Method for nitrogen rejection and or helium recovery in an LNG liquefaction plant

• US 8,522,574 B2
• Filed: 12/31/2008
• Issued: 09/03/2013
• Est. Priority Date: 12/31/2008
• Status: Active Grant

• Current Assignee: Kellogg Brown & Root LLC (KBR Incorporated)
• Original Assignee: Kellogg Brown & Root LLC (KBR Incorporated)
• Inventors: Crawford, Duffer, Anantharaman, Bharthwaj, Coyle, David
• Primary Examiner(s): Jules, Frantz
• Assistant Examiner(s): CRENSHAW, HENRY T
• Application Number:
  US12/347,085
• Publication Number:
  US 20100162755A1
• Time in Patent Office: 1,707 Days
• Field of Search: 626/06, 626/11, 626/12, 626/13, 626/17, 626/18, 626/20, 626/21, 626/30
• US Class Current: 62/621
• CPC Class Codes: F25J 2200/02 in a single pressure main column system
• CPC Class Codes: F25J 2200/40 Features relating to the provision of boil-up in the bottom of a column
• CPC Class Codes: F25J 2200/70 Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
• CPC Class Codes: F25J 2205/02 using simple phase separation in a vessel or drum
• CPC Class Codes: F25J 2205/04 in the feed line, i.e. upstream of the fractionation step
• CPC Class Codes: F25J 2215/04 Recovery of liquid products
• CPC Class Codes: F25J 2240/02 Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
• CPC Class Codes: F25J 2240/30 Dynamic liquid or hydraulic expansion with extraction of work, e.g. single phase or two-phase turbine
• CPC Class Codes: F25J 2270/02 Internal refrigeration with liquid vaporising loop
• CPC Class Codes: F25J 2270/04 Internal refrigeration with work-producing gas expansion loop
• CPC Class Codes: F25J 3/0209 Natural gas or substitute natural gas
• CPC Class Codes: F25J 3/0233 separation of CnHm with 1 carbon atom or more
• CPC Class Codes: F25J 3/0242 separation of CnHm with 3 carbon atoms or more
• CPC Class Codes: F25J 3/0257 separation of nitrogen from air F25J3/04, production of nitrogen in general C01B21/00
• CPC Class Codes: F25J 3/029 of helium

Abstract

Methods of reducing the concentration of low boiling point components in liquefied natural gas are disclosed. The methods involve dynamic decompression of the liquefied natural gas and one or more pre-fractionation vessels. Particular embodiments are suited for recovering helium and/or nitrogen enriched streams from a liquefied natural gas stream.

Claims

1. A method of reducing the concentration of components having low boiling points in liquefied natural gas comprising:

providing an initial LNG stream at an initial liquefaction temperature and pressure;

passing the initial LNG stream through a first heat exchanger and a first liquid expander to reduce the temperature and dynamically decompress the LNG stream to obtain a first expanded LNG stream;

decompressing the first expanded LNG stream in a second liquid expander to obtain a second expanded LNG stream containing a vapor phase;

passing the second expanded LNG stream to a first pre-fractionation vessel for flash equilibrium separation to obtain a first vapor stream and a first liquid stream;

decompressing the first vapor stream in a first vapor expander to produce an expanded first vapor stream;

introducing the expanded first vapor stream to a fractionation column, wherein the expanded first vapor stream is introduced to an upper section of the fractionation column;

decompressing the first liquid stream in a third liquid expander to obtain a second liquid stream comprising a vapor phase;

separating the second liquid stream in a second pre-fractionation vessel for flash equilibrium separation to provide a second vapor stream and a third liquid stream;

introducing the second vapor stream and the third liquid stream to the fractionation column;

withdrawing a third vapor stream as an overhead from the fractionation column;

withdrawing from a lower portion of the fractionation column a fourth liquid stream;

passing at least a portion of the third vapor stream through the first heat exchanger to cool the initial LNG stream;

passing at least a portion of the third liquid stream through the first heat exchanger to cool the initial LNG stream and then to a third pre-fractionation vessel for flash equilibrium separation into a fourth vapor stream and a fifth liquid stream; and

introducing the fourth vapor stream and the fifth liquid stream to the fractionation column.

2. The method of claim 1, further comprising providing a second vapor expander in fluid communication with the second pre-fractionation vessel and the fractionation column, wherein the second vapor expander dynamically decompresses the second vapor stream to obtain an expanded second vapor stream.

3. The method of claim 2, further comprising:

mixing the expanded first vapor stream and the expanded second vapor stream to obtain an expanded mixed vapor stream; and

introducing the expanded mixed vapor stream to the upper section of the fractionation column.

4. The method of claim 1, wherein the fourth vapor stream provides vapor to the fractionation column needed to strip low boiling point components.

5. The method of claim 1, wherein the first and second pre-fractionation vessels are flash drums.

6. The method of claim 1, wherein the first and second pre-fractionation vessels do not contain trays.

7. The method of claim 1, wherein at least a portion of the first or second vapor streams passes through the first heat exchanger to cool the initial LNG stream.

8. The method of claim 7, wherein the third liquid stream is introduced to an upper portion of the fractionation column.

9. The method of claim 1, wherein the third vapor stream is nitrogen enriched.

10. The method of claim 1, wherein the fourth vapor stream and the fifth liquid stream are introduced to a lower portion of the fractionation column.

11. The method of claim 1, wherein the initial LNG stream comprises nitrogen, and wherein the first vapor stream and the second vapor stream each comprise at least 60 wt % of the nitrogen present in the initial LNG stream.

12. The method of claim 1, wherein the initial LNG stream comprises nitrogen and wherein the first vapor stream and the second vapor stream each comprise at least 95 wt % of the nitrogen present in the initial LNG stream.

13. The method of claim 1, wherein the fourth vapor stream and the fifth liquid stream are introduced to the fractionation column at a location below where the third liquid stream is introduced to the fractionation column.

14. A method of reducing the concentration of components having low boiling points in liquefied natural gas comprising:

passing an initial LNG stream through a first heat exchanger and a first liquid expander to reduce the temperature and dynamically decompress the LNG stream to obtain a first expanded LNG stream;

decompressing the first expanded LNG stream in a second liquid expander to obtain a second expanded LNG stream containing a vapor phase;

introducing the second expanded LNG stream to a first pre-fractionation vessel for flash equilibrium separation to obtain a first vapor stream and a first liquid stream;

decompressing the first vapor stream in a first vapor expander to obtain an expanded first vapor stream;

introducing the expanded first vapor stream to a fractionation column;

decompressing the first liquid stream in a third liquid expander to obtain a second liquid stream comprising a vapor phase;

separating the second liquid stream in a second pre-fractionation vessel for flash equilibrium separation to provide a second vapor stream and a third liquid stream;

decompressing the second vapor stream in a second vapor expander to obtain an expanded second vapor stream;

mixing the expanded first vapor stream and the expanded second vapor stream to obtain an expanded mixed vapor stream;

introducing the expanded mixed vapor stream to the upper section of the fractionation column;

introducing the third liquid stream to the fractionation column;

withdrawing a third vapor stream as an overhead from the fractionation column;

withdrawing a fourth liquid stream from a lower portion of the fractionation column;

passing at least a portion of the third vapor stream through the first heat exchanger to cool the initial LNG stream;

passing at least a portion of the third liquid stream through the first heat exchanger and to a third pre-fractionation vessel for flash equilibrium separation into a fourth vapor stream and a fifth liquid stream; and

introducing the fourth vapor stream and the fifth liquid stream to the fractionation column.

15. The method of claim 14, wherein the first, second, and third pre-fractionation vessels are flash drums.

16. The method of claim 14, wherein the initial LNG stream comprises nitrogen, and wherein the first vapor stream and the second vapor stream each comprise at least 60 wt % of the nitrogen present in the initial LNG stream.

17. The method of claim 14, wherein the initial LNG stream comprises nitrogen and wherein the first vapor stream and the second vapor stream each comprise at least 95 wt % of the nitrogen present in the initial LNG stream.

18. A method of reducing the concentration of components having low boiling points in liquefied natural gas comprising:

passing an initial LNG stream through a first heat exchanger and a first liquid expander to reduce the temperature and dynamically decompress the LNG stream to obtain a first expanded LNG stream;

decompressing the first expanded LNG stream in a second liquid expander to obtain a second expanded LNG stream containing a vapor phase;

introducing the second expanded LNG stream to a first flash drum to obtain a first vapor stream and a first liquid stream;

decompressing the first vapor stream from the first flash drum in a first vapor expander to obtain an expanded first vapor stream;

introducing the expanded first vapor stream to a fractionation column;

decompressing the first liquid stream in a third liquid expander to obtain a second liquid stream comprising a vapor phase;

separating the second liquid stream in a second flash drum to provide a second vapor stream and a third liquid stream;

decompressing the second vapor stream in a second vapor expander to obtain an expanded second vapor stream;

mixing the expanded first vapor stream and the expanded second vapor stream to obtain an expanded mixed vapor stream;

introducing the expanded mixed vapor stream to the upper section of the fractionation column;

introducing a first portion of the third liquid stream to the fractionation column;

passing a second portion of the third liquid stream through the first heat exchanger and to a third flash drum to obtain a fourth vapor stream and a fifth liquid stream;

introducing the fourth vapor stream and the fifth liquid stream to a lower portion of the fractionation column;

withdrawing a third vapor stream as an overhead from the fractionation column;

withdrawing a fourth liquid stream from the lower portion of the fractionation column; and

passing at least a portion of the third vapor stream through the first heat exchanger to cool the initial LNG stream.

19. The method of claim 18, wherein the initial LNG stream comprises nitrogen, and wherein the first vapor stream and the second vapor stream each comprise at least 60 wt % of the nitrogen present in the initial LNG stream.

20. The method of claim 18, wherein the initial LNG stream comprises nitrogen and wherein the first vapor stream and the second vapor stream each comprise at least 95 wt % of the nitrogen present in the initial LNG stream.