Process for conversion of residue employing de-asphalting and delayed coking

• US 10,584,290 B2
• Filed: 03/06/2018
• Issued: 03/10/2020
• Est. Priority Date: 08/17/2017
• Status: Active Grant

• Current Assignee: Indian Oil Corporation Limited (Government of India)
• Original Assignee: Indian Oil Corporation Limited (Government of India)
• Inventors: Pradeep, Ponoly Ramachandran, Das, Satyen Kumar, Prasad, Terapalli Hari Venkata Devi, Kottakuna, Arjun Kumar, Bhattacharyya, Debasis, Mazumdar, Sanjiv Kumar, Ramakumar, Sankara Sri Venkata
• Primary Examiner(s): Boyer, Randy
• Assistant Examiner(s): Valencia, Juan C
• Application Number:
  US15/913,401
• Publication Number:
  US 20190055481A1
• Time in Patent Office: 735 Days
• 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 57/08 Non-mechanical pretreatment of the charge C10L9/00 takes precedence, e.g. desulfurization
• CPC Class Codes: C10G 21/003 Solvent de-asphalting
• CPC Class Codes: C10G 2300/1077 Vacuum residues
• CPC Class Codes: C10G 2300/206 Asphaltenes
• CPC Class Codes: C10G 55/04 including at least one thermal cracking step
• CPC Class Codes: C10G 9/005 Coking (in order to produce liquid products mainly)

Abstract

The present invention relates to resid processing, particularly related to conversion of resid material with maximum recovery of lighter hydrocarbons. The invented process utilizes a novel scheme for integration of solvent de-asphalting and delayed coking processes to maximize the residue conversion to valuable products, with cleaner quality of middle distillates and fuel oil products, in comparison with other integrated solvent de-asphalting and delayed coking schemes. This process also has an additional flexibility to vary the recycle quantity, without impacting fractionator operation of the delayed coking section, which further enhances the product recovery and achieves maximum conversion of the resid feedstock, with minimum impact on liquid product properties.

Claims

1. An integrated coking and solvent de-asphalting process, the process comprising:

(a) introducing a feedstock [1] near to bottom of a fractionator column [2] to obtain a mixed feed [3] drawn out from the bottom of the fractionator column, wherein the mixed feed [3] comprises the feedstock [1] and an internal recycle stream in the range from 5 to 80 wt % of the feedstock;

(b) contacting the mixed feed [3] with a solvent [5] in a extractor [4] to obtain a pitch stream [6] containing asphaltenic fraction and predominantly a paraffinic stream [10] containing a de-asphalted oil and the solvent;

(c) passing the pitch stream [6] to a pitch solvent stripper [7] to obtain a residual pitch stream [8] and the solvent;

(d) heating the residual pitch stream [8] in a furnace [16] to a coking temperature to obtain a hot pitch stream [17];

(e) transferring the hot pitch stream [17] to one of a plurality of coke drums [18, 19] where it undergoes thermal cracking reaction to obtain hydrocarbon vapours [20] and coke; and

(f) passing the hydrocarbon vapours [20] to the fractionator column [2] to obtain product fraction.

2. The process as claimed in claim 1, wherein the solvent to the mixed feed ratio in step (b) is in the range of 2:

1 to 50;

1.

3. The process as claimed in claim 1, wherein the paraffinic stream [10] is transferred to a solvent separator [11] to obtain the solvent and the de-asphalted oil [12].

4. The process as claimed in claim 1, wherein the paraffinic stream [10] further comprises a lighter paraffinic fraction of the internal recycle stream.

5. The process as claimed in claim 3, wherein the solvent is recovered from the de-asphalted oil [12] in an oil solvent stripper [13] to obtain the solvent and a residual de-asphalted oil [14].

6. The process as claimed in claim 5, wherein the solvent recovered from the pitch solvent stripper [7], the solvent separator [11] and the oil solvent stripper [13] is recycled to the extractor [4].

7. The process as claimed in claim 1, wherein the solvent is selected from the group comprising of hydrocarbons having 3 to 7 carbon atoms and mixtures thereof.

8. The process as claimed in claim 1, wherein the extractor [4] is operated at a temperature in the range of 55 to 300°

C.

9. The process as claimed in claim 1, wherein the extractor [4] is operated at a pressure in the range of 1 to 60 kg/cm² (g).

10. The process as claimed in claim 1, wherein the coke drums [18, 19] are operated at a temperature in the range of 470 to 520°

C.

11. The process as claimed in claim 1, wherein the coke drums [18, 19] are operated at a pressure in the range of 0.5 to 5 Kg/cm² (g).

12. The process as claimed in claim 1, wherein residence time of the hot pitch stream [17] in the coke drums [18, 19] is in the range of 10 to 26 hours.

13. The process as claimed in claim 1, wherein the feedstock [1] has conradson carbon residue content in the range of 4 to 30 wt % and density in the range of 0.95 to 1.08 g/cc.

14. The process as claimed in claim 1, wherein the feedstock [1] is selected from vacuum residue, atmospheric residue, shale oil, coal tar, clarified oil, residual oil, heavy waxy distillate, foots oil, slop oil or blend of hydrocarbons.

15. The process as claimed in claim 1, wherein the product fraction is offgas selected from the group consisting of LPG and naphtha [21], Kerosene [22], Light coker gas oil [23], Heavy coker gas oil [24] and Coker fuel oil [25].