Conversion of asphaltene-containing charge stocks and product separation process

Claim 2

A process for separating a mixture of a hydrocarbon-selective solvent comprising a light hydrocarbon having from about 3 to about 7 carbon atoms per molecule and deasphalted oil which comprises the sequential steps of: (a) introducing said mixture into a first separation zone, at superatmospheric pressure and a first temperature above the critical temperature of said solvent, to provide (i) a first solvent-rich vaporous phase, and, (ii) a first solvent-lean liquid phase; (b) introducing said first liquid phase into a second separation zone, at substantially the same pressure and a higher second temperature to provide (i) a second solvent-rich vaporous phase and, (ii) a second solvent-lean liquid phase; (c) introducing said first and second vaporous phases into a third separation zone, at a lower pressure and lower third temperature, (i) to recover a solvent concentrate and, (ii) to provide a solvent-lean vaporous phase; (d) distilling said solvent-lean vaporous phase to remove hydrocarbons boiling below the boiling point of said solvent and to recover additional solvent concentrate; and, (e) stripping solvent from said second liquid phase to recover substantially solvent-free deasphalted oil.

Claim 3

The process of claim 1 further characterized in that said first temperature is in the range of about 200° F to about 540° F.

Claim 4

The process of claim 1 further characterized in that said solvent is a mixture of normal butane and isopentane.

Claim 5

The process of claim 1 further characterized in that said solvent is a mixture of propane and normal butane.

Claim 6

The process of claim 1 further characterized in that said solvent is isopentane.

Claim 7

The process of claim 3 further characterized in that said first temperature is in the range of about 200° F. to about 410° F.

Claim 8

A process for the conversion of an asphaltene-containing, hydrocarbonaceous black oil, and the recovery of deasphalted oil therefrom, which comprises the sequential steps of: (a) reacting said black oil and hydrogen, in admixture with asphaltenes and a metallic sulfide selected from the sulfides of the iron-group metals and the metals from Groups V-B and VI-B, in a reaction zone at conversion conditions selected to convert insoluble asphaltic material into lower-boiling hydrocarbons; (b) separating the resulting reaction product effluent, in a first separation zone, to provide (i) a hydrogen-rich first vaporous phase and, (ii) a first liquid phase, containing metallic sulfides and unreacted asphaltenes, and recycling at least a portion of said first vaporous phase to combine with said black oil; (c) separating said first liquid phase, in a second separation zone, at a lower temperature and pressure to provide (i) a second vaporous phase, containing normally gaseous hydrocarbons, and, (ii) a second liquid phase; (d) deasphalting said second liquid phase with a hydrocarbon-selective solvent comprising a light hydrocarbon having from about 3 to about 7 carbon atoms per molecule in a solvent extraction zone to provide (i) a solvent-rich third liquid phase, containing deasphalted oil, and, (ii) a solvent-lean mixture of unreacted asphaltenes and metallic sulfides; (e) separsting said solvent-lean mixture, in a third separation zone, at substantially the same temperature and a lower pressure to provide (i) a solvent concentrated third vaporous phase and, (ii) a substantially solvent-free asphaltene/metallic sulfide mixture, and recycling at least a portion of said mixture to said reaction zone; (f) separating said solvent concentrate and said solvent-rich third liquid phase, in a fourth separation zone, at superatmospheric pressure and a first temperature above the critical temperature of said solvent, to provide (i) a solvent-rich fourth vaporous phase and, (ii) a solvent-lean fourth liquid phase; (g) separating said fourth liquid phase, in a fifth separation zone at substantially the same pressure and a higher second temperature to provide a solvent-rich fifth vaporous phase and, a solvent-lean fifth liquid phase containing deasphalted oil; (h) introducing said fourth and fifth vaporous phases into a sixth separation zone, at a lower third temperature and a lower pressure, (i) to recover a substantially pure first solvent concentrate and, (ii) to provide a solvent-lean sixth vaporous phase; (i) distilling said solvent-lean sixth vaporous phase to remove hydrocarbons boiling below the boiling point of said solvent and to recover an additional second solvent concentrate; and, (j) stripping solvent from said fifth liquid phase to recover substantially solvent-free deasphalted oil.

Claim 9

A process for the conversion of an asphaltene-containing, hydrocarbonaceous black oil, and the recovery of deasphalted oil therefrom, which comprises the sequential steps of: (a) reacting said black oil and hydrogen, in admixture with asphaltenes and a metallic sulfide selected from the sulfides of the iron-group metals and the metals from Groups V-B and VI-B, in a reaction zone at conversion conditions selected to convert insoluble asphaltic material into lower-boiling hydrocarbons; (b) separating the resulting reaction product effluent, in a first separation zone, to provide (i) a hydrogen-rich first vaporous phase and, (ii) a first liquid phase, containing metallic sulfides and unreacted asphaltenes, and recycling at least a portion of said first vaporous phase to combine with said black oil; (c) separating said first liquid phase, in a second separation zone, at a lower temperature and pressure to provide (i) a second vaporous phase, containing normally gaseous hydrocarbons, and, (ii) a second liquid phase; (d) deasphalting said second liquid phase with a hydrocarbon-selective solvent comprising a light hydrocarbon having from about 3 to about 7 carbon atoms per molecule in a solvent extraction zone to provide (i) a solvent-rich third liquid phase, containing deasphalted oil, and, (ii) a solvent-lean mixture of unreacted asphaltenes and metallic sulfides; (e) separsting said solvent-lean mixture, in a third separation zone, at substantially the same temperature and a lower pressure to provide (i) a solvent concentrated third vaporous phase and, (ii) a substantially solvent-free asphaltene/metallic sulfide mixture, and recycling at least a portion of said mixture to said reaction zone; (f) separating said solvent concentrate and said solvent-rich third liquid phase, in a fourth separation zone, at superatmospheric pressure and a first temperature above the critical temperature of said solvent, to provide (i) a solvent-rich fourth vaporous phase and, (ii) a solvent-lean fourth liquid phase; (g) separating said fourth liquid phase, in a fifth separation zone at substantially the same pressure and a higher second temperature to provide a solvent-rich fifth vaporous phase and, a solvent-lean fifth liquid phase containing deasphalted oil; (h) introducing said fourth and fifth vaporous phases into a sixth separation zone, at a lower third temperature and a lower pressure, (i) to recover a substantially pure first solvent concentrate and, (ii) to provide a solvent-lean sixth vaporous phase; (i) distilling said solvent-lean sixth vaporous phase to remove hydrocarbons boiling below the boiling point of said solvent and to recover an additional second solvent concentrate; and, (j) stripping solvent from said fifth liquid phase to recover substantially solvent-free deasphalted oil.

Claim 10

The process of claim 7 further characterized in that said first and second solvent concentrates are introduced into said solvent extraction zone.

Claim 11

The process of claim 7 further characterized in that said first vaporous phase is separated, at substantially the same pressure and a temperature in the range of about 60° F. to about 140° F., to remove normally vaporous hydrocarbons and to increase the hydrogen concentration prior to recycling a portion thereof to combine with said black oil.