Process and facility for making coke suitable for metallurgical purposes

• US 4,551,232 A
• Filed: 02/09/1983
• Issued: 11/05/1985
• Est. Priority Date: 02/09/1983
• Status: Expired due to Term

• Current Assignee: Intevep, S.A. (PDVSA Gas SA)
• Original Assignee: Intevep, S.A. (PDVSA Gas SA)
• Inventors: Calderon, Jose L., Betancourt, Humberto
• Primary Examiner(s): Dixon, Jr., William R.
• Assistant Examiner(s): Prezlock, Cynthia A.
• Application Number:
  US06/465,210
• Time in Patent Office: 1,000 Days
• Field of Search: 208/131, 208/92, 208/85, 208/251 R, 202/84, 202/209, 196/46, 196/105
• US Class Current: 208/92
• 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

Abstract

Process and facility for upgrading heavy hydrocarbonaceous materials for making coke suitable for metallurgical purposes comprises mixing the heavy hydrocarbonaceous materials with a diluent having a closely controlled boiling range and subjecting the oil diluent mixture to distillation and careful fractionation so as to maximize liquid yields in the coking step.

Claims

1. A process for the production of metallurgical coke from a heavy crude oil feedstock comprising:

(a) providing a crude oil feedstock inlet;

(b) feeding a crude oil feedstock to said crude oil inlet, said crude oil feedstock being characterized by the following composition and properties;

space="preserve" listing-type="tabular">______________________________________ Gravity, °

API 6-12 Viscosities;

KV at 180°

F., cst 400-2500 KV at 140°

F., cst 2000-20000 KV at 122°

F., cst 5000-40000 Metals Content;

Iron, wt ppm 15-25 Vanadium, wt ppm 300-500 Nickel, wt ppm 60-120 Asphaltenes, % wt 6-12 Salt Content as NaCl, Lbs/1000 BBls. 35-1000 Pour Point, °

F. 50-90 Sulfur, % wt 3.5-4.5 Water and Sediments, % Vol 0.2-10 ______________________________________

(c) mixing said crude oil feedstock with a diluent in an amount equal to about 10 to 50% by volume, said diluent being characterized by a gravity of between 20 to 65 API and a boiling point range of between 150°

F. and 800°

F.;

(d) feeding the crude oil and diluent mixture to an atmospheric distillation unit wherein said crude oil and diluent mixture is subjected to distillation whereby gas products, a 500°

F. minus liquid overheat hydrocarbon product and 500°

F. plus residuum are produced;

(e) feeding the atmospheric distillation residuum to a combination tower comprising a heat transfer portion and a fractionator portion wherein said distillation residuum is subjected to fractionation so as to produce a reduced coker feed;

(f) withdrawing said reduced coker feed from the fractionator portion of said combination tower and passing said reduced coker feed to a delayed coking drum wherein the coker feed decomposes leaving a mass of metallurgical coke;

(g) recycling the coker effluent from said delayed coking drum directly to the fractionator portion of said combination tower;

(h) contacting said atmospheric distillation residuum with said coker effluent in the fractionator portion of said combination tower so as to produce a reduced coker feed mixed with recycle;

(i) withdrawing said coker feed mixed with recycle from the fractionator portion of said combination tower and passing said coker feed mixed with recycle to a delayed coking drum wherein the coker feed mixed with recycle decomposes leaving a mass of metallurgical coke; and

(j) recycling the coker effluent from said delayed coking drum directly to the fractionator portion of said combination tower wherein said incoming atmospheric distillation residuum is contacted with the coker effluent.

2. A process according to claim 1 including subjecting said 500°

F. minus liquid overhead hydrocarbon product to further treatment whereby naphtha and off gases are separated out as overhead products and a diluent having a boiling point range of about between 150°

F. and 800°

F. is produced.

3. A process according to claim 1 wherein the diluent has a viscosity of about 0.5 to 10.5 KV at 100°

F., cst and of about 0.1 to 3.0 KV at 210°

F., cst.

4. A process according to claim 1 including subjecting said 500°

F. minus liquid overhead hydrocarbon product to further treatment whereby a diluent having a boiling point range of about 150°

F. to 800°

F., a specific gravity of about 20°

to 65°

API and a viscosity of about 0.5 to 10.5 KV at 100°

F., cst and of about 0.1 to 3.0 KV at 210°

F. is produced and recycling said diluent and mixing said diluent with the incoming crude oil feedstock so as to lower the viscosity and pour point of the heavy crude oil feedstock.

5. A process according to claim 1 including recycling said diluent and mixing said diluent with said incoming heavy crude oil at said crude oil inlet so as to lower the viscosity and pour point of the heavy crude oil feedstock and aid in the dehydration and desalting of the feedstock.

6. A process according to claim 3 including recycling said diluent and mixing said diluent with said incoming heavy crude oil at said crude oil inlet so as to lower the viscosity and pour point of the heavy crude oil feedstock and aid in the dehydration and desalting of the feedstock.

7. A process according to claim 1 including the steps of first dehydrating and thereafter desalting said crude oil and diluent mixture prior to atmospheric distillation so as to obtain a water content of about not more than 1 volume percent and a salt content of not more than about 5 PTB.

9. A process according to claim 3 including subjecting said 500°

F. minus liquid overhead hydrocarbon product to further treatment whereby naphtha and off gases are separated out as overhead products and a diluent having a boiling point of about between 150°

F. and 800°

F. is produced.

8. A process for the production of metallurgical coke from a heavy crude oil feedstock comprising:

(a) providing a crude oil feedstock inlet;

(b) feeding a crude oil feedstock to said crude oil inlet, said crude oil feedstock being characterized by the following composition and properties;

space="preserve" listing-type="tabular">______________________________________ Gravity, °

API 6-12 Viscosities;

KV at 180°

F., cst 400-2500 KV at 140°

F., cst 2000-20000 KV at 122°

F., cst 5000-40000 Metals Content;

Iron, wt ppm 15-25 Vanadium, wt ppm 300-500 Nickel, wt ppm 60-120 Asphaltenes, % wt 6-12 Salt Content as NaCl, Lbs/1000 BBls. 35-1000 Pour Point, °

F. 50-90 Sulfur, % wt 3.5-4.5 Water and Sediments, % Vol 0.2-10 ______________________________________

(c) mixing said crude oil feedstock with diluent in an amount equal to about 10 to 50% by volume, said diluent being characterized by a gravity of between 20 to 65 API and a boiling point range of between 150°

F. and 800°

F.;

(d) feeding the crude oil and diluent mixture to an atmospheric distillation unit wherein said crude oil and diluent mixture is subjected to distillation whereby gas products, a 500°

F. minus liquid overhead hydrocarbon product and a 700°

F. plus residuum are produced;

(e) feeding the atmospheric distillation residuum to a vacuum distillation unit wherein said atmospheric distillation residuum is subjected to vacuum distillation whereby gas and liquid hydrocarbon distillate products and a 900°

F. plus vacuum residuum are produced;

(f) feeding said vacuum residuum to a combination tower comprising a heat transfer portion and a fractionator portion wherein said vacuum residuum is subjected to fractionation so as to produce a reduced coker feed;

(g) withdrawing said reduced coker feed from the fractionator portion of said combination tower and passing said reduced coker feed to a delayed coking drum wherein the coker feed decomposes leaving a mass of metallurgical coke;

(h) recycling the coker effluent from said delayed coking drum directly to the fractionator portion of said combination tower;

(i) contacting said vacuum residuum with said coker effluent in the fractionator portion of said combination tower so as to produce a reduced coker feed mixed with recycle;

(j) withdrawing said coker feed mixed with recycle from the fractionator portion of said combination tower and passing said coker feed mixed with recycle to a delayed coking drum wherein the coker feed mixed with recycle decomposes leaving a mass of metallurgical coke; and

(k) recycling the overhead products from said delayed coking drum directly to the fractionator portion of said combination tower wherein said incoming vacuum residuum is contacted with the coker effluent.

10. A process according to claim 8 including passing said coker feed mixed with recycle through a furnace so as to heat said coker feed to a temperature of about 920°

F. prior to feeding said coker feed to said delayed coking drum.

11. A process according to claim 8 wherein the diluent has a viscosity of about 0.5 to 10.5 KV at 100°

F., cst and of about 0.1 to 3.0 KV at 210°

F., cst.

12. A process according to claim 8 including subjecting said 500°

F. minus liquid overhead hydrocarbon product to further treatment whereby a diluent having a boiling point range of about 150°

F. to 800°

F., a specific gravity of about 20°

to 65°

API and a viscosity of about 0.5 to 10.5 KV at 100°

F., cst and of about 0.1 to 3.0 KV at 210°

F. is produced and recycling said diluent and mixing said diluent with the incoming crude oil feedstock so as to lower the viscosity and pour point of the heavy crude oil feedstock.

13. A process according to claim 8 including the steps of first dehydrating and thereafter desalting said crude oil and diluent mixture prior to atmospheric distillation so as to obtain a water content of about not more than 1 volume percent and a salt content of not more than about 5 PTB.