Abstract: Systems, reactors, and processes for regenerating ionic liquid using catalyst. A plurality of tubular reactors are provided having a first end and a second end and catalyst particles disposed in the tubular reactor between the first end and the second end. A line supplies separated ionic liquid catalyst to the first end of the tubular reactor. Hydrogen is also supplied. Regenerated ionic liquid catalyst is recovered from the second end of the tubular reactor. The inner surface of the tubular reactor is preferably non-corrosive or non-reactive. A fluoropolymer lining may be used. The tubular reactors are modular, and may be changed out with the catalyst inside when the catalyst are to be replaced.

Abstract: A regenerator vessel for adsorbing halogen-containing material from a regenerator vent gas stream has a plurality of catalyst nozzles disposed at a top portion of the regenerator vessel. A first gas outlet is associated with a chlorination zone, and a second gas outlet associated with a combustion zone. A drying zone is in fluid communication with an air heater and the drying zone located in a bottom portion of the regenerator vessel. The first gas outlet is configured to withdraw a first gas stream from the chlorination zone and the second gas outlet is configured to withdraw a second gas stream from the combustion zone. The top portion of the regenerator vessel has an adsorption zone having a vent gas inlet port, a vent gas outlet port, and a portion of an annular catalyst bed.

Abstract: Processes for the direct alkylation of ethylene with isobutane or isopentane using a highly active ionic liquid alkylation catalyst are described. Ethylene is sent to a high-temperature alkylation reactor loop, and C3, C4, and C5 olefins are routed to a low temperature alkylation reactor loop. In each reactor, the olefins are contacted with an excess of isobutane or isopentane in the presence of a highly active ionic liquid catalyst. Portions of the reactor effluent streams are fed to a common downstream catalyst separation and product fractionation sections. The remainder of the reactor effluent is recycled back to the respective alkylation reactor.

Abstract: Processes for the direct alkylation of ethylene with isobutane or isopentane using a highly active ionic liquid alkylation catalyst are described. Ethylene is sent to a high-temperature alkylation reactor loop, and C3, C4, and C5 olefins are routed to a low temperature alkylation reactor loop. In each reactor, the olefins are contacted with an excess of isobutane or isopentane in the presence of a highly active ionic liquid catalyst. Portions of the reactor effluent streams are fed to a common downstream catalyst separation and product fractionation sections. The remainder of the reactor effluent is recycled back to the respective alkylation reactor.

Abstract: A regenerator vessel for adsorbing halogen-containing material from a regenerator vent gas stream has a plurality of catalyst nozzles disposed at a top portion of the regenerator vessel. A first gas outlet is associated with a chlorination zone, and a second gas outlet associated with a combustion zone. A drying zone is in fluid communication with an air heater and the drying zone located in a bottom portion of the regenerator vessel. The first gas outlet is configured to withdraw a first gas stream from the chlorination zone and the second gas outlet is configured to withdraw a second gas stream from the combustion zone. The top portion of the regenerator vessel has an adsorption zone having a vent gas inlet port, a vent gas outlet port, and a portion of an annular catalyst bed.

Abstract: Hydroprocessing reactor internals height reduction is achieved by placing a mixing chamber above the collection tray. The mixing chamber has spillways on the top (top spillways) and the side of the mixing chamber (side spillways) for fluid entry. The design of the spillways has a significant impact on pressure drop. The pressure drop is reduced by having wide shallow spillways rather than narrow and deep spillways without impacting mixing performance. With both side and top spillways, the height of the mixing chamber can be reduced significantly with minimal impact on fluid mixing and pressure drop.

Abstract: The hydroprocessing reactor quench zone internals comprise a collection tray, a mixing chamber, a ring quench distributer, a rough liquid distribution tray, and a vapor-liquid distribution tray. The rough liquid distribution tray has a central pan for receiving vapor and liquid out of the mixing chamber and multiple fluid distribution troughs attached to the central pan that extended radially outwards with the outer end close to the reactor shell. The fluid distribution troughs can include at least one longitudinal baffle, or at least one cross baffle, or both, and optionally an end baffle. The baffles improve the liquid and/or vapor flow in the rough liquid distribution tray.

Abstract: Systems, reactors, and processes for regenerating ionic liquid using catalyst. A plurality of tubular reactors are provided having a first end and a second end and catalyst particles disposed in the tubular reactor between the first end and the second end. A line supplies separated ionic liquid catalyst to the first end of the tubular reactor. Hydrogen is also supplied. Regenerated ionic liquid catalyst is recovered from the second end of the tubular reactor. The inner surface of the tubular reactor is preferably non-corrosive or non-reactive. A fluoropolymer lining may be used. The tubular reactors are modular, and may be changed out with the catalyst inside when the catalyst are to be replaced.

Abstract: Hydroprocessing reactor internals height reduction is achieved by placing a mixing chamber above the collection tray. The mixing chamber has spillways on the top (top spillways) and the side of the mixing chamber (side spillways) for fluid entry. The design of the spillways has a significant impact on pressure drop. The pressure drop is reduced by having wide shallow spillways rather than narrow and deep spillways without impacting mixing performance. With both side and top spillways, the height of the mixing chamber can be reduced significantly with minimal impact on fluid mixing and pressure drop.

Abstract: Multiple downcomer trays having increased active area for vapor-liquid contact and separation are described. The increased active area of the tray is achieved by adding raised bubble promoters surrounded by perforated vertical contactors on the tray deck. The bubble promoters and surrounding vertical contactors are located under the downcomers from the tray above. The bubble promoter and surrounding vertical contactor promote uniform fluid flow and contact.

Abstract: Multiple downcomer trays having increased active area for vapor-liquid contact and separation are described. The increased active area of the tray is achieved by adding raised bubble promoters surrounded by perforated vertical contactors on the tray deck. The bubble promoters and surrounding vertical contactors are located under the downcomers from the tray above. The bubble promoter and surrounding vertical contactor promote uniform fluid flow and contact.