Method for producing high VCM coke

• US 9,062,256 B2
• Filed: 05/11/2012
• Issued: 06/23/2015
• Est. Priority Date: 05/13/2011
• Status: Active Grant

• Current Assignee: Catalytic Distillation Technologies (Lummus Technology LLC)
• Original Assignee: Catalytic Distillation Technologies (Lummus Technology LLC)
• Inventors: Faegh, Ahmad, Collins, John C., Manral, Virendra, Reisen, Gary
• Primary Examiner(s): Robinson, Renee E
• Application Number:
  US13/469,593
• Publication Number:
  US 20120285862A1
• Time in Patent Office: 1,138 Days
• Field of Search: 208/100, 208/131
• US Class Current: 1/1
• CPC Class Codes: C10B 27/06 Conduit details, e.g. valves
• CPC Class Codes: C10B 39/06 in the oven
• CPC Class Codes: C10B 41/00 Safety devices, e.g. signalling or controlling devices for use in the discharge of coke
• CPC Class Codes: C10B 41/08 for the withdrawal of the distillation gases
• 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 57/045 containing mineral oils, bitumen, tar or the like or mixtures thereof
• CPC Class Codes: C10G 2300/107 Atmospheric residues having a boiling point of at least about 538 °C
• CPC Class Codes: C10G 2300/1077 Vacuum residues
• CPC Class Codes: C10G 2300/4006 Temperature
• CPC Class Codes: C10G 2300/4081 Recycling aspects
• CPC Class Codes: C10G 2400/06 Gasoil
• CPC Class Codes: C10G 9/005 Coking (in order to produce liquid products mainly)
• CPC Class Codes: C10L 2290/02 Combustion or pyrolysis
• CPC Class Codes: C10L 2290/06 Heat exchange, direct or indirect
• CPC Class Codes: C10L 2290/58 Control or regulation of the fuel preparation of upgrading process
• CPC Class Codes: C10L 5/04 Raw material of mineral origin to be used; Pretreatment thereof pretreatment of fuels of non-mineral origin C10L5/40

Abstract

A process and apparatus for improving the production of coke having a high volatile combustible material content are disclosed. The process may include, for example: heating a coker feedstock to a coking temperature to produce a heated coker feedstock; contacting the heated coker feedstock with a quench medium to reduce a temperature of the heated coker feedstock and produce a quenched feedstock; feeding the quenched feedstock to a coking drum; subjecting the quenched feedstock to thermal cracking in the coking drum to (a) crack a portion of the quenched feedstock to produce a cracked vapor product, and (b) produce a coke product having a volatile combustible material (VCM) concentration in the range from about 13% to about 50% by weight, as measured by ASTM D3175.

Claims

1. A process for producing a coke fuel, the process comprising:

heating a coker feedstock to a coking temperature to produce a heated coker feedstock;

transferring the heated coker feedstock to a coking drum, wherein during transfer the heated coker feedstock undergoes thermal cracking;

contacting the heated coker feedstock with a quench medium proximate an inlet of the coking drum to reduce a temperature of the heated coker feedstock and produce a quenched feedstock;

feeding the quenched feedstock to the coking drum;

subjecting the quenched feedstock to thermal cracking in the coking drum to (a) crack a portion of the quenched feedstock to produce a cracked vapor product, and (b) produce a coke product having a volatile combustible material (VCM) concentration in the range from about 13% to about 50% by weight, as measured by ASTM D3175.

2. The process of claim 1, wherein the VCM concentration is in the range from about 16% to about 22% by weight.

3. The process of claim 1, further comprising:

recovering the cracked vapor product from an outlet of the coking drum; and

controlling a temperature of the recovered cracked vapor product proximate the outlet of the coking drum by adjusting at least one of a feed rate and a temperature of the quench medium.

4. The process of claim 3, wherein the controlling maintains the temperature proximate the outlet within the range from 750°

F. to about 850°

F.

5. The process of claim 4, wherein the controlling maintains the temperature proximate the outlet within the range from 775°

F. to about 800°

F.

6. The process of claim 3, further comprising fractionating the recovered cracked vapor product to recover two or more hydrocarbon fractions.

7. The process of claim 6, wherein the two or more hydrocarbon fractions include at least one of a wash oil fraction, a quench oil fraction, a coker heavy gas oil fraction, a coker light gas oil fraction, and a naphtha fraction.

8. The process of claim 6, further comprising using at least a portion of one or more of the wash oil fraction, the quench oil fraction, the coker heavy gas oil fraction, the coker light gas oil fraction, and combinations thereof as the quench medium.

9. The process of claim 1, wherein the coking temperature is in the range from about 900°

F. to about 1100°

F.

10. The process of claim 1, wherein the contacting step decreases a temperature of the heated coker feedstock by at least 10°

F.

11. The process of claim 1, wherein the contacting step decreases a temperature of the heated coker feedstock by at least 50°

F.

12. The process of claim 1, wherein the contacting step decreases a temperature of the heated coker feedstock by at least 100°

F.

13. The process of claim 1, wherein the quench medium comprises at least one of coker heavy gas oil, coker light gas oil, coker feedstock, hydrocarbon mixtures having a boiling point in the range from about 500°

F. to about 950°

F., and combinations thereof.

14. The process of claim 1, wherein the contacting the heated coker feedstock with a quench medium is performed immediately upstream of a diverter valve for directing the quenched feedstock to the coking drum and away from a second coking drum.

15. The process of claim 1, wherein the contacting the heated coker feedstock with a quench medium is performed downstream of a diverter valve for directing the quenched feedstock to the coking drum and away from a second coking drum.