Process for upgrading heavy crude oil production

• US 5,948,242 A
• Filed: 10/15/1997
• Issued: 09/07/1999
• Est. Priority Date: 10/15/1997
• Status: Expired due to Term

• Current Assignee: BriteWater International, Inc.
• Original Assignee: Unipure Corporation
• Inventors: Ohsol, Ernest O., Gillespie, Thomas E., Pinkerton, John W., Laity, Thomas H.
• Primary Examiner(s): Griffin, Walter D.
• Assistant Examiner(s): Nguyen, Tam M.
• Application Number:
  US08/950,482
• Time in Patent Office: 692 Days
• Field of Search: 208/187, 208/188, 208/181, 208/179, 210/707
• US Class Current: 208/181
• CPC Class Codes: C10G 21/003 Solvent de-asphalting
• CPC Class Codes: C10G 33/04 with chemical means
• CPC Class Codes: C10G 53/04 including at least one extraction step

Abstract

A process for upgrading heavy crude oil production is described which involves adding a diluent, or solvent, which is a light hydrocarbon to reduce the viscosity and specific gravity of the crude oil being processed. After dilution, the emulsions in the crude are broken and the separation of the crude into the components follows, aided by a second injection of diluent. This upgrades the crude and enhances the amount recovered for processing at a refinery. A high asphalt content of a heavy crude can also be tolerated in the practice of this invention resulting in environmentally-benign solids and water exiting a process which due to the modularization of equipment can be practiced at the well-head itself.

Claims

1. A process for upgrading heavy, high viscosity, crude oil produced as a crude oil/water emulsion comprising the steps of:

adding a sufficient amount of a light hydrocarbon diluent having a boiling point of from about 10°

to about 180°

F. to said crude oil/water emulsion to form a mixture having a viscosity of less than about 50 cp;

heating and pressurizing said mixture to suitable conditions for breaking said crude-oil/water emulsion contained in said mixture by flashing;

breaking the crude oil/water emulsion and forming a vapor effluent and a liquid effluent by flashing said mixture to a sufficiently low pressure to vaporize at least about 5 percent by volume of said mixture;

separating crude oil from said liquid effluent; and

recovering said separated crude oil.

2. The process of claim 1 further comprising the step of removing gross solids from said crude oil/water emulsion prior to the flashing step and said separating step includes introducing a stream of additional hydrocarbon diluent to enhance the removal of asphaltic material from the crude oil.

3. The process of claim 1 wherein the amount of hydrocarbon diluent is from about 10 to about 35 percent by volume of the oil in the crude oil/water emulsion.

4. The process of claim 1 wherein the hydrocarbon diluent is selected from the group consisting of C₃ to C₇ paraffinic or naphthenic hydrocarbons C₆ to C₈ aromatic hydrocarbons, casinghead gas condensate, light aromatic distillate and mixtures thereof.

5. The process of claim 1 wherein the hydrocarbon diluent is a mixture of more than one light hydrocarbon boiling at a temperature of from about 10°

to about 180°

F.

6. A process for upgrading a heavy, high viscosity, crude oil/water emulsion containing water, solids, and impurities comprising heavy metals, asphaltic, asphaltenic and resinous materials, which process comprises the steps of:

removing gross solids from said crude-oil/water emulsion;

adding a light hydrocarbon diluent to the crude oil emulsion to form a mixture containing said crude-oil/water emulsion and said diluent;

pressurizing and heating said mixture;

flashing said heated mixture under such conditions to vaporize a sufficient amount of said mixture to break the crude oil emulsion and to form a vapor effluent containing said diluent, water, crude oil and some entrained solids and a liquid effluent containing said diluent, water, crude oil and solids;

separating said crude oil and asphaltic and alphaltene materials in said liquid effluent from water, solids and impurities,

adding additional diluent to the liquid effluent after the flashing step, using 200 to 800 volume percent based on the separated oil content, selecting the diluent from the group of C₄ through C₇ paraffinic or naphthanic hydrocarbons at a moderate temperature of 60°

to 100°

F. to obtain a continuous single phase oil-diluent solution;

gently warming the oil-diluent solution to a temperature within about 5°

F. to about 25°

F. of the critical temperature of the diluent causing a substantial part of the asphaltic or asphaltenic content of the crude oil to precipitate, causing the asphaltic solid or semi-solid material to settle from the lighter oil-diluent solution;

separating the diluent from the oil for recycling; and

recovering the crude oil product.

7. The process of claim 6 wherein said diluent is normal butane or isobutane.

8. The process of claim 6 wherein said diluent is pentane.

9. The process of claim 6 wherein said diluent is heptane.

10. The process of claim 6 wherein said diluent is a mixture of C₃ -C₅ hydrocarbons.

11. The process of claim 6 wherein said diluent is a C₅ -C₆ -C₇ blend.

12. The process of claim 6 which includes the step of recovering the diluent in a plurality of stages, using progressively lower pressures and supplying heat to vaporize the diluent.

13. The process of claim 6 further comprising the steps of steam stripping the diluent from the oil, condensing the vapors and decanting the condensed water from the recovered diluent.

14. The process of claim 6 wherein said additional diluent is introduced in a continuous countercurrent contacting device, near an asphaltic removal end and diluent-oil solution is removed at an opposite end.

15. The process of claim 14 wherein a temperature gradient is maintained within said contacting device with a higher temperature at the diluent-oil discharge end by suitable heat transfer means.

16. The process of claim 14 wherein said contacting device is a Rotating Disc Contactor.

17. The process of claim 14 which includes the step of recovering diluent from the separated asphaltic material.

18. The process of claim 17 further comprising the step of subjecting the separated asphaltic material, while still containing some diluent to a countercurrent washing with water containing a chelating agent for removal of heavy metals from the asphaltic material.

19. The process of claim 18 in which the chelating agent is EDTA or one of its sodium salts.

20. The process of claim 18 in which the chelating agent is nitrilotrisacetic acid.

21. The process of claim 18 in which the chelating agent is a glycolic acid.