초록 ▼

A method is disclosed for cracking a carbo-metallic oil feed containing high amounts of coke forming carbonaceous materials as characterized by a carbon residue on pyrolysis of at least about 1 and by a level of heavy metal(s) of at least about 5.5 ppm by weight of Nickel Equivalents. The method inc

A method is disclosed for cracking a carbo-metallic oil feed containing high amounts of coke forming carbonaceous materials as characterized by a carbon residue on pyrolysis of at least about 1 and by a level of heavy metal(s) of at least about 5.5 ppm by weight of Nickel Equivalents. The method includes contacting the feed with cracking catalyst bearing an accumulation of at least about 3,000 ppm by weight of Nickel Equivalents of heavy metal(s) and with additional material including water. The resultant stream flows through a progressive flow type reactor for a vapor residence time of about 0.5 to about 6 seconds at conditions sufficient for causing a conversion per pass of about 60% to about 90%. The additional material is added in a weight ratio relative to feed of up to about 0.4 and includes water in a weight ratio relative to feed of at least about 0.04. The water may be introduced as steam and/or liquid water. After such contact, catalyst is separated from product vapors and thereafter regenerated with oxygen-containing gas under conditions sufficient to reduce carbon on catalyst to about 0.25 percent by weight or less while maintaining a CO:CO2 molar ratio of at least about 0.25 in combustion gases in heat exchange contact with the catalyst.

대표청구항 ▼

A process for economically converting carbo-metallic oils to lighter products, comprising: I. providing a converter feed which contains at least about 70% by volume of 650°F.+material characterized by a carbon residue on pyrolysis of at least about 2 and by containing at least about 5.5 ppm by weigh

A process for economically converting carbo-metallic oils to lighter products, comprising: I. providing a converter feed which contains at least about 70% by volume of 650°F.+material characterized by a carbon residue on pyrolysis of at least about 2 and by containing at least about 5.5 ppm by weight of Nickel Equivalents of heavy metal(s); II. bringing said converter feed together with cracking catalyst having an equilibrium microactivity test conversion activity level of at least about 60 volume percent and bearing an accumulation of at least about 3,000 ppm by weight of Nickel Equivalents of heavy metal(s), expressed as metal(s) on regenerated equilibrium catalyst, and with additional material in a weight ratio relative to feed of up to about 0.4 including H2O in a weight ratio relative to feed of at least about 0.04 to form a stream comprising a suspension of said catalyst in said feed and said additional material wherein the catalyst to feed weight ratio is at least about 6 and the ratio of the partial pressure of the additional material relative to the partial pressure of the feed is in the range of about 0.8 to about 4, and causing the resultant stream to flow at a linear velocity of at least about 35 feet per second through a progressive flow type reactor having an elongated reaction chamber which is at least in part vertical or inclined for a vapor residence time in the range of about 0.5 to about 2.5 seconds at a reaction chamber outlet temperature of about 900 to about 1,300°F. and under a total pressure of about 15 to about 35 pounds per square inch absolute sufficient for causing a conversion per pass in the range of about 60% to about 90%, while producing at least about 6% coke by weight based on fresh feed and laying down coke on the catalyst in amounts in the range of about 0.3 to about 3% by weight; III. abruptly separating catalyst from product vapors at the downstream end of said elongated reaction chamber, discharging the catalyst thus separated into a catalyst collection chamber, and preventing at least about 80% by volume of the total feed and product vapors which have passed through said elongated reaction chamber from having further contact with the thus separated catalyst in said catalyst collection chamber; IV. stripping said separated catalyst; V. regenerating said catalyst with oxygen-containing combustion-supporting gas under conditions of time, temperature and atmosphere sufficient to reduce the carbon on the catalyst to about 0.25% by weight or less, while forming combustion product gases which comprise CO and/or CO2, and maintaining the CO:CO2 molar ratio of those combustion product gases formed from the burning of at least the major portion of the coke at a level of at least about 0.25 while such gases are in heat exchange contact with the catalyst; and VI. recycling the regenerated catalyst to the reactor at a temperature of at least about 1,275°F. for contact with fresh feed.