleted stream to the regeneration zone. Other embodiments include different orders of the steps.

A process for regenerating catalyst particles is disclosed. The process includes the steps: (a) withdrawing a regeneration zone effluent comprising halogen from a regeneration zone, wherein the regeneration zone contains catalyst particles comprising halogen; (b) contacting a first portion of the regeneration zone effluent with adsorbent in a first adsorption zone, removing halogen from the first portion of the regeneration zone effluent, and withdrawing from the first adsorption zone a first adsorption zone effluent; (c) contacting the first adsorption zone effluent with a water removing material to create a first water-depleted stream; and (d) passing the first water-depleted stream to the regeneration zone. Other embodiments include different orders of the steps.

A catalyst comprising a Group IIIA metal, a Group VIII noble metal, and an optional promoter metal, on a support selected from silica, alumina, silica-alumina compositions, rare earth modified alumina, and combinations thereof, doped with iron, a Group VIB metal, a Group VB metal, or a combination thereof, offers decreased reactivation time under air soak in comparison with otherwise identical catalysts. Reducing reactivation time may, in turn, reduce costs, both in inventory and capital.