Rebalancing a main heat exchanger in a process for liquefying a tube side stream

Patent metadata

Field	Value
Publication number	US-9562718-B2
Application number	US-201113637992-A
Country	US
Kind code	B2
Filing date	Mar 31, 2011
Priority date	Mar 31, 2010
Publication date	Feb 7, 2017
Grant date	Feb 7, 2017

Abstract

A process for liquefying a tube side stream in a main heat exchanger is described. The process comprises the steps of: a) providing a first mass flow to the warm end of a first subset of individual tubes, b) providing a second mass flow to the warm end of a second subset of individual tubes, c) evaporating a refrigerant stream on the shell side; d) measuring an exit temperature of the first mass flow; e) measuring an exit temperature of the second mass flow; and, f) comparing the exit temperature of the first mass flow measured in step d) to the exit temperature of the second mass flow measured in step e), the process characterized in that at least one of the first and second mass flows is adjusted to equalize the exit temperature of the first mass flow with the exit temperature of the second mass flow.

First claim

What is claimed is:

1. A process for liquefying a first tube side stream in a main heat exchanger having a warm end and a cold end, the main heat exchanger comprising a wall defining a shell side within which is arranged a coil-wound tube bundle, the process comprising:
a) introducing a first mass flow of said first tube side stream in gaseous form to a warm end of a first subset of individual tubes of said tube bundle, said first subset of individual tubes being evenly distributed radially across said tube bundle;
b) separate from said first mass flow, introducing a second mass flow of said first tube side stream in gaseous form to a warm end of a second subset of individual tubes of said tube bundle, said second subset of individual tubes being evenly distributed radially across said tube bundle;
c) evaporating a refrigerant stream on the shell side to provide cooling to said first mass flow and said second mass flow whereby said first tube side stream becomes a liquid;
d) measuring an exit temperature of said first mass flow removed as a liquid from a cold end of said first subset of individual tubes;
e) measuring an exit temperature of said second mass flow removed as a liquid from a cold end of said second subset of individual tubes; and
f) comparing the exit temperature of said first mass flow measured in step d) to the exit temperature of said second mass flow measured in step e), and adjusting at least one of the first and second mass flows to equalize the exit temperature of said first mass flow with the exit temperature of said second mass flow.

2. The process of claim 1 , wherein when the exit temperature of said first mass flow measured in d) is higher than the temperature of said second mass flow measured in e), said first mass flow is reduced compared to said second mass flow.

3. The process of claim 1 , wherein when the exit temperature of said first mass flow measured in d) is lower than the temperature of said second mass flow measured in e), said second mass flow is reduced relative to said first mass flow.

4. The process of claim 1 , wherein at least one of the first and second mass flows is adjusted to equalize the exit temperature of said first mass flow with the exit temperature of said second mass flow by adjusting at least one of the first or second mass flows at the cold end of the main heat exchanger.

5. The process of claim 1 , wherein at least one of the first and second mass flows is adjusted to equalize the exit temperature of said first mass flow with the exit temperature of said second mass flow by adjusting at least one of the first or second mass flows at the warm end of the main heat exchanger.

6. The process of claim 1 , wherein said first mass flow is adjusted by reducing the number of individual tubes in said first subset of individual tubes.

7. The process of claim 1 , wherein said first mass flow is adjusted by plugging or removing one or more individual tubes in said first subset of individual tubes.

8. The process of claim 1 , wherein said first mass flow is adjusted by restricting the first mass flow supplied to said first subset of individual tubes.

9. The process of claim 1 , wherein said second mass flow is adjusted by reducing the number of individual tubes in said second subset of individual tubes.

10. The process of claim 1 , wherein said second mass flow is adjusted by plugging or removing one or more individual tubes in said second subset of individual tubes.

11. The process of claim 1 , wherein said second mass flow is adjusted by restricting the second mass flow supplied to said second subset of individual tubes.

12. The process of claim 1 , wherein said tube bundle comprises a warm tube bundle arranged towards a warm end of said tube bundle, and a cold tube bundle arranged towards a cold end of said tube bundle, each of said warm tube bundle and said cold tube bundle having a warm end and a cold end.

13. The process of claim 12 , wherein said first tube side stream enters the warm end of said warm tube bundle as a liquid and exits the cold end of said cold tube bundle as a sub-cooled liquid.

14. The process of claim 12 , wherein said first tube side stream enters the warm end of said warm tube bundle as a gaseous, methane-rich feed which has been at least partially liquefied by the time said first tube side stream passes from the warm end of said warm tube bundle into the warm end of said cold tube bundle.

15. The process of claim 12 , wherein said first tube side stream enters the warm end of said cold tube bundle as a liquid and exits the cold end of said cold tube bundle as a sub-cooled liquid.

16. The process of claim 15 , wherein the sub-cooled liquid is removed from the cold end of said cold tube bundle of said main heat exchanger before being directed to storage.

17. The process of claim 12 , wherein said first tube side stream exchanges heat with a predominately liquid light refrigerant stream which is progressively boiled off on the shell side of said cold tube bundle.

18. The process of claim 17 , wherein evaporated refrigerant removed from a warm end of the shell side of said main heat exchanger is fed to first and second refrigerant compressors in which the evaporated refrigerant is compressed to form a high pressure refrigerant stream.

19. The process of claim 18 , wherein the high pressure refrigerant stream is directed to a heat exchanger wherein the high pressure refrigerant stream is cooled to produce a partly-condensed refrigerant stream which is then introduced into a separator to separate out a heavy refrigerant fraction in liquid form and a light refrigerant fraction in gaseous form.

20. The process of claim 19 , wherein said heavy refrigerant fraction becomes a second tube side stream which is supplied at the warm end of said warm tube bundle as a liquid and exits at the cold end of said warm tube bundle as a sub-cooled heavy refrigerant stream in liquid form.

21. The process of claim 20 , wherein the sub-cooled heavy refrigerant stream removed at the cold end of said warm tube bundle is expanded across a first expansion device to form a reduced pressure heavy refrigerant stream that is then introduced into the shell side of said main heat exchanger at a location intermediate between the cold end of said warm tube bundle and the warm end of said cold tube bundle, and wherein said reduced pressure heavy refrigerant stream is allowed to evaporate in the shell side, thereby cooling the fluids in the first and second tube side streams as they pass through said warm tube bundle.

22. The process of claim 21 , wherein part of said light refrigerant fraction from said separator becomes a third tube side stream which is introduced into the warm end of said warm tube bundle as a gas and exits at the cold end of said cold tube bundle as a sub-cooled liquid.

23. The process of claim 22 , wherein said third tube side stream is cooled from a gas to a liquid as said third tube side stream passes through said warm tube bundle and is cooled from a liquid to a sub-cooled liquid light refrigerant stream as said third tube side stream passes through said cold bundle.

24. The process of claim 23 , wherein said sub-cooled liquid light refrigerant stream removed from the cold end of said cold tube bundle is expanded through a second expansion device to cause a reduction in pressure and produce a reduced pressure light refrigerant stream.

25. The process of claim 24 , wherein

Assignees

• Hodges Derek William
• Kerber Christiane
• Steinbauer Manfred
• Hammerdinger Markus
• Linde Ag

Inventors

• Hodges Derek William
• Kerber Christiane
• Steinbauer Manfred
• Hammerdinger Markus

Classifications

• F25J2290/32

  Details on header or distribution passages of heat exchangers, e.g. of reboiler-condenser or plate heat exchangers · CPC title

• F25J2220/62

  Separating low boiling components, e.g. He, H2, N2, Air · CPC title

• F25J5/002

  for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger · CPC title

• F25J2290/60

  Details about pipelines, i.e. network, for feed or product distribution · CPC title

• F28F13/00

  Arrangements for modifying heat-transfer, e.g. increasing, decreasing (F28F1/00 - F28F11/00 take precedence) · CPC title