Abstract: Apparatus for liquid feed dispersion in fluid catalytic cracking systems is disclosed wherein an improved fluidized catalytic cracking nozzle assembly having a nozzle unit so constructed that substantially all liquid fed through the unit is converted to mist-sized particles over a wide-angle dispersion pattern, the unit being recessed within a protective pipe having a shield on the inside thereof in the area of the recess, without concurrent addition of steam to affect liquid that may flow therethrough.

Abstract: An improved liquid hydrocarbon feed method is disclosed wherein substantially all of the liquid is converted to mist sized particles over a wide angled dispersion pattern without a concurrent shroud of steam or water. Such dispersion promotes vapor phase catalytic reaction between hydrocarbon vapors and fluidized catalyst in a reaction time of 1 to 3 seconds. The misting nozzle is characterized by a swirl chamber to which the full hydrocarbon feed, with or without steam included in the feed, is supplied for centrifugal rotation by vane members to form a free vortex. The flow is then released through a reduced area square-edge orifice having a short throat to form and maintain a characteristic "vena contrata" from such an orifice during flow into the catalyst stream in the riser reactor for dispersion over a wide angled conical dispersion pattern. Such flow from the orifice allows the nozzle to be recessed out of the flowing catalyst stream.

Abstract: Method and apparatus for liquid feed dispersion in fluid catalytic cracking systems wherein an improved fluidized catalytic cracking nozzle assembly having a nozzle unit so constructed that substantially all liquid fed through the unit is converted to mist-sized particles over a wide-angle dispersion pattern, the unit being recessed within a protective pipe having a shield on the inside thereof in the area of the recess, is disclosed.

Abstract: An improved liquid hydrocarbon feed method is disclosed wherein substantially all of the liquid is converted to mist sized particles over a wide angled dispersion pattern without a concurrent shroud of steam or water. Such dispersion promotes vapor phase catalytic reaction between hydrocarbon vapors and fluidized catalyst in a reaction time of 1 to 3 seconds. The misting nozzle is characterized by a swirl chamber to which the full hydrocarbon feed, with or without steam included in the feed, is supplied for centrifugal rotation by vane members to form a free vortex. The flow is then released through a reduced area square-edge orifice having a short throat to form and maintain a characteristic "vena contrata" from such an orifice during flow into the catalyst stream in the riser reactor for dispersion over a wide angled conical dispersion pattern. Such flow from the orifice allows the nozzle to be recessed out of the flowing catalyst stream.

Abstract: A vapor recovery shroud of relatively small size is positioned in a large diameter catalyst disengaging vessel of a fluid catalytic cracking system so that vapor released directly from the riser reactor pipe must execute a reversal of flow direction to enter the vapor recovery shroud which results in a fast, efficient separation of reactive hydrocarbons from spent catalyst. At the same time vapors from the stripper and catalyst are separated by gravity and inertia in the large diameter separation vessel so that stripper vapors also vent through the vapor recovery shroud. Vapor is vented from the vapor recovery shroud through cyclone means confined within the disengaging vessel. Preferably, the inlet to the vapor recovery shroud is located adjacent to the riser reactor outlet because this location is the most rarefield in catalyst density and provides the shortest path for hydrocarbon vapors to exit the hot separation vessel and enter a distillation system.

Abstract: A vapor recovery shroud of relatively small size is positioned in a large diameter catalyst disengaging vessel of a fluid catalytic cracking system so that vapor released directly from the riser reactor pipe must execute a reversal of flow direction to enter the vapor recovery shroud. At the same time catalyst and vapors from the stripper are separated by gravity and inertia in the large diameter separation vessel so that stripper vapors may also vent through the vapor recovery shroud. Vapor is vented from the vapor recovery shroud through cyclone means confined within the disengaging vessel. Preferably, the inlet to the vapor recovery shroud is located adjacent to the riser reactor outlet because this location is the most rarefied in catalyst density and provides the shortest path for hydrocarbon vapors to exit the hot separation vessel and enter a distillation system.