Apparatus and systems for upgrading heavy oil using catalytic hydrocracking and thermal coking

• US 9,969,946 B2
• Filed: 08/26/2015
• Issued: 05/15/2018
• Est. Priority Date: 07/30/2012
• Status: Active Grant

• Current Assignee: Headwaters Heavy Oil, LLC (Seven Group Holdings Limited)
• Original Assignee: Headwaters Heavy Oil, LLC (Seven Group Holdings Limited)
• Inventors: Harris, Everette, Gendler, Jeffrey
• Primary Examiner(s): Seifu, Lessanework
• Application Number:
  US14/836,792
• Publication Number:
  US 20150361360A1
• Time in Patent Office: 993 Days
• CPC Class Codes: B01J 23/28 Molybdenum
• CPC Class Codes: B01J 27/043 with iron group metals or platinum group metals
• CPC Class Codes: B01J 27/047 with chromium, molybdenum, tungsten or polonium
• CPC Class Codes: B01J 27/051 Molybdenum
• CPC Class Codes: B01J 35/50 characterised by their shape or configuration
• CPC Class Codes: B01J 35/66 Pore distribution
• CPC Class Codes: B01J 35/69 bimodal
• CPC Class Codes: B01J 37/04 Mixing B01J37/0009, B01J37/0018 take precedence
• CPC Class Codes: B01J 37/086 Decomposition of an organometallic compound, a metal complex or a metal salt of a carboxylic acid
• CPC Class Codes: B01J 37/20 Sulfiding
• 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 2300/206 Asphaltenes
• CPC Class Codes: C10G 47/12 Inorganic carriers
• CPC Class Codes: C10G 69/06 including at least one step of thermal cracking in the absence of hydrogen
• CPC Class Codes: C10G 9/005 Coking (in order to produce liquid products mainly)

Abstract

Methods and systems for hydroprocessing heavy oil feedstocks to form an upgraded material involve the use of a colloidal or molecular catalyst dispersed within a heavy oil feedstock, a pre-coking hydrocracking reactor, a separator, and a coking reactor. The colloidal or molecular catalyst promotes upgrading reactions that reduce the quantity of asphaltenes or other coke forming precursors in the feedstock, increase hydrogen to carbon ratio in the upgraded material, and decrease boiling points of hydrocarbons in the upgraded material. The methods and systems can be used to upgrade vacuum tower bottoms and other low grade heavy oil feedstocks. The result is one or more of increased conversion level and yield, improved quality of upgraded hydrocarbons, reduced coke formation, reduced equipment fouling, processing of a wider range of lower quality feedstocks, and more efficient use of supported catalyst if used in combination with the colloidal or molecular catalyst, as compared to a conventional hydrocracking process or a conventional thermal coking process.

Claims

1. A hydroprocessing system for hydroprocessing a heavy oil feedstock to form coke and upgraded hydrocarbon products, comprising:

a heavy oil feedstock comprised of a substantial quantity of hydrocarbons having a boiling point greater than about 343°

C., asphaltenes or other coke forming precursors, and a colloidal or molecular catalyst dispersed throughout the feedstock;

a pre-coking hydrocracking reactor configured to heat or maintain the heavy oil feedstock at a hydrocracking temperature together with hydrogen and convert at least a portion of higher boiling hydrocarbons in the heavy oil feedstock in the presence of the colloidal or molecular catalyst to lower boiling hydrocarbons, reduce the quantity of asphaltenes or other coke forming precursors by at least 20%, and thereby form an upgraded material, the pre-coking hydrocracking reactor comprised of (i) an inlet port at a bottom of the reactor into which the heavy oil feedstock and hydrogen are introduced and (ii) an outlet port at a top of the reactor from which the upgraded material, colloidal or molecular catalyst, and hydrogen are withdrawn;

a first separator configured to separate gaseous and volatile fractions from a liquid hydrocarbon fraction in the upgraded material, the first separator being comprised of (i) an inlet through which the upgraded material is introduced, (ii) a first outlet through which the gaseous and volatile fractions are withdrawn, and (iii) a second outlet through which the liquid hydrocarbon fraction is withdrawn;

one or more coking reactors configured to receive and process the liquid hydrocarbon fraction; and

a second separator configured to receive and process upgraded products from the one or more coking reactors, the second separator having an inlet and an outlet, wherein the inlet of the second separator is in fluid communication with an outlet of the one or more coking reactors and the outlet of the second separator is in fluid communication with an inlet of the one or more coking reactors.

2. The hydroprocessing system of claim 1, wherein the heavy oil feedstock comprises at least one of heavy crude oil, oil sand bitumen, atmospheric tower bottoms, vacuum tower bottoms, resid, visbreaker bottoms, coal tar, heavy oil from oil shale, or liquefied coal.

3. The hydroprocessing system of claim 1, wherein the heavy oil feedstock comprises at least about 10 wt % asphaltenes or other coke forming precursors.

4. The hydroprocessing system of claim 1, wherein the pre-coking hydrocracking reactor comprises at least one of a slurry phase reactor, an ebullated bed reactor, or a fixed bed reactor.

5. The hydroprocessing system of claim 1, wherein the pre-coking hydrocracking reactor is a slurry phase reactor including (i) an inlet port at a bottom of the slurry phase reactor into which the heavy oil feedstock and hydrogen are introduced and (ii) an outlet port at a top of the slurry phase reactor from which the upgraded material, colloidal or molecular catalyst, and hydrogen are withdrawn.

6. The hydroprocessing system of claim 5, the slurry phase reactor further comprising a recycle channel, a recycling pump, and a distributor grid plate.

7. The hydroprocessing system of claim 1, wherein the first separator comprises a hot separator.

8. The hydroprocessing system of claim 1, wherein the first separator comprises a distillation tower.

9. The hydroprocessing system of claim 1, wherein the first separator comprises a hot separator and a distillation tower.

10. The hydroprocessing system of claim 1, wherein the liquid hydrocarbon fraction from the first separator and introduced into the one or more coking reactors comprises a vacuum reduced crude.

11. The hydroprocessing system of claim 1, wherein the one or more coking reactors comprise one or more delayed coking reactors, fluid coking reactors, or Flexicoking®

reactors.

12. The hydroprocessing system of claim 1, the system comprising:

the pre-coking hydrocracking reactor as a first hydrocracking reactor; and

a second pre-coking hydrocracking reactor downstream of the first hydrocracking reactor, wherein the second pre-coking hydrocracking reactor is configured to further upgrade the upgraded material from the first hydrocracking reactor, the second hydrocracking reactor comprising at least one of a slurry phase reactor, an ebullated bed reactor, or a fixed bed reactor.

13. The hydroprocessing system of claim 1, further comprising:

a secondary pre-coking hydrocracking reactor downstream from the first separator; and

a secondary separator downstream from the secondary pre-coking hydrocracking reactor,

wherein the second pre-coking hydrocracking reactor is configured to upgrade the liquid hydrocarbon fraction from the first separator to form a further upgraded material to be introduced into the secondary separator, which is configured to separate gaseous and volatile fractions from a liquid hydrocarbon fraction in the further upgraded material.

14. The hydroprocessing system of claim 1, the pre-coking hydrocracking reactor being configured to perform upgrading reactions that reduce the quantity of asphaltenes or other coke forming precursors by at least 40 wt %.

15. The hydroprocessing system of claim 1, the pre-coking hydrocracking reactor being configured to perform upgrading reactions that reduce the quantity of asphaltenes or other coke forming precursors by at least 60 wt %.

16. The hydroprocessing system of claim 1, the hydroprocessing system being configured to convert at least 60 wt % of hydrocarbons having a boiling point of at least 524°

C. (975°

F.).

17. The hydroprocessing system of claim 1, the hydroprocessing system being configured to convert at least 70 wt % of hydrocarbons having a boiling point of at least 524°

C. (975°

F.).

18. The hydroprocessing system of claim 1, the hydroprocessing system being configured to convert at least 80 wt % of hydrocarbons having a boiling point of at least 524°

C. (975°

F.).

19. The hydroprocessing system of claim 1, the hydroprocessing system being configured to convert at least 85 wt % of hydrocarbons having a boiling point of at least 524°

C. (975°

F.).

20. The hydroprocessing system of claim 1, the hydroprocessing system being configured to yield at least 80 wt % of C4+ hydrocarbons and a boiling point of less than about 524°

C. (975°

F.).

21. The hydroprocessing system of claim 1, the hydroprocessing system being configured to reduce coke formation by at least 25 wt % compared to coking in the absence of hydrocracking catalyzed by the molecular or colloidal catalyst.

22. The hydroprocessing system of claim 1, further comprising:

a pre-mixer configured to mix a hydrocarbon oil diluent and an oil soluble catalyst precursor at a temperature below a decomposition temperature of the catalyst precursor starts and form a diluted precursor mixture;

a second mixer, downstream from the pre-mixer, configured the mix the diluted precursor mixture with a heavy oil feedstock to yield a conditioned feedstock that is configured to form the colloidal or molecular catalyst upon heating and decomposing the catalyst precursor and allowing metal liberated therefrom to react with sulfur liberated from the feedstock; and

a heater configured to heat the conditioned feedstock, decompose the catalyst precursor, and cause or allow metal liberated from the decomposed catalyst precursor to react with sulfur liberated from the heavy oil feedstock and form the colloidal or molecular catalyst.

23. The hydroprocessing system of claim 22, wherein the hydrocarbon oil diluent comprises at least one of vacuum gas oil, decant oil, cycle oil, or light gas oil.

24. The hydroprocessing system of claim 22, wherein the catalyst precursor comprises at least one transition metal and at least one organic moiety comprising or derived from 3-cyclopentylpropionic acid, cyclohexanebutyric acid, biphenyl-2-carboxylic acid, 4-heptylbenzoic acid, 5-phenylvaleric acid, geranic acid, 10-undecenoic acid, dodecanoic acid, octanoic acid, 2-ethylhexanoic acid, naphthanic acid, pentacarbonyl, or hexacarbonyl.

25. The hydroprocessing system of claim 24, wherein the at least one transition metal comprises one or more of Mo, Ni, Co, W, V or Fe.

26. The hydroprocessing system of claim 22, the catalyst precursor comprising at least one of molybdenum 3-cyclopentylpropionate, molybdenum cyclohexanebutanoate, molybdenum biphenyl-2-carboxylate, molybdenum 4-heptylbenzoate, molybdenum 5-phenylpentanoate, molybdenum geranate, molybdenum 10-undecenoate, molybdenum dodecanoate, molybdenum 2-ethylhexanoate, molybdenum naphthanate, molybdenum hexacarbonyl, vanadium octoate, vanadium naphthanate, or iron pentacarbonyl.

27. The hydroprocessing system of claim 22, the ratio of catalyst precursor composition to hydrocarbon oil diluent being in a range of about 1:

100 to about 1;

5.

28. The hydroprocessing system of claim 22, wherein the pre-mixer is configured to mix the hydrocarbon oil diluent and catalyst precursor composition at temperature in a range of about 25°

C. to about 250°

C., wherein the mixer is configured to mix the diluted precursor mixture and heavy oil feedstock being at a temperature in a range of about 25°

C. to about 350°

C., and wherein the heater is configured to heat the conditioned feedstock to a temperature in a range of about 275°

C. to about 375°

C.

29. The hydroprocessing system of claim 22, wherein the pre-mixer is configured to mix the hydrocarbon oil diluent and catalyst precursor composition at temperature in a range of about 75°

C. to about 150°

C., wherein the mixer is configured to mix the diluted precursor mixture and heavy oil feedstock being at a temperature in a range of about 75°

C. to about 250°

C., and wherein the heater is configured to heat the conditioned feedstock to a temperature in a range of about 310°

C. to about 360°

C.

30. The hydroprocessing system of claim 22, the hydrocarbon oil diluent and catalyst precursor composition being mixed at temperature in a range of about 75°

C. to about 150°

C., the diluted precursor mixture and heavy oil feedstock being mixed at a temperature in a range of about 75°

C. to about 250°

C., and the conditioned feedstock being heated to a temperature in a range of about 310°

C. to about 360°

C.

31. The hydroprocessing system of claim 22, wherein the pre-mixer is configured to mix the hydrocarbon oil diluent and catalyst precursor for a time period in a range of about 1 second to about 20 minutes, and wherein the mixer is configured to mix the diluted precursor mixture and heavy oil feedstock for a time period in a range of about 1 second to about 20 minutes.

32. The hydroprocessing system of claim 22, wherein the pre-mixer is configured to mix the hydrocarbon oil diluent and catalyst precursor for a time period in a range of about 1 second to about 10 minutes, and wherein the mixer is configured to mix the diluted precursor mixture and heavy oil feedstock for a time period in a range of about 1 second to about 10 minutes.

33. The hydroprocessing system of claim 1, wherein the pre-coking hydrocracking reactor comprises at least one of a slurry phase reactor, an ebullated bed reactor, or a fixed bed reactor.

34. A hydroprocessing system for hydroprocessing a heavy oil feedstock to form coke and upgraded hydrocarbon products, comprising:

a heavy oil feedstock comprised of a substantial quantity of hydrocarbons having a boiling point greater than about 343°

C., asphaltenes or other coke forming precursors, and a colloidal or molecular catalyst dispersed throughout the feedstock;

a pre-coking slurry-phase hydrocracking reactor configured to heat or maintain the heavy oil feedstock at a hydrocracking temperature together with hydrogen and convert at least a portion of higher boiling hydrocarbons in the heavy oil feedstock in the presence of the colloidal or molecular catalyst to lower boiling hydrocarbons, reduce the quantity of asphaltenes or other coke forming precursors by at least 20%, and thereby form an upgraded material, the pre-coking hydrocracking reactor comprised of (i) an inlet port at a bottom of the reactor into which the heavy oil feedstock and hydrogen are introduced and (ii) an outlet port at a top of the reactor from which the upgraded material, colloidal or molecular catalyst, and hydrogen are withdrawn;

a separator configured to separate gaseous and volatile fractions from a liquid hydrocarbon fraction in the upgraded material, the separator being comprised of (i) an inlet through which the upgraded material is introduced into the separator, (ii) a first outlet through which the gaseous and volatile fractions are withdrawn, and (iii) a second outlet through which the liquid hydrocarbon fraction is withdrawn;

one or more coking reactors configured to receive and process at least a portion of the liquid hydrocarbon fraction and form upgraded products and coke; and

a coking fractionator configured to fractionate the liquid hydrocarbon fraction received from the separator and the upgraded products received from the one or more coking reactors, the coking fractionator being comprised of (i) a first inlet through which the liquid hydrocarbon fraction is received from the separator, (ii) a first outlet through which at least a portion of a fractionated liquid hydrocarbon is withdrawn to the one or more coking reactors, (iii) a second inlet through which the upgraded products from the one or more coking reactors are received, and (iv) a second outlet through which fractioned products from the liquid hydrocarbon fraction and/or the one or more coking reactors are withdrawn.

35. A hydroprocessing system for hydroprocessing a heavy oil feedstock to form coke and upgraded hydrocarbon products, comprising:

a heavy oil feedstock comprised of a substantial quantity of hydrocarbons having a boiling point greater than about 343°

C., asphaltenes or other coke forming precursors, and a colloidal or molecular catalyst dispersed throughout the feedstock;

a pre-coking ebullated-bed hydrocracking reactor comprising a solid supported ebullated bed catalyst and the colloidal or molecular catalyst and that is configured to heat or maintain the heavy oil feedstock at a hydrocracking temperature together with hydrogen and convert at least a portion of higher boiling hydrocarbons in the heavy oil feedstock to lower boiling hydrocarbons, reduce the quantity of asphaltenes or other coke forming precursors by at least 20%, and thereby form an upgraded material, the pre-coking hydrocracking reactor comprised of (i) an inlet port at a bottom of the reactor into which the heavy oil feedstock and hydrogen are introduced and (ii) an outlet port at a top of the reactor from which the upgraded material, colloidal or molecular catalyst, and hydrogen are withdrawn;

a hot separator configured to separate gaseous and volatile fractions from a liquid hydrocarbon fraction in the upgraded material;

a distillation tower configured to receive the liquid hydrocarbon fraction from the hot separator and separate distillates from a residual material;

a coking fractionator configured to receive the residual material from the distillation tower and upgraded products from one or more coking reactors and fractionate them into fractionated products and a fractioned liquid hydrocarbon, the coking fractionator being comprised of (i) a first inlet through which the residual material is received from the distillation tower, (ii) a first outlet through which the fractionated products are withdrawn, and (iii) a second inlet through which upgraded products from the one or more coking reactors are received; and

(iv) a second outlet through which the fractionated liquid hydrocarbon is withdrawn; and

the one or more coking reactors configured to receive and process the fractionated liquid hydrocarbon from the coking fractionator and form the upgraded products and coke, the one or more coking reactors including an inlet in fluid communication with the second outlet of the coking fractionator and an outlet in fluid communication with the second inlet of the coking fractionator.