Shell Oil Comapny

Wesley A Parker

John E Gwyn

Donald E Hardesty

Thomas S Dewitz

Glenn R McCullough

A Haluk Bilgic

George P Hinds, Jr

Jack E Stanley

The invention here disclosed is a novel apparatus and method for the separation of solid and fluid phases in a horizontal elongated cyclone separator with a novel inclined solid dropout continuous and uninterrupted slot in the bottom to transfer a solid phase via primary mass separation from either an upflow or a downflow reactor in the initial portion of the cyclone separator to a downcomer which may be equipped with a stripping function. The instant horizontal elongated cyclone separator is constructed to ensure an elongated helical flow path of the vapor phase with a minor portion of the catalyst particles therein from one end of the cyclone separator to a withdrawal conduit to disengage via secondary centrifical separation a minor portion of the solid phase from the fluid phase. The minor portion of the solid phase is thereafter transmitted to the stripping function by a vertical downcomer interconnecting the stripping function and the bottom of the horizontal elongated cyclone separator. The entire apparatus is constructed so that the tangential velocity of the fluid across the upper section or lower section of the reactor tube divided by the superficial axial velocity of fluid across the cross section of the withdrawal conduit is greater than 0.2 which guarantees formation of the vortex in the horizontal elongated cyclone separator.

Reactor and horizontal cyclone separator with primary mass flow and

Catalyst and hydrocarbon vapors are separated in a cyclone zone attached to the discharge of a riser cracking operation. A vortex stabilizer separating the cyclone zone from a stripping zone allows stripping gas from the stripping zone to be passed upwardly into the cyclone zone countercurrent to the downward flow of catalyst, thereby improving the separation and stripping of gaseous hydrocarbons from separated catalyst. The combined cyclone-stripping zone reduces catalyst hydrocarbon contact time, thereby improving gasoline yield and olefin content, decreasing gas make, and reducing coke deposits.

Apparatus for the separation of fluid cracking catalyst particles from

An apparatus for reducing the pressure drop in a riser reactor equipped with a horizontal tee joint connection which uses a fluid injection means selectively located at a point juxtaposed to the connection of the horizontal and vertical tubes to prohibit fine particle catalysts from backflow down the elongated riser reactor which omission thereby provides (1) an easy upflow of catalysts and hydrocarbon vapors through the riser reactor and (2) an incentive for the flow of particles up through the elongated riser and transfer laterally to the horizontal tee joint connection.

Selective placement of fluid injection in a riser reactor equipped with

An apparatus to reduce the pressure drop in a riser reactor equipped with a horizontal tee joint connection which uses a mechanical implant located at a point juxtaposed the connection of the horizontal and vertical tubes to prohibit fine particle catalysts from backflow down through the elongated riser reactor which thereby provides an easy upflow of catalysts through the riser reactor.

Mechanical implant to reduce back pressure in a riser reactor equipped

Catalyst and hydrocarbon vapors are separated in a cyclone zone attached to the discharge of a riser cracking operation. Vortex stabilizing means separating the cyclone zone from a stripping zone allows stripping gas from said stripping zone to be passed upwardly into said cyclone zone countercurrent to the downward flow of catalyst, thereby improving the separation and stripping of gaseous hydrocarbons from separated catalyst. The combined cyclone-stripping zone reduces catalyst hydrocarbon contact time, thereby improving gasoline yield and olefin content, decreasing gas make, and reducing coke deposits.

Separation of fluid cracking catalyst particles from gaseous hydrocarbons

An oxygen-containing gas distribution apparatus is dicslosed which can be employed in the fluidized bed regeneraton of carbon-contaminated catalysts, such as cracking catalysts.Said apparatus comprises a plurality of gas discharge nozzles affixed to at least one manifold member substantially horizontally disposed at the lower end of the regeneration chamber, said nozzles being restricted in internal cross-sectional area in their upstream portion connected to the manifold member and expanded in the internal cross-sectional area of their downstream portion such that a) the numerical ratio of the difference between the diameter of the downstream portion and the diameter of the upstream portion divided by the length of the downstream portion taken in the direction of gas flow does not exceed 0.18 and b) the ratio of the diameter of the upstream portion to its length taken in direction of gas flow does not exceed 1.67.

Oxygen-containing gas distribution apparatus employed in fluidized bed

In fluidized bed regeneration of carbon-contaminated catalysts, such as cracking catalysts, wherein at least a portion of the oxygen-containing gas required for fluidization and burn-off of carbon deposits is introduced as a separate stream into the dense phase of the fluidized catalyst, contained in the regeneration chamber, by means of a plurality of gas discharge nozzles, affixed to at least one manifold member substantially horizontally disposed at the lower end of the regeneration chamber, catalyst attrition is reduced and backflow of catalyst particles into the nozzles is minimized by utilizing gas discharges which are restricted in internal cross-sectional area in their upstream portion connected to the manifold member and expanded in the internal cross-sectional area of their downstream portion such that (a) the numerical ratio of the difference between diameter of the downstream portion and the diameter of the upstream portion divided by the length of the downstream portion taken in the direction of gas flow does not exceed 0.18 and (b) the ratio of the diameter of the upstream portion to its length taken in direction of gas flow does not exceed 1.67.

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Houston, TX, United States of America

Wesley A Parker