IP Library › Granted Patent US 12,215,922
Granted Patent B2
US 12,215,922 · App. 16/421,138 · Granted Feb 4, 2025

Integrated heavy hydrocarbon and BTEX removal in LNG liquefaction for lean gases

Inventors: John Mak (Santa Ana, CA); Jacob Thomas (Sugar Land, TX); Dhirav Patel (Sugar Land, TX); Curt Graham (Mission Viejo, CA); Irene Zhang (Sugar Land, TX)
Assignee: Fluor Technologies Corporation
F25J3/0209F25J3/0242F25J2205/04F25J2205/50F25J2210/06F25J2210/60F25J2220/64
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Quick Facts
Patent No.
US 12,215,922
App. No.
16/421,138
Granted
Feb 4, 2025
Kind
B2
Abstract

A method for removing heavy hydrocarbons from a feed gas by: feeding, into an absorber, a top reflux stream and a second reflux stream below the top reflux stream, wherein the absorber produces an absorber bottom product stream and an absorber overhead product stream; depressurizing and feeding the absorber bottom product stream to a stripper to produce a stripper bottom product stream and a stripper overhead product stream; cooling and feeding a portion of the absorber overhead product stream back to the absorber as the top reflux stream; and pressurizing and feeding the stripper overhead product stream back to the absorber as the second reflux stream. Systems for carrying out the method are also provided.

Claims (94)

1. A method for removing heavy hydrocarbons from a feed gas, the method comprising:

cooling an inlet gas in a propane pre-cooling heat exchanger;

separating the cooled inlet gas to produce the feed gas and a feed liquid;

feeding, into an absorber, the feed gas, a top reflux stream, and a second reflux stream below the top reflux stream, wherein the absorber produces an absorber bottom product stream and an absorber overhead product stream;

depressurizing and feeding the absorber bottom product stream to a stripper to produce a stripper bottom product stream and a stripper overhead product stream;

cooling and feeding a portion of the absorber overhead product stream back to the absorber as the top reflux stream; and

pressurizing and feeding the stripper overhead product stream back to the absorber as the second reflux stream.

2. The method of claim 1 , further comprising:

feeding the feed liquid to the stripper; and

expanding the feed gas before feeding the feed gas to the absorber, wherein the feed gas is fed to a lower portion of the absorber.

3. The method of claim 2 , wherein expanding the feed gas comprises expanding the feed gas in a turboexpander.

4. The method of claim 1 , wherein cooling the inlet gas comprises:

after passing the inlet gas through the propane pre-cooling heat exchanger, passing the inlet gas through a cold box, wherein the cold box comprises a plurality of passes configured to provide heat exchange between the inlet gas, the absorber overhead product stream, the absorber bottom product stream, the stripper overhead product stream, and the portion of the absorber overhead product stream.

5. The method of claim 1 , further comprising:

after passing the inlet gas through the propane pre-cooling heat exchanger, passing the inlet gas through a first heat exchanger, wherein the first heat exchanger is configured to cross-exchange the inlet gas with a part of the absorber overhead product stream.

6. The method of claim 1 , wherein the propane pre-cooling heat exchanger is part of a propane pre-cooling train of a LNG liquefaction plant, the method further comprising: locating the propane pre-cooling train to a NGL extraction train that contains the absorber and the stripper.

7. The method of claim 1 , wherein a combined mass flow rate of the feed liquid and the absorber bottom product stream is less than 10% of a mass flowrate of the inlet gas.

8. The method of claim 1 , wherein the inlet gas has less than 2 gallons per thousand cubic feet of gas of C3+ components.

9. The method of claim 1 , before cooling and feeding the portion of the absorber overhead product stream back to the absorber, the method further comprising:

heating a first part of the of the absorber overhead product stream and cooling the inlet gas in a first heat exchanger;

heating a second part of the absorber overhead product stream and cooling the portion of the absorber overhead product stream in a second heat exchanger; and

heating a third part of the absorber overhead product stream and cooling the stripper overhead product stream in a third heat exchanger.

10. The method of claim 9 , further comprising:

combining the heated first, second, and third parts to form a heat exchanged absorber overhead product, and

compressing the heat exchanged absorber overhead product to form a residue gas stream at a pressure of from about 800 psig to about 900 psig, wherein the portion of the absorber overhead product stream that is fed back to the absorber as the top reflux stream is a portion of the residue gas stream.

11. The method of claim 9 , further comprising:

combining the heated first, second, and third parts to form a heat exchanged absorber overhead product,

wherein the heat exchanged absorber overhead product does not need recompression before a second portion of the absorber overhead product stream flows to a LNG liquefaction plant as a product feed.

12. The method of claim 1 , before cooling and feeding the portion of the absorber overhead product stream back to the absorber, the method further comprising:

heating the absorber overhead product stream in a cold box to form a heat exchanged absorber overhead product.

13. The method of claim 12 , further comprising:

compressing the absorber overhead product stream to form a residue gas stream at a pressure of from about 800 psig to about 900 psig, wherein the portion of the absorber overhead product stream that is fed back to the absorber as the top reflux stream is a portion of the residue gas stream.

14. The method of claim 13 , wherein a second portion of the absorber overhead product stream forms a product feed to a LNG liquefaction plant.

15. The method of claim 1 , wherein a second portion of the absorber overhead product stream forms a product feed to a LNG liquefaction plant.

16. The method of claim 15 , wherein the second portion has a pressure in a range of 800 psig to 900 psig.

17. The method of claim 1 , further comprising:

at least partially condensing the portion of the absorber overhead product stream prior to feeding the portion of the absorber overhead product stream back to the absorber.

18. The method of claim 1 , further comprising:

cooling and at least partially condensing a portion of the stripper overhead product stream prior to feeding the stripper overhead product stream back to the absorber.

19. The method of claim 1 , wherein the absorber is operated at a higher pressure than the stripper.

20. The method of claim 1 , wherein the top reflux stream and the second reflux stream comprise primarily methane.

21. A system for removing heavy hydrocarbons from a feed gas, the system comprising:

a propane pre-cooling heat exchanger configured to cool an inlet gas;

an absorber, wherein the absorber is configured to receive a top reflux stream and a second reflux stream within a top portion of the absorber, receive an expanded feed gas stream at a bottom portion of the absorber, and produce an absorber bottom product stream and an absorber overhead product stream;

a stripper, wherein the stripper is configured to receive a feed liquid and the absorber bottom product stream and produce a stripper overhead product stream and a stripper bottom product stream;

a pressure reduction valve configured to reduce a pressure of the absorber bottom product stream between the absorber and the stripper; and

a compressor configured to pressurize the stripper overhead product stream from the stripper to form a compressed stripper overhead product stream, wherein the compressed stripper overhead product stream is configured to pass back to the absorber as the second reflux stream.

22. The system of claim 21 , further comprising:

a cold box, wherein the cold box is configured to cool and at least partially condense the compressed stripper overhead product stream to form the second reflux stream, cool and at least partially condense a portion of the absorber overhead product stream to form the top reflux stream, and cool and partially condense the inlet gas to produce the feed gas and the feed liquid.

23. The system of claim 22 , further comprising:

a separator, wherein the separator is configured to receive and separate the inlet gas into the feed gas and the feed liquid; and

an expander, wherein the expander is configured to receive the feed gas from the separator and expand the feed gas to produce the expanded feed gas stream, wherein the expander is a turboexpander.

24. The system of claim 21 , further comprising:

a first heat exchanger configured to further cool the inlet gas using a first part of the absorber overhead product stream;

a second heat exchanger configured to cool and at least partially condense a portion of a residue gas stream using a second part of the absorber overhead product stream, wherein a portion of the residue gas stream forms the top reflux;

a third heat exchanger configured to cool and at least partially condense the compressed stripper overhead product stream to form the second reflux stream using a third part of the absorber overhead product stream.

25. The system of claim 24 , further comprising:

a separator, wherein the separator is configured to receive and separate the inlet gas into the feed gas and the feed liquid;

an expander, wherein the expander is configured to receive the feed gas from the separator and expand the feed gas to produce the expanded feed gas stream, wherein the expander is a turboexpander; and

a second compressor configured to compress a heat exchanged absorber overhead product stream to form the residue gas stream,

wherein the first part, second part, and third part of the absorber overhead product stream are configured to combine to form the heat exchanged absorber overhead product stream.

26. The system of claim 25 , further comprising:

a LNG liquefaction plant, wherein the propane pre-cooling heat exchanger is relocated from the LNG liquefaction plant to a location upstream of the absorber for cooling the inlet gas.

27. The system of claim 21 , wherein the stripper has an internal diameter less than 30% of an internal diameter of the absorber.

28. The system of claim 21 , wherein the absorber and the stripper are integrated into a single column.

29. A system for removing heavy hydrocarbons from a feed gas, the system comprising:

a propane pre-cooling heat exchanger configured to cool an inlet gas;

an absorber section and a stripper section, wherein the absorber section is configured to operate at a pressure higher than the stripper section,

wherein the absorber section comprises:

an absorber, wherein the absorber is configured to receive a top reflux stream and a second reflux stream within a top portion of the absorber, receive an expanded feed gas stream at a bottom portion of the absorber, and produce an absorber bottom product stream and an absorber overhead product stream, and

wherein the stripper section comprises:

a stripper, wherein the stripper is configured to receive a feed liquid and a reduced pressure absorber bottom product stream and produce a stripper overhead product stream and a stripper bottom product stream;

a pressure reduction valve configured to reduce a pressure of the absorber bottom product stream to produce the reduced pressure absorber bottom product stream; and

a compressor configured to pressurize the stripper overhead product stream from the stripper to form the second reflux stream.

30. The system of claim 29 , further comprising:

a heat exchanger, wherein the heat exchanger is configured to cool and at least partially condense the second reflux stream prior to the second reflux stream entering the absorber, cool and at least partially condense a portion of the absorber overhead product stream to form the top reflux stream, and cool and at least partially condense the inlet gas to produce the feed gas and the feed liquid.

31. The system of claim 30 , further comprising:

a second pressure reduction valve, wherein the second pressure reduction valve is configured to reduce a pressure of the top reflux stream prior to the top reflux stream entering the absorber;

a separator, wherein the separator is configured to receive and separate the inlet gas into the feed gas and the feed liquid;

a third pressure reduction valve, the third pressure reduction valve configured to reduce a pressure of the feed liquid prior to the feed liquid entering the stripper;

an expander, wherein the expander is configured to receive the feed gas from the separator and expand the feed gas to produce the expanded feed gas stream, wherein the expander is a turboexpander.

32. The system of claim 29 , further comprising:

a first heat exchanger configured to further cool the inlet gas using a first part of the absorber overhead product stream;

a second heat exchanger configured to cool and at least partially condense a portion of a residue gas stream using a second part of the absorber overhead product stream, wherein a portion of the residue gas stream forms the top reflux; and

a third heat exchanger configured to cool and at least partially condense the compressed stripper overhead product stream to form the second reflux stream using a third part of the absorber overhead product stream.

33. The system of claim 32 , further comprising:

a separator, wherein the separator is configured to receive and separate the inlet gas into the feed gas and the feed liquid;

an expander, wherein the expander is configured to receive the feed gas from the separator and expand the feed gas to produce the expanded feed gas stream, wherein the expander is a turboexpander; and

a second compressor configured to compress a heat exchanged absorber overhead product stream to form the residue gas stream,

wherein the first part, second part, and third part of the absorber overhead product stream are configured to combine to form the heat exchanged absorber overhead product stream.

34. The system of claim 29 , further comprising:

a LNG liquefaction plant, wherein the propane pre-cooling heat exchanger is absent from the LNG liquefaction plant and is located upstream of the absorber for cooling the inlet gas.

35. The system of claim 29 , wherein the stripper has an internal diameter less than 30% of an internal diameter of the absorber.

36. The system of claim 29 , wherein the absorber and the stripper are integrated into a single column.

Assignments (1)
ASSIGNMENT OF ASSIGNOR'S INTEREST Recorded Aug 23, 2019
From: MAK, JOHN; THOMAS, JACOB; PATEL, DHIRAV; GRAHAM, CURT; ZHANG, IRENE
To: FLUOR TECHNOLOGIES CORPORATION, A DELAWARE CORPORATION
Reel/Frame 050142/0817 →
Continuity (1)
Related Publication 20200370824A1 · Nov 26, 2020
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