Apparatus for the liquefaction of natural gas and methods relating to same

• US 7,591,150 B2
• Filed: 05/15/2006
• Issued: 09/22/2009
• Est. Priority Date: 05/04/2001
• Status: Active Grant

• Current Assignee: Battelle Energy Alliance LLC (Battelle Memorial Institute)
• Original Assignee: Battelle Energy Alliance LLC (Battelle Memorial Institute)
• Inventors: Wilding, Bruce M., Turner, Terry D., McKellar, Michael G.
• Primary Examiner(s): Doerrler; William C
• Application Number:
  US11/383,411
• Publication Number:
  US 20060218939A1
• Time in Patent Office: 1,226 Days
• Field of Search: 626/13, 625/32, 625/37
• US Class Current: 62/613
• CPC Class Codes: F25J 1/0022 Hydrocarbons, e.g. natural gas
• CPC Class Codes: F25J 1/0037 of a return stream
• CPC Class Codes: F25J 1/004 by flash gas recovery F25J1/0267 takes precedence
• CPC Class Codes: F25J 1/0045 by vaporising a liquid return stream
• CPC Class Codes: F25J 1/0201 using only internal refrigeration means, i.e. without external refrigeration
• CPC Class Codes: F25J 1/0232 integration within a pressure letdown station of a high pressure pipeline system
• CPC Class Codes: F25J 1/0247 start-up of the process
• CPC Class Codes: F25J 1/0251 Intermittent or alternating process, so-called batch process, e.g. "peak-shaving"
• CPC Class Codes: F25J 1/0275 adapted for special use of the liquefaction unit, e.g. portable or transportable devices
• CPC Class Codes: F25J 2205/20 using solidification of components
• CPC Class Codes: F25J 2205/60 using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
• CPC Class Codes: F25J 2205/84 using filter
• CPC Class Codes: F25J 2210/06 Splitting of the feed stream, e.g. for treating or cooling in different ways
• CPC Class Codes: F25J 2215/60 Methane
• CPC Class Codes: F25J 2220/62 Separating low boiling components, e.g. He, H2, N2, Air
• CPC Class Codes: F25J 2220/66 Separating acid gases, e.g. CO2, SO2, H2S or RSH
• CPC Class Codes: F25J 2220/68 Separating water or hydrates
• CPC Class Codes: F25J 2230/60 the fluid being hydrocarbons or a mixture of hydrocarbons
• CPC Class Codes: F25J 2270/04 Internal refrigeration with work-producing gas expansion loop
• CPC Class Codes: F25J 2280/02 Control in general, load changes, different modes ("runs"), measurements
• CPC Class Codes: F25J 3/08 : Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixturescold traps B01D8/00

Abstract

An apparatus and method for producing liquefied natural gas. A liquefaction plant may be coupled to a source of unpurified natural gas, such as a natural gas pipeline at a pressure letdown station. A portion of the gas is drawn off and split into a process stream and a cooling stream. The cooling stream passes through an expander creating work output. A compressor may be driven by the work output and compresses the process stream. The compressed process stream is cooled, such as by the expanded cooling stream. The cooled, compressed process stream is expanded to liquefy the natural gas. A gas-liquid separator separates a vapor from the liquid natural gas. A portion of the liquid gas is used for additional cooling. Gas produced within the system may be recompressed for reintroduction into a receiving line or recirculation within the system for further processing.

Claims

1. A method of producing liquid natural gas, the method comprising:

providing a source of unpurified natural gas and flowing a portion of the unpurified natural gas from the source;

dividing the portion of unpurified natural gas into at least a process stream and a cooling stream;

flowing the process stream sequentially through a compressor and a first side of at least one heat exchanger;

flowing the cooling stream sequentially through an expander and a second side of the at least one heat exchanger;

sensing a temperature of the process stream after it exits the first side of the at least one heat exchanger;

flowing substantially all of the process stream from the first side of the at least one heat exchanger to the second side of the at least one heat exchanger if a sensed temperature is warmer than a specified temperature; and

flowing at least a portion of the process stream from the first side of the at least one heat exchanger to a gas-liquid separator if the sensed temperature is colder than the specified temperature.

2. The method according to claim 1, wherein the specified temperature is between approximately −

90°

F. and approximately −

180°

F.

3. The method according to claim 1, wherein flowing substantially all of the process stream from the first side of the at least one heat exchanger to the second side of the at least one heat exchanger further includes flowing at least a portion of the process stream through an expansion valve.

4. The method according to claim 1, wherein flowing at least a portion of the process stream from the first side of the at least one heat exchanger to a gas-liquid separator further includes flowing the at least a portion of the process stream through at least one expansion valve.

5. The method according to claim 4, wherein flowing the at least a portion of the process stream through at least one expansion valve includes flowing the at least a portion of the process stream through at least two expansion valves.

6. The method according to claim 5, further comprising arranging the at least two expansion valves in a parallel flow configuration.

7. The method according to claim 6, further comprising configuring a first expansion valve of the at least two expansion valves to exhibit a first flow capacity (C_v) and configuring a second valve of the at least two expansion valves to exhibit a second flow capacity (C_v), different from the first flow capacity (C_v).

8. The method according to claim 6, further comprising flowing approximately 80% of the at least a portion of the process stream through a first expansion valve of the at least two expansion valves.

9. The method according to claim 8, further comprising flowing a remainder of the at least a portion of the process stream through a second expansion valve of the at least two expansion valves.

10. The method according to claim 1, further comprising producing a slurry of liquid natural gas and solid carbon dioxide from the at least a portion of the process stream within the gas-liquid separator.

11. The method according to claim 10, further comprising agitating the slurry to keep the solid carbon dioxide substantially suspended within the liquid natural gas.

12. The method according to claim 11, wherein agitating the slurry further includes bubbling a gas through the slurry.

13. The method according to claim 10, further comprising transferring at least a portion of the slurry from the gas-liquid separator to at least one transfer tank.

14. The method according to claim 13, wherein transferring at least a portion of the slurry from the gas-liquid separator to at least one transfer tank further comprises selectively transferring the at least a portion of the slurry from the gas-liquid separator to a plurality of transfer tanks.

15. The method according to claim 14, further comprising flowing the at least a portion of the slurry from at least one of the plurality of transfer tanks to at least one hydrocyclone.

16. The method according to claim 15, wherein flowing the at least a portion of the slurry from at least one of the plurality of transfer tanks to at least one hydrocyclone further comprises selectively flowing the at least a portion of slurry from the at least one of the plurality of transfer tanks to a plurality of hydrocyclones.

17. The method according to claim 15, further comprising flowing a slush that is rich in solid carbon dioxide through an underflow of the at least one hydrocyclone to a sublimation tank.

18. The method according to claim 17, further comprising subliming the solid carbon dioxide to a gas.

19. The method according to claim 15, further comprising flowing liquid natural gas through an overflow of the at least one hydrocyclone to a diversion tank.

20. The method according to claim 19, further comprising flowing the liquid natural gas through at least one filter prior to flowing the liquid natural gas to the diversion tank.

21. The method according to claim 19, further comprising flowing at least a portion of the liquid natural gas from the diversion tank to the second side of the at least one heat exchanger.

22. The method according to claim 21, further comprising flowing the at least a portion of the liquid natural gas to a storage tank.

23. The method according to claim 21, further comprising flowing the at least a portion of the cooling stream back into the source of unpurified natural gas.

24. The method according to claim 23, further comprising compressing the at least a portion of the cooling stream prior to flowing it into the source of unpurified natural gas.

25. The method according to claim 21, further comprising recirculating at least a portion of the cooling stream back into at least one of the cooling stream and the process stream.

26. The method according to claim 25, further comprising compressing the at least a portion of the cooling stream prior to recirculating it into at least one of the cooling stream and the process stream.

27. The method according to claim 1, further comprising compressing the portion of the unpurified natural gas flowed from the source prior to dividing the portion of unpurified natural gas into at least a process stream and a cooling stream.

28. A liquefaction plant comprising:

a first flow path defined and configured for sequential delivery of a first stream of natural gas through a compressor and a first side of at least one heat exchanger;

a second flow path defined and configured for sequential delivery of a second stream of natural gas through an expander and a second side of the at least one heat exchanger;

at least two paths including a cooling path and a liquid production path formed from the first flow path at a location subsequent an intended flow of the first stream of natural gas through the first side of the at least one heat exchanger, wherein the cooling path is defined and configured to selectively direct a flow of gas to the second side of the at least one heat exchanger and wherein the liquid production path is defined and configured to selectively direct a flow of gas to a gas-liquid separator.

29. The liquefaction plant of claim 28, further comprising at least one transfer tank located and configured to receive a solid-liquid slurry from the gas-liquid separator.

30. The liquefaction plant of claim 29, wherein the at least one transfer tank includes at least two transfer tanks which are in selective communication with the gas-liquid separator.

31. The liquefaction plant of claim 29, further comprising at least one hydrocyclone in selective communication with the at least one transfer tank.

32. The liquefaction plant of claim 31, further comprising a diversion tank in communication with an overflow of the at least one hydrocyclone.

33. The liquefaction plant of claim 32, further comprising a pump located and configured to convey a mass of liquid from the diversion tank to the second side of the at least one heat exchanger.

34. The liquefaction plant of claim 32, further comprising a storage tank in selective communication with the diversion tank.

35. The liquefaction pant of claim 32, further comprising at least one filter disposed in a flow path between the at least one hydrocyclone and the diversion tank.

36. The liquefaction plant of claim 31, further comprising a sublimation tank in communication with an underflow of the at least one hydrocyclone.

37. The liquefaction plant of claim 28, further comprising a recompression compressor configured to receive a flow of gas from the second side of the at least one heat exchanger.

38. The liquefaction plant of claim 37, further comprising another flow path from the recompression compressor to an exit of the liquefaction plant.

39. The liquefaction plant of claim 37, further comprising another flow path from the recompression compressor to at least one of the first flow path and the second flow path.

40. The liquefaction plant of claim 28, further comprising another compressor in communication with the first flow path and the second flow path.