Petroleum upgrading process

• US 9,382,485 B2
• Filed: 09/14/2010
• Issued: 07/05/2016
• Est. Priority Date: 09/14/2010
• Status: Active Grant

• Current Assignee: Saudi Arabian Oil Company (Government of Saudi Arabia)
• Original Assignee: Saudi Arabian Oil Company (Government of Saudi Arabia)
• Inventors: Al-Dossary, Mohammed Rashid, Choi, Ki-Hyouk, Punetha, Ashok K., Ghamdi, Sameer Ali
• Primary Examiner(s): Boyer, Randy
• Application Number:
  US12/881,807
• Publication Number:
  US 20120061294A1
• Time in Patent Office: 2,121 Days
• Field of Search: None
• US Class Current: 1/1
• CPC Class Codes: C10G 2300/1033 Oil well production fluids
• CPC Class Codes: C10G 2300/107 Atmospheric residues having a boiling point of at least about 538 °C
• CPC Class Codes: C10G 2300/1074 Vacuum distillates
• CPC Class Codes: C10G 2300/1077 Vacuum residues
• CPC Class Codes: C10G 2300/202 Heteroatoms content, i.e. S, N, O, P
• CPC Class Codes: C10G 2300/205 Metal content
• CPC Class Codes: C10G 2300/4006 Temperature
• CPC Class Codes: C10G 2300/4012 Pressure
• CPC Class Codes: C10G 2300/805 Water
• CPC Class Codes: C10G 47/32 in the presence of hydrogen-generating compounds
• CPC Class Codes: C10G 65/12 including cracking steps and other hydrotreatment steps

Abstract

A method and apparatus for upgrading a petroleum feedstock with supercritical water are provided. The method includes the steps of: (1) heating and pressurizing a petroleum feedstock; (2) heating and pressurizing a water feed to above the supercritical point of water; (3) combining the heated and pressurized petroleum feedstock and the heated and pressurized water feed to produce a combined feed; (4) supplying the combined feed to a hydrothermal reactor to produce a first product stream; (5) supplying the first product stream to a post-treatment process unit to produce a second product stream; and (6) separating the second product stream into a treated and upgraded petroleum stream and a water stream.

Claims

1. A method for upgrading of petroleum feedstock, comprising the steps of:

providing a pressurized and heated petroleum feedstock, wherein said petroleum feedstock is maintained at a temperature of between about 10°

C. and 250°

C. and a pressure of at least about 22.06 MPa;

providing a pressurized and heated water feed, wherein said water feed is maintained at a temperature of between about 250°

C. and 650°

C. and a pressure of at least about 22.06 MPa;

combining said pressurized and heated petroleum feedstock and said pressurized and heated water feed to form a combined petroleum and water feed stream;

supplying the combined petroleum and water feed stream to a hydrothermal reactor to produce a first product stream, wherein said reactor is maintained at a temperature of between 380°

C. and 550°

C., the combined petroleum and water feed stream being maintained within the hydrothermal reactor for a residence time operable to crack hydrocarbons present in the combined petroleum and water feed stream;

transferring the first product stream to a post-treatment device to produce a second product stream, wherein said post-treatment device is maintained at a temperature of between about 100°

C. and 300°

C., wherein water present in the post-treatment device is maintained in a liquid phase;

collecting the second product stream from the post treatment device, the second product stream comprising hydrocarbon product and water, wherein the hydrocarbon product has a reduced sulfur content relative to the petroleum feedstock.

2. The method of claim 1 further comprising the step of maintaining the hydrothermal reactor at a temperature and pressure such that the water is in a supercritical state.

3. The method of claim 1 wherein the post-treatment device further comprises a post-treatment catalyst.

4. The method of claim 3 wherein the post-treatment catalyst includes an active species selected from the group consisting of the Group VIB, and Group VIIIB elements.

5. The method of claim 3 wherein the post-treatment catalyst is a desulfurization catalyst.

6. The method of claim 3 further comprising the step of maintaining the post-treatment device at a temperature and pressure such that water is in a sub-critical state.

7. The method of claim 3 further comprising the step of maintaining the post-treatment device at a temperature of between about 120 and 200°

C.

8. The method of claim 1 further comprising supplying the combined petroleum and water feed stream to the hydrothermal reactor through a transport line, wherein the residence time of the combined petroleum and water feed stream in the transport line is between about 0.1 seconds and 10 minutes.

9. The method of claim 1 wherein the upgrading of the petroleum feedstock in the hydrothermal reactor is in the absence of external hydrogen gas.

10. The method of claim 1 wherein the upgrading of the petroleum feedstock in the hydrothermal reactor is in the absence of external catalyst.

11. The method of claim 1 wherein the ratio of petroleum feed to water feed is between about 2:

1 to 1;

2.

12. The method of claim 1 wherein the residence time of the combined petroleum and water stream in the hydrothermal reactor is between 1 second and 120 minutes.

13. The method of claim 1 wherein the residence time of the combined petroleum and water stream in the hydrothermal reactor is between 2 minutes and 30 minutes.

14. The method of claim 1 wherein hydrogen is not supplied to the post-treatment device.

15. A method for upgrading petroleum, the method comprising the steps of:

(1) providing a heated and pressurized a petroleum feedstock;

(2) providing a water feed, wherein said water feed is in the supercritical state;

(3) combining the heated and pressurized petroleum feedstock and the supercritical water feed to produce a combined petroleum and supercritical water feed;

(4) supplying the petroleum and supercritical water combined feed to a hydrothermal reactor to produce a first product stream;

(5) supplying the first product stream to a post-treatment device to produce a second product stream, wherein said post-treatment device is maintained at a temperature of between about 100°

C. and 300°

C., wherein water present in the post-treatment device is maintained in a liquid phase; and

(6) separating the second product stream into an upgraded petroleum stream and a water stream, wherein said upgraded petroleum stream has a reduced sulfur content relative to the petroleum feedstock.

16. The method of claim 15 wherein the hydrothermal reactor is maintained at a temperature and pressure sufficient to maintain the water in its supercritical state.

17. The method of claim 15 wherein the contact time of the petroleum feedstock and the supercritical water is between 0.1 seconds and 1 minute.

18. The method of claim 15 wherein the contact time of the petroleum feedstock and the supercritical water is between 0.5 seconds and 10 seconds.

19. The method of claim 15 wherein the hydrothermal reactor is maintained at a temperature greater than about 400°

.

20. The method of claim 15 wherein hydrogen is not supplied to the post-treatment device.

21. A method for upgrading a petroleum feedstock, comprising the steps of:

providing a petroleum feedstock and water mixture to a reaction zone, wherein said reaction zone is maintained at a temperature and pressure that is greater than about the supercritical point of water, and said reaction zone does not include externally supplied hydrogen;

allowing the petroleum feed and the supercritical water to contact in the reaction zone for a first reaction time to produce a first reactor product stream, wherein the reaction time is operable to upgrade at least a portion of the petroleum feedstock;

supplying the first reactor product stream to a second reactor and contacting the first reactor product stream with a hydrocarbon upgrading catalyst to produce a second reactor product stream that includes upgraded hydrocarbons, wherein the second reactor is maintained at a temperature below 300°

C. and pressure that is less than the critical pressure of water, wherein water present in the post-treatment device is maintained in a liquid phase, and wherein the reaction product and catalyst are contacted for a second reaction time that is sufficient to remove at least a portion of sulfur containing compounds present reaction product; and

separating the second reactor product stream into an upgraded hydrocarbon product stream and a water stream.