Coking of gas oil from slurry hydrocracking

• US 9,109,165 B2
• Filed: 11/15/2008
• Issued: 08/18/2015
• Est. Priority Date: 11/15/2008
• Status: Active Grant

• Current Assignee: UOP Llc (Honeywell International Inc.)
• Original Assignee: UOP Llc (Honeywell International Inc.)
• Inventors: Zimmerman, Paul R., Clary, Dennis M.
• Primary Examiner(s): Boyer, Randy
• Application Number:
  US12/271,880
• Publication Number:
  US 20100122931A1
• Time in Patent Office: 2,467 Days
• Field of Search: 208/50
• US Class Current: 1/1
• CPC Class Codes: C10B 55/00 Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material cracking oils C10G
• CPC Class Codes: C10B 55/10 according to the "fluidised bed" technique
• CPC Class Codes: C10B 57/045 containing mineral oils, bitumen, tar or the like or mixtures thereof
• CPC Class Codes: C10G 47/00 Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions C10G15/00 takes precedence; destructive hydrogenation of non-melting solid carbonaceous or similar materials C10G1/06
• CPC Class Codes: C10G 69/06 including at least one step of thermal cracking in the absence of hydrogen
• CPC Class Codes: C10G 9/005 Coking (in order to produce liquid products mainly)

Abstract

Integrated slurry hydrocracking (SHC) and coking methods for making slurry hydrocracking (SHC) distillates are disclosed. Representative methods involve passing a slurry comprising a vacuum column resid, a liquid coker product, and a solid particulate through an SHC reaction zone in the presence of hydrogen to obtain the SHC distillate. Atmospheric distillation in the SHC product recovery section yields a combined SHC gas oil/SHC pitch stream that is sent to coking to generate the liquid coker product. In a representative embodiment, vacuum distillation in the SHC product recovery is avoided, thereby eliminating equipment that is often most susceptible to fouling.

Claims

1. A method for making a distillate hydrocarbon component by integrating slurry hydrocracking (SHC) and coking, the method comprising:

(a) passing a slurry comprising a crude oil vacuum column residue, a liquid coker product obtained from a delayed coker or a fluidized coker, and a solid particulate through an SHC reaction zone in the presence of hydrogen to provide an SHC effluent,

(b) recovering said SHC distillate and a combination of an SHC gas oil and an SHC pitch from said SHC effluent,

(c) coking said combination of said SHC gas oil and said SHC pitch in a delayed coker or a fluidized coker to provide said liquid coker product and coke.

2. The method of claim 1, wherein the SHC distillate comprises less than about 20% by weight of hydrocarbons boiling at a temperature of greater than 343°

C. (650°

F.).

3. The method of claim 1, wherein the overall pitch conversion of the crude oil vacuum column residue is at least about 90%.

4. An integrated process for preparing a slurry hydrocracking (SHC) distillate, the process comprising:

(a) coking an SHC gas oil to obtain a liquid coker product and coke;

(b) passing a heavy hydrocarbon feedstock comprising vacuum column residue from a crude vacuum column and at least a portion of said liquid coker product through an SHC reaction zone in the presence of hydrogen to provide an SHC effluent; and

(c) recovering said SHC distillate and said SHC gas oil from said SHC effluent.

5. The process of claim 4, wherein said liquid coker product is obtained from a delayed coker or a fluidized coker.

6. The process of claim 4, wherein said liquid coker product comprises at least about 30% by weight of aromatics.

7. The process of claim 4, wherein the heavy hydrocarbon feedstock is present as a slurry, in combination with a solid particulate, in said SHC reaction zone.

8. The process of claim 7, wherein said solid particulate comprises a compound of a metal of Group IVB, Group VB, Group VIB, Group VIIB, or Group VIII.

9. The process of claim 4, wherein the overall pitch conversion of said heavy hydrocarbon feedstock is at least 90%.

10. An integrated process for preparing a slurry hydrocracking (SHC) distillate, the process comprising:

(a) coking an SHC gas oil to obtain a liquid coker product and coke;

(b) passing a heavy hydrocarbon feedstock comprising vacuum column residue and at least a portion of said liquid coker product through an SHC reaction zone in the presence of hydrogen to provide an SHC effluent; and

(c) recovering said SHC gas oil from an SHC effluent in an SHC atmospheric column;

wherein an SHC distillate is recovered in one or more distillate products comprising (i) a vapor fraction from flash separation of said SHC effluent in an SHC high pressure separator, (ii) one or more distilled fractions from said SHC atmospheric distillation column, or (iii) both (i) and (ii); and

said one or more distilled fractions from said atmospheric distillation column are selected from the group consisting of a naphtha product, a diesel product, or a mixture of thereof.

11. The process of claim 10, wherein said SHC gas oil is recovered in combination with an SHC pitch as a liquid bottoms product of said SHC atmospheric distillation column.

12. The process of claim 11, wherein said SHC gas oil has an initial boiling point of at least about 343°

C. (650°

F.).

13. The process of claim 10, further comprising hydrotreating a distillate feedstock comprising said one or more distillate products in a hydrotreating zone to obtain a hydrotreated distillate.

14. The process of claim 13, wherein said distillate feedstock further comprises, in addition to said SHC distillate, a straight-run distillate.

15. The process of claim 13, wherein said hydrotreated distillate has an API gravity of at least about 20°

.

16. The process of claim 10, wherein said SHC gas oil is recovered in combination with said SHC pitch as bottoms fraction from vacuum flash separation of a liquid bottoms product of an SHC atmospheric distillation column.

17. The process of claim 10, wherein said SHC gas oil has an initial boiling point of at least about 427°

C. (800°

F.).

18. The process of claim 10, wherein said SHC reaction zone is maintained at a temperature from about 343°

C. (650°

F.) to about 538°

C. (1000°

F.), a pressure from about 3.5 MPa (500 psig) to about 21 MPa (3000 psig), and a space velocity from about 0.1 to about 30 volumes of heavy hydrocarbon feedstock per hour per volume of said SHC zone.