Mobil Oil Corporation

Other

Amos A Avidan

Samuel A Tabak

David L Johnson

Frederick J Krambeck

Fritz A Smith

Jorge L Soto

Tai-Sheng Chou

Sergei Yurchak

Arthur A Chin

Reuel Shinnar

Hartley Owen

David Lawrence Stern

Scott A Stevenson

Mark F Mathias

Gary J Green

Gerald J Teitman

Ronald M Gould

J Scott Buchanan

Margaret Nemet-Mavrodin

Nazeer A Bhore

Khushrav E Nariman

Raghu K Menon

Joseph F Sodomin, Iii

Susan Patricia Donnelly

Anthony Y Kam

Peter M Adornato

Steven E Kane

A process for thermally and catalytically upgrading a heavy feed in a single riser reactor FCC unit is disclosed. A heavy feed is cracked in the base of the riser at higher than normal cracking temperatures for at least 1.0 seconds of vapor residence time, then quenched. Quenching with large amounts of quench, preferably downstream of the mid point of the riser, increases conversion as compared to use of the same amount of quench within one second. Small amounts of quench, near the riser outlet, crack heavy feed roughly as well as large amounts of quench, near the base of the riser. High velocity, atomizing quench nozzles reduce riser pressure and/or catalyst slip in downstream portions of the riser, further increasing gasoline selectivity and reducing coke yields.

Catalytic cracking with delayed quench

There is provided a process directed to the use of gases containing or mixed with carbon monoxide, such as synthesis gas, to aid in the regeneration of sulfur oxide-sorbed solid oxides, such as magnesium aluminates or spinels. This process is especially useful in applications where the solid oxide is used to purify the flue gas stream from an FCC regenerator, coal or oil-fired plant, power plant or process heat furnace, or the tail gas from a Claus plant. The process is also useful to remove sulfur oxides from flue gases produced in solid fuel combusters. According to this invention, carbon monoxide may be used alone or in combination with other gases to make the regeneration of the solid oxide exothermic or less endothermic, thereby improving the effectiveness of the regeneration.

Sox sorbent regeneration

A process and apparatus for controlling the flow of FCC catalyst around a catalyst regenerator, using a non-mechanical valve, is disclosed. The preferred non-mechanical valve provides a de-aeration section, addition of fluidizing gas, a 'U' trap seal, and venturi gas outlet on the top of the trap, for reliable flow control of non-uniform settling particles such as FCC catalyst. Control of the flow of a fluidizing gas to such a valve changes the flow properties of the FCC catalyst and permits flow control without resort to plug valves, or other internal mechanical valves, which are difficult to use in the harsh environment experienced within FCC regenerators.

Process and apparatus for non-mechanical flow control of catalyst around

Oxides of nitrogen (NO.sub.x) emissions from an FCC regenerator are reduced by forcing the regenerator to operate between full and partial CO burn mode. Operating with less than 1 mole % O2 and up to 1 or 2% CO in the flue gas creates conditions which oxidize nitrogen compounds in coke on spent catalyst to NOx, and simultaneously convert NOx in the regenerator to nitrogen. A downstream CO boiler can burn this low CO flue gas without producing large amounts of NOx. Most NOx emissions can be eliminated. An apparatus, with the regenerator air:coke ratio controlled by both CO and O2 analyzers monitoring regenerator flue gas, is also disclosed.

FCC of nitrogen containing hydrocarbons and catalyst regeneration

A process and apparatus for achieving hot catalyst stripping of spent FCC catalyst in a stripper mounted over a bubbling bed regenerator. Hot catalyst stripping is achieved by indirect transfer of heat from the regenerator to the stripper. Heat pipes, surface modifications such as fins on the stripper vessel, or use of a stripper in, or connective with, a heat exchange tube bundle may be used to heat spent catalyst with heat from the regenerator dilute phase, without transferring catalyst from the regenerator. The benefits of hotter catalyst stripping are achieved, without increasing catalyst traffic in the regenerator.

Process and apparatus for indirect heating of catalyst stripper above a

A process and apparatus are disclosed for achieving turbulent or fast fluidized bed regeneration of spent FCC catalyst in a bubbling bed regenerator having a stripper mounted over the regenerator and a stripped catalyst standpipe within the regenerator. A coke combustor vessel is immersed in, and in open fluid communication with, the bubbling dense bed of the existing regenerator vessel. Spent catalyst is discharged into the coke combustor, mixes with hot regenerated catalyst which flows into the coke combustor, and regenerated with combustion air in a turbulent or fast fluidized bed. Catalyst and flue gas are discharged up into a dilute phase transport riser, preferably into cyclone which separate hot regenerated catalyst from flue gas. Regenerated catalyst is collected in the bubbling dense bed surrounding the coke combustor, and some is recycled by flowing into the coke combustor for direct contact heat exchange.

Process and apparatus for fast fluidized bed regeneration of catalyst in

A method is disclosed for increasing heat transfer efficiency between a conduit and a gas flowing through the conduit by fluidizing in the gas stream a Geldart Type A powder having controlled fines content. The invention further provides a method for integrating two fluid beds to transfer heat from a heat source to a fluid-bed reaction zone.

Using fluidized particles

A circulating fluid bed combustion (CFBC) unit, which burns a carbon and nitrogen containing fuel to produce heat and flue gas comprising NO.sub.x, operates with reduced emissions of NO.sub.x from the flue gas by adding to the circulating fluid bed a catalytically effective amount of a DeNO.sub.x catalyst, such as bismuth oxide on a silica/alumina support. The DeNO.sub.x catalyst may circulate freely with the circulating inventory of particulates in the CFB, or can be disposed on a heavier particle which 'slips' and has an extended residence time in the combustion zone where the carbonaceous fuel is burned. A CO combustion promoter, such as Pt on silica/alumina may also be present.

Reducing NO.sub.x emissions from a circulating fluid bed combustor

A fluid bed catalytic paraffin upgrading process is disclosed. By closely controlling catalyst particle size distribution and density, together with feedstock superficial vapor velocity, the fluid bed is maintained in a turbulent flow regime. Surprisingly, maintaining the fluid bed in a turbulent flow regime shifts the product selectivity away from methane and ethane and toward the more valuable products hydrogen, light olefins and C.sub.5 + gasoline. In the most preferred embodiment, the catalyst contains a dehydrogenation metal component such as gallium, zinc, platinum or rhenium to provide a C.sub.5+ gasoline product rich in aromatics. Catalysts useful in the inventive process include zeolites as well as layered siliceous materials.

Turbulent fluid bed paraffin conversion process

A catalytic reactor system for cracking heavy oil in a FCC vertical reactor with lift gas. Olefinic light cracking gas separated from the FCC effluent is upgraded in a catalytic reactor to increase gasoline production. Byproduct light paraffinic gas from the second reactor is recycled to the FCC reactor as lift gas.

Integrated catalytic reactor system with light olefin upgrading

A known method for passivating contaminant metals on an FCC catalyst comprises treating the catalyst with a sufficient amount of a sulfur-containing compound capable of associating with the contaminant metals when in contact therewith. An improvement comprises contacting the catalyst with the sulfur-containing compound for at least 3 seconds. In another embodiment of the invention, the improvement comprises contacting the catalyst with the sulfur-containing compound in a separate treatment vessel.

Method for passivating metals on an FCC catalyst

Process and apparatus for upgrading light olefinic crackate gas from a fluidized catalytic cracking unit having a riser reactor for contacting hot solid cracking catalyst with a heavy hydrocarbon feedstock, said light crackate gas containing ethene, propene and other C.sub.1 -C.sub.4 lower aliphatics, comprising the steps of:

Integrated catalytic cracking process with light olefin upgrading

Addition of a CO combustion promoter to a circulating fluid bed (CFB) combustion unit and reduction of the air addition rate to 100-110% of stoichiometric improves the efficiency of CO burning, reduces emissions of CO and improves the efficiency of the unit. Stable, reduced temperature operation with air rates close to stoichiometric, reduces NO.sub.x emissions. A circulating (100-400 micron particles) or fast settling (400-1200 micron particle) CO combustion promoter may be used.

Circulating fluid bed combustion with CO combustion promoter and reduced

Addition of a readily fluidizable, 100-400 micron average diameter particular CO combustion promoter to a circulating fluid bed (CFB) combustion unit improves the efficiency of CO burning, reduces emissions of CO and improves the efficiency of the unit.

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Yardley, PA, United States of America

Amos A Avidan