Process for converting heavy petroleum fractions, comprising an ebullated bed hydroconversion step and a hydrotreatment step

• US 6,447,671 B1
• Filed: 03/24/2000
• Issued: 09/10/2002
• Est. Priority Date: 03/25/1999
• Status: Expired due to Term

• Current Assignee: Institut Francais Du Petrole (IFP Energies Nouvelles)
• Original Assignee: Institut Francais Du Petrole (IFP Energies Nouvelles)
• Inventors: Kressmann, Stéphane, Morel, Frédéric, Duplan, Jean-Luc
• Primary Examiner(s): Dang, Thuan D.
• Application Number:
  US09/535,167
• Time in Patent Office: 900 Days
• Field of Search: 208/84, 208/58, 208/210
• US Class Current: 208/89
• CPC Class Codes: C10G 65/04 including only refining steps
• CPC Class Codes: C10G 65/12 including cracking steps and other hydrotreatment steps

Abstract

The invention concerns a process for converting a hydrocarbon fraction with a sulphur content of at least 0.1% by weight, an initial boiling point of at least 340° C. and an end point of at least 440° C., characterized in that it comprises the following steps:

a) treating the hydrocarbon feed in a treatment section in the presence of hydrogen, said section comprising at least one three-phase reactor, containing at least one ebullated bed hydroconversion catalyst and operating in liquid and gas upflow mode;

b) sending at least a portion of the effluent from step a) to a section for eliminating catalyst particles contained in said effluent;

c) sending at least a portion of the effluent from step b) to a treatment section, treatment being carried out in the presence of hydrogen and optionally a hydrocarbon fraction from a fixed bed hydrotreatment step.

Claims

1. A process for converting a hydrocarbon feed containing at least one hydrocarbon fraction with a sulphur content of at least 0.1% by weight, an initial boiling point of at least 340°

C. and an end point of at least 440°

C., characterized in that it comprises the following steps;

a) treating said hydrocarbon feed in a section for treatment carried out in the presence of hydrogen, said section comprising at least one three-phrase reactor, containing at least one hydroconversion catalyst wherein a mineral support is at least partially amorphous, in an ebullated bed, operating in liquid and gas upflow mode, said reactor comprising at least one means for withdrawing catalyst from said reactor located close to the reactor bottom and at least one means for supplying fresh catalyst to said reactor located close to the top of said reactor;

b) sending at least one portion of the effluent from step a) to a section for eliminating catalyst particles containing in said effluent, said section comprising at least one means for eliminating said solid particles and at least one means for recovering an effluent containing fewer solid particles than the effluent from step a);

c) sending at least a portion of the effluent from step b) to a section for treatment carried out in the presence of hydrogen, said section comprising at least one reactor containing at least one fixed bed hydrotreatment catalyst wherein the mineral support is at least partially amorphous, under conditions enabling an effluent with a reduced sulphur content and a high middle distillate content to be obtained.

2. A process according to claim 1, in which the hydrocarbon feed is an atmospheric residue, a straight run vacuum residue, a vacuum residue from the conversion process, an oil deasphalted using a solvent, of propane, butane or pentane, an asphalt diluted by a hydrocarbon fraction of an LCO, an HCO, a DO, a VGO a slurry, or combinations thereof, the gas oil and vacuum gas oil obtained by straight run distillation and the various hydrocarbon fractions produced being capable of being recycled in mixtures in any proportions with the feeds cited above.

3. A process according to claim 1, in which a hydrocarbon fraction is added to the effluent from step b).

4. A process according to claim 1, in which at least a portion of the effluent obtained from step c) is sent to a distillation zone (step d) from which a gas fraction, a gasoline engine fuel fraction, a gas oil engine fuel fraction and a liquid fraction which is heavier than the gas oil fraction are recovered.

5. A process according to claim 4, in which the liquid fraction which is heavier than the gas oil fraction obtained from step d) is sent to a catalytic cracking section (step e) in which it is treated under conditions which produce a gas fraction, a gasoline fraction, a gas oil fraction and a slurry fraction.

6. A process according to claim 5, in which at least a portion of the gas oil fraction recovered in catalytic cracking step e) is recycled to step a) and/or step c).

7. A process according to claim 5, in which catalytic cracking step e) is carried out under conditions which produce a gasoline fraction at least a portion of which is sent to a fuel storage zone, a gas oil fraction at least a portion of which is sent to a gas oil storage zone and a slurry fraction at least a portion of which is sent to a heavy fuel storage zone.

8. A process according to claim 7, in which at least a portion of the gas oil fraction and/or the gasoline fraction obtained in catalytic cracking step e) is recycled to the inlet of the catalytic cracking section.

9. A process according to claim 5, in which at least a portion of the slurry fraction obtained in catalytic cracking step e) is recycled to the inlet of the catalytic cracking step.

10. A process according to claim 4, in which at least a portion of the liquid fraction which is heavier than the gas oil fraction obtained in step d) or f) is returned either to the hydroconversion of step a), or to the hydrotreatment step of c), or to each of these two sections.

11. A process according to claim 1, characterized in that it comprises a step a1) between step a) and step b) in which the product from step a) is split into a heavy liquid fraction which is sent to step b) for eliminating solid catalyst particles and into a lighter fraction which is recovered.

12. A process according to claim 11, in which the lighter liquid fraction which is recovered is sent to a distillation zone from which a gas fraction, a gasoline engine fuel, a gas oil engine fuel and a liquid fraction which is heavier than the gas oil fraction are recovered.

13. A process according to claim 11, in which the lighter liquid fraction which is recovered is sent to the distillation zone of step d).

14. A process according to claim 1, in which the step b comprises using at least two separation means in parallel one of which is used to carry out separation while the other is purged of retained fines.

15. A process according to claim 1, in which during step a) the treatment in the presence of hydrogen is carried out under an absolute pressure of 2.5 to 35 MPa, at a temperature of about 330°

C. to 550°

C. with an hourly space velocity of about 0.1 to 10 h<sup>−

1</sup> and the quantity of hydrogen mixed with the feed is about 50 to 5000 Nm³/m³.

16. A process according to claim 1, in which hydrotreatment step c) is carried out at an absolute pressure of about 2 to 35 MPa, at a temperature of about 300°

C. to 500°

C. with an hourly space velocity of about 0.1 to 5 h<sup>−

1</sup> and the quantity of hydrogen mixed with the feed is about 100 to 5000 Nm³/m³.

17. A process according to claim 4, in which at least a portion of the heavier liquid fraction of hydrotreated feed obtained in step d) is sent to a heavy fuel storage zone.

18. A process according to claim 4, in which at least a portion of the gasoline engine fuel fraction and the gas oil engine fuel fraction obtained from step d) are sent to respective fuel storage zones.

19. A process according to claim 2, in which a hydrocarbon fraction is added to the effluent from step b).

20. A process according to claim 5, in which at least a portion of the gas oil fraction recovered in catalytic cracking step e) is recycled to step a) and step c).

21. A process according to claim 1, wherein in step c) the whole of the effluent containing fewer solid particles from step b) is sent to a section for treatment.

22. A process according to claim 21, in which the hydrocarbon feed is an atmospheric residue, a straight run vacuum residue, a vacuum residue from the conversion process, an oil deasphalted using a solvent, of propane, butane or pentane, an asphalt diluted by a hydrocarbon fraction of an LCO, an HCO, a DO, a VGO a slurry, or combinations thereof, the gas oil and vacuum gas oil obtained by straight run distillation and the various hydrocarbon fractions produced being capable of being recycled in mixtures in any proportions with the feeds cited above.

23. A process according to claim 21, in which a hydrocarbon fraction is added to the effluent from step b).

24. A process according to claim 21, in which at least a portion of the effluent obtained from step c) is sent to a distillation zone (step d) from which a gas fraction, a gasoline engine fuel fraction, a gas oil engine fuel fraction and a liquid fraction which is heavier than the gas oil fraction are recovered.

25. A process according to claim 24, in which the liquid fraction which is heavier than the gas oil fraction obtained from step d) is sent to a catalytic cracking section (step e) in which it is treated under conditions which produce a gas fraction, a gasoline fraction, a gas oil fraction and a slurry fraction.

26. A process according to claim 25, in which at least a portion of the gas oil fraction recovered in catalytic cracking step e) is recycled to step a) and/or step c).

27. A process according to claim 24, in which catalytic cracking step e) is carried out under conditions which produce a gasoline fraction at least a portion of which is sent to a fuel storage zone, a gas oil fraction at least a portion of which is sent to a gas oil storage zone and a slurry fraction at least a portion of which is sent to a heavy fuel storage zone.

28. A process according to claim 27, in which at least a portion of the gas oil fraction and/or the gasoline fraction obtained in catlytic cracking step e) is recycled to the inlet of the catalytic cracking section.

29. A process according to claim 25, in which at least a portion of the slurry fraction obtained in catalytic cracking step e) is recycled to the inlet of the catalytic cracking step.

30. A process according to claim 24, in which at least a portion of the liquid fraction which is heavier than the gas oil fraction obtained in step d) or f) is returned either to the hydroconversion of step a), or to the hydrotreatment step of c), or to each of these two sections.

31. A process according to claim 21, in which the step b comprises using at least two separation means in parallel one of which is used to carry out separation while the other is purged of retained fines.

32. A process according to claim 21, in which during step a) the treatment in the presence of hydrogen is carried out under an absolute pressure of 2.5 to 35 MPa, at a temperature of about 300EC to 550EC with an hourly space velocity of about to 0.1 to 10 h⁻

1 and the quantity of hydrogen mixed with the feed is about 50 to 5000 Nm³/m³.

33. A process according to claim 21, in which hydrotreatment step c) is carried out at an absolute pressure of about 2 to 35 MPa, at a temperature of about 300EC to 500EC with an hourly space velocity of about 0.1 to 5 h⁻

1 and the quantity of hydrogen mixed with the feed is about 100 to 5000 Nm³/m³.

34. A process according to claim 24, in which at least a portion of the heavier liquid fraction of hydrotreated feed obtained in step d) is sent to a heavy fuel storage zone.

35. A process according to claim 24, in which at least a portion of the gasoline engine fuel fraction and the gas oil engine fuel fraction obtained from step d) are sent to respective fuel storage zones.

36. A process according to claim 22, in which a hydrocarbon fraction is added to the effluent from step b).

37. A process according to claim 25, in which at least a portion of the gas oil fraction recovered in catalytic cracking step e) is recycled to step a) and step c).

38. A process according to claim 11, in which the hydrocarbon feed is an atmospheric residue, a straight run vacuum residue, a vacuum residue from the conversion process, an oil deasphalted using a solvent, of propane, butane or pentane, an asphalt diluted by a hydrocarbon fraction of an LCO, an HCO, a DO, a VGO a slurry, or combinations thereof, the gas oil and vacuum gas oil obtained by straight run distillation and the various hydrocarbon fractions produced being capable of being recycled in mixtures in any proportions with the feeds cited above.

39. A process according to claim 11, in which a hydrocarbon fraction is added to the effluent from step b).

40. A process according to claim 11, in which at least a portion of the effluent obtained from step c) is sent to a distillation zone (step d) from which a gas fraction, a gasoline engine fuel fraction, a gas oil engine fuel fraction and a liquid fraction which is heavier than the gas oil fraction are recovered.

41. A process according to claim 40, in which the liquid fraction which is heavier than the gas oil fraction obtained from step d) is sent to a catalytic cracking section (step e) in which it is treated under conditions which produce a gas fraction, a gasoline fraction, a gas oil fraction and a slurry fraction.

42. A process according to claim 41, in which at least a portion of the gas oil fraction recovered in catalytic cracking step e) is recycled to step a) and/or step c).

43. A process according to claim 40, in which catalytic cracking step e) is carried out under conditions which produce a gasoline fraction at least a portion of which is sent to a fuel storage zone, a gas oil fraction at least a portion of which is sent to a gas oil storage zone and a slurry fraction at least a portion of which is sent to a heavy fuel storage zone.

44. A process according to claim 41, in which at least a portion of the gas oil fraction and/or the gasoline fraction obtained in catalytic cracking step e) is recycled to the inlet of the catalytic cracking section.

45. A process according to claim 41, in which at least a portion of the slurry fraction obtained in catalytic cracking step e) is recycled to the inlet of the catalytic cracking step.

46. A process according to claim 40, in which at least a portion of the liquid fraction which is heavier than the gas oil fraction obtained in step d) or f) is returned either to the hydroconversion of step a), or to the hydrotreatment step of c), or to each of these two selections.

47. A process according to claim 11, in which the step b comprises using at least two separation means in parallel one of which is used to carry out separation while the other is purged of retained fines.

48. A process according to claim 11, in which during step a) the treatment in the presence of hydrogen is carried out under an absolute pressure of 2.5 to 35 MPa, at a temperature of about 300EC to 550EC with an hourly space velocity of about to 0.1 to 10 h⁻

1 and the quantity of hydrogen mixed with the feed is about 50 to 5000 Nm³/m³.

49. A process according to claim 11, in which hydrotreatment step c) is carried out at an absolute pressure of about 2 to 35 MPa, at a temperature of about 300EC to 500EC with an hourly space velocity of about 0.1 to 5 h⁻

1 and the quantity of hydrogen mixed with the feed is about 100 to 5000 Nm³/m³.

50. A process according to claim 40, in which at least a portion of the heavier liquid fraction of hydrotreated feed obtained in step d) is sent to a heavy fuel storage zone.

51. A process according to claim 40, in which at least a portion of the gasoline engine fuel fraction and the gas oil engine fuel fraction obtained from step d) are sent to respective fuel storage zones.

52. A process according to claim 38, in which a hydrocarbon fraction is added to the effluent from step b).

53. A process according to claim 41, in which at least a portion of the gas oil fraction recovered in catalytic cracking step e) is recycled to step a) and step c).