Mobil Oil Corporation

Benjamin Gross

Wooyoung Lee

Madhava Malladi

Sterling E Voltz

Hartley Owen

James H Haddad

Klaus W Schatz

Byung C Choi

Donald M Nace

Solomon M Jacob

Michael P Ramage

Jong Lee

James H Beech

Heavy petroleum oils such as resids are subjected to visbreaking in the presence of a hydroaromatic hydrogen donor solvent having an aromatic and alpha-to-aromatic proton content each of at least 20 percent of the total solvent hydrogen. The amount of donor solvent is from 0.1 to 50, preferably 0.1 to 20, weight percent of the heavy oil feed. The visbreaking may be carried out at relatively high severities as the use of the donor solvent reduces coke formation as well as producing a product of reduced viscosity, pour point and sedimentation characteristics. Reaction severity is usually in the range of 250 to 1500 seconds ERT at 800.degree. F. (427.degree. C.) but may range up to 15000 seconds ERT. Suitable solvents may be obtained from catalytic cracking process, for example, FCC cycle oils, slurry oils and main column bottoms.

Visbreaking process

A fast fluidized bed regenerator of an FCC apparatus is improved by incorporating into the regenerator an internal riser, for more complete combustion of coke, and by providing a means of preventing catalyst flow reversals between the spent and regenerated beds of the catalyst.

Method and apparatus for regenerating cracking catalyst

The operation of FCC apparatus is improved by decreasing oil partial pressure in the FCC reactor riser by about 10 psia, as compared to the normal oil partial pressure in the riser, thereby increasing octane rating of the gasoline produced in the FCC unit. The oil partial pressure may be reduced by injecting a suitable amount of an inert diluent into the riser, or by decreasing throughput of the FCC reactor.

Increased gasoline octane in FCC reactor

Apparatus for regenerating cracking catalyst

A process is described for visbreaking a deasphalted hydrocarbon oil and subsequently reblending the recovered asphaltene fraction to produce a product of low viscosity and pour point and requiring less cutter stock oil as compared to conventional visbreaking processes.

Process for visbreaking resid deasphaltenes

In a fluid catalytic cracking (FCC) process and apparatus, the heat balance between the reactor and the regenerator of the FCC operation is partially uncoupled by transferring at least a portion of thermal energy from the reactor vessel downflow riser to the regenerator vessel. The transfer of thermal energy results in a higher regenerating temperature. The thermal energy is recirculated to the upstream section of the downflow reactor riser through a regenerated catalyst having higher temperature. Consequently, the outlet of the reactor vessel is maintained at a substantially constant temperature (e.g., 1000.degree. F.) and the rate of conversion of the oil feed and the octane number of gasoline produced in the process are increased.

Heat balance in FCC process and apparatus with downflow reactor riser

A fluid catalytic cracking (FCC) process and apparatus using a riser and a reactor for cracking of petroleum feeds in the presence of a catalyst and a regenerator for regenerating the spent catalyst are improved by providing a downflow riser. The downflow riser assures uniform distribution of the catalyst throughout the feed, decreases contact time of the catalyst with the feed and decreases the amount of coke made in the process.

FCC Reactor with a downflow reactor riser

In a fluid catalytic cracking (FCC) process and apparatus, the heat balance between the reactor and the regenerator of the FCC operation is partially uncoupled by transferring at least a portion of thermal energy from the reactor vessel riser to the regenerator vessel. The transfer of thermal energy results in a higher regenerating temperature. The thermal energy is recirculated to the bottom section of the reaction riser through a regenerated catalyst having higher temperature. Consequently, the outlet of the reaction vessel is maintained at a substantially constant temperature (e.g., 100.degree. F.) and the rate of conversion of the oil feed and the octane number of gasoline produced in the process are increased.

Heat balance in FCC process

A process is disclosed for enhancing the conversion of carbon monoxide within the regenerator of a cracking unit used to regenerate spent catalysts from the catalytic cracking of gas oil by the addition of controlled amounts of either copper chromite, cobalt chromite, or mixtures thereof. Conversion of carbon monoxide in the regenerator is accomplished while maintaining the efficiency of the cracking reaction at high levels.

Catalytic cracking process utilizing a copper chromite oxidation catalyst

A process is disclosed for enhancing the conversion of carbon monoxide within the regenerator of a methanol conversion unit used to regenerate spent catalysts from the conversion of methanol by the addition of controlled amounts of either copper chromite, cobalt chromite, or mixtures thereof. Conversion of carbon monoxide in the regenerator is accomplished while maintaining the efficiency of the methanol conversion unit at high levels.

Control of CO emissions in a process for producing gasoline from methanol

An improved catalytic process wherein trace amounts of a metal of period 5 and 6 of Group VIII or rhenium is added to the total catalyst inventory for cracking of gas oil is disclosed. With this improved process, the yield of gasoline, fuel oil, total cracked products, or predetermined combinations thereof, is maximized for the fluid catalytic cracking of any predetermined feed, usually a gas oil. The process employs a kinetic predictive or a correlative model of the cracking process to identify proper operating conditions, including CO.sub.2 /CO ratio in the effluent from the regenerator, and also requires control of the metal activity to achieve optimal conversion of CO to CO.sub.2 in the regenerator. Also disclosed is an improved method for control of a fluid catalytic process wherein the cracking catalyst comprises trace amounts of a metal selected from the group Pt, Pd, Rh, Ru, Ir, Os and Re.

Catalytic cracking process

A riser cracking operation is described for the production of gasoline and distillate material by the combination of cracking fresh gas oil charged to the base of a riser cracking zone for admixture with freshly regenerated catalyst to form a suspension thereof at an elevated cracking temperature, a second hydrocarbon fraction of more difficult cracking characteristics is charged to the suspension rising in the riser cracking zone at a point selected from 10 to about 30 feet above the riser bottom and the riser inlet temperature is restricted to be within the range of 900.degree. to 1000.degree. F.

Method for catalytic cracking heavy oils

In the fluid catalytic cracking process, improved adaptive behavior of the catalyst section with the regenerator operating in the complete CO-burning mode is achieved by including, as elements of control, variable preheat of the oil feed and variable recycle of regenerated catalyst to spent catalyst. In response to excursions of the regenerated catalyst temperature, such as would be caused by change of feedstock, the oil preheat temperature and recycle ratio are altered in a direction to restore the regenerated catalyst temperature to a predetermined value. The improved control system extends the useful control range, and it also diminishes counterproductive changes in severity induced by disturbances such as change of feedstock quality.

FCC Catalyst section control

In the fluid catalytic cracking process, improved adaptive behavior of the catalyst section with the regenerator operating in the complete CO-burning mode is achieved by including within the regenerator, as an element of control, variable recycle of regenerated to spent catalyst. In response to excursions of the regenerated catalyst temperature, such as would be caused by change of feedstock, the recycle ratio is altered in a direction to restore the temperature to a predetermined value. The improved control system extends the useful control range, and it also diminishes counterproductive changes in severity induced by disturbances such as change of feedstock quality.

The specific disclosure is directed to a catalytic cracking model wherein the reactant and product species are lumped according to molecular type and boiling range. The specific invariant lumping scheme includes paraffins, naphthenes, aromatic rings, and aromatic substituent groups.

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Cherry Hill, NJ, United States of America

Benjamin Gross