System and process for liquefying high pressure natural gas

• US 6,367,286 B1
• Filed: 11/01/2000
• Issued: 04/09/2002
• Est. Priority Date: 11/01/2000
• Status: Expired due to Term

• Current Assignee: Black & Veatch International Company (Black & Veatch Corporation)
• Original Assignee: Black & Veatch Pritchard Incorporated
• Inventors: Price, Brian C.
• Primary Examiner(s): Doerrler, William
• Assistant Examiner(s): Drake, Malik N.
• Application Number:
  US09/704,064
• Time in Patent Office: 524 Days
• Field of Search: 626/13, 626/20, 626/21, 626/22
• US Class Current: 62/613
• CPC Class Codes: F25J 1/0022 Hydrocarbons, e.g. natural gas
• CPC Class Codes: F25J 1/0035 by gas expansion with extraction of work
• CPC Class Codes: F25J 1/0052 by vaporising a liquid refrigerant stream
• CPC Class Codes: F25J 1/0212 as a single flow MCR cycle
• CPC Class Codes: F25J 2200/04 in a dual pressure main column system
• 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 2200/72 Refluxing the column with at least a part of the totally condensed overhead gas
• CPC Class Codes: F25J 2205/04 in the feed line, i.e. upstream of the fractionation step
• CPC Class Codes: F25J 2230/20 Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
• CPC Class Codes: F25J 2230/22 Compressor driver arrangement, e.g. power supply by motor, gas or steam turbine
• CPC Class Codes: F25J 2230/60 the fluid being hydrocarbons or a mixture of hydrocarbons
• CPC Class Codes: F25J 2235/60 the fluid being (a mixture of) hydrocarbons
• 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 2245/02 Recycle of a stream in general, e.g. a by-pass stream
• CPC Class Codes: F25J 2270/12 External refrigeration with liquid vaporising loop
• CPC Class Codes: F25J 2270/66 Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
• 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

Abstract

A system and a method for efficiently removing natural gas liquids from a natural gas stream at an elevated pressure and liquefying the natural gas stream at an elevated pressure by use of a turbo expander and a compressor.

Claims

1. A process for liquefying a natural gas stream having a pressure greater than about 500 psig in a mixed refrigerant process to produce a liquefied natural gas product, the method comprising:

a) cooling the natural gas stream in a heat exchanger in the mixed refrigerant process to a first temperature less than about −

40_F. to produce a cooled natural gas stream;

b) passing the cooled natural gas stream to a liquids separation zone to produce a first gas stream and a first liquids stream;

c) passing the first liquids stream to a methane separation tower at a temperature less than about −

40°

F. and at a pressure less than about 650 psig to produce a second gas stream comprising methane and a second liquids stream containing natural gas liquids;

d) passing the first gas stream to a turbo expander to reduce the pressure of the first gas stream to a pressure less than about 650 psig to produce a reduced pressure gas stream and passing the reduced pressure gas stream to the methane separation vessel;

e) driving a compressor with the turbo expander;

f) passing the second gas stream to the compressor and compressing the second gas stream to a pressure of at least about 500 psig to produce a compressed gas stream; and

,

g) passing the compressed gas stream to the heat exchanger for liquefaction at a pressure of at least about 500 psig to produce the liquefied natural gas.

2. The method of claim 1 wherein the first temperature is from about −

40 to about −

120°

F.

3. The method of claim 1 wherein the first liquids stream is passed to the methane separation tower at a temperature from about −

40 to about −

120°

F.

4. The method of claim 1 wherein the methane separation tower has an overhead temperature from about −

100 to about −

150°

F. and operatesat a pressure less than about 650 psig.

5. The method of claim 1 wherein the second liquid stream is passed to a fractionator to produce a third gas stream and a stream comprising natural gas liquids.

6. The method of claim 5 wherein the third gas stream is cooled, liquefied and pumped to combination with the compressed gas stream.

7. The method of claim 1 wherein the compressor is also driven by a motor.

8. The method of claim 1 wherein the reduced pressure gas stream is passed to a second separation zone to produce a third gas stream and a third liquid stream with the third gas stream being passed to the compressor and the third liquid stream being passed to the methane separation tower.

9. A process for liquefying a natural gas stream having a pressure greater than about 500 psig in a natural gas liquefaction process to produce a liquefied natural gas product, the process comprising:

a) cooling the natural gas stream in a heat exchanger in the natural gas liquefaction process to a first temperature less than about −

40°

F. to produce a cooled natural gas stream;

b) passing the cooled natural gas stream to a liquids separation zone to produce a first gas stream and a first liquids stream;

c) passing the first liquids stream to a methane separation tower at a temperature less than about −

40°

F. and at a pressure less than about 650 psig to produce a second gas stream comprising methane and a second liquids stream containing natural gas liquids;

d) passing the first gas stream to a turbo expander to reduce the pressure of the first gas stream to a pressure less than about 650 psig to produce a reduced pressure gas stream and passing the reduced pressure gas stream to the methane separation tower;

e) driving a compressor with the turbo expander;

f) passing the second gas stream to the compressor and compressing the second gas stream to a pressure of at least about 500 psig to produce a compressed gas stream; and

,

g) passing the compressed gas stream to the heat exchanger for liquefaction at a pressure of at least about 500 psig to produce the liquefied natural gas.

10. The method of claim 9 wherein the first temperature is from about −

40 to about −

120°

F.

11. The method of claim 9 wherein the first liquids stream is passed to the methane separator at a temperature from about −

40 to about −

120°

F.

12. The method of claim 9 wherein the methane separator is at a temperature from about −

100 to about −

120°

F. and at a pressure less than about 650 psig.

13. The method of claim 9 wherein the second liquid stream is passed to a fractionator to produce a third gas stream and a stream comprising natural gas liquids.

14. The method of claim 13 wherein the third gas stream is cooled, liquefied and pumped to combination with the compressed gas stream.

15. The method of claim 9 wherein the compressor is also driven by a motor.

16. The method of claim 9 wherein the reduced pressure gas stream is passed to a second separative zone to produce a third gas stream and a third liquid stream with the third gas stream being passed to the compressor and the third liquid stream being passed to the methane separation tower.

17. A system for liquefying a natural gas stream having a pressure greater than about 500 psig, the system comprising:

a) a refrigeration unit adapted to cool the natural gas to a temperature sufficient to liquefy at least a major portion of the natural gas, the refrigeration unit having an intermediate gas outlet, an intermediate gas inlet and a product liquefied natural gas outlet;

b) a separator in fluid communication with the intermediate gas outlet and having a gas outlet and a liquids outlet;

c) a methane separator tower in fluid communication with the liquids outlet and having an overhead gas outlet, a bottom liquid outlet and a gas inlet;

d) a turbo expander in fluid communication with the gas outlet from the separator and the gas inlet to the methane separator tower; and

,

e) a compressor driven by the turbo expander and in fluid communication with the overhead gas outlet and having a compressed gas outlet in fluid communication with the intermediate gas inlet.

18. The system of claim 17 wherein the system further comprises a fractionator in fluid communication with the bottom liquid outlet and having a separated gas outlet and a natural gas liquids outlet.

19. The system of claim 18 wherein the separated gas outlet is in fluid communication via a heat exchanger, a pump and a line with the intermediate gas inlet.

20. The system of claim 17 wherein the refrigeration unit comprises a plurality of heat exchange zones.

21. A process for efficiently separating natural gas liquids from a natural gas stream at a pressure greater than about 500 psig to produce a high pressure gas stream and a natural gas liquids stream, the process comprising:

a) cooling the natural gas stream to a first temperature less than about −

40°

F. to produce a cooled natural gas stream;

b) passing the cooled natural gas stream to a liquids separation zone to produce a first gas stream and a first liquids stream;

c) passing the first liquids stream to a methane separation vessel at a temperature less than about −

40°

F. and at a pressure less than about 650 psig to produce a second gas stream comprising methane and a second liquids stream containing natural gas liquids;

d) passing the first gas stream to a turbo expander to reduce the pressure of the first gas stream to a pressure less than about 650 psig to produce a reduced pressure gas stream and passing the reduced pressure gas stream to the methane separation tower;

e) driving a compressor with the turbo expander; and

,

f) passing the second gas stream to the compressor and compressing the second gas stream to produce a high pressure compressed gas stream.

22. The process of claim 21 wherein the second liquid stream is passed to a fractionator to produce a third gas stream and a stream comprising natural gas liquids.

23. The method of claim 21 wherein the reduced pressure gas stream is passed to a second separation zone to produce a third gas stream and a third liquid stream with the third gas stream being passed to the compressor and the third liquid stream being passed to the methane separation tower.