ETHANE RECOVERY OR ETHANE REJECTION OPERATION

• US 20180266760A1
• Filed: 05/24/2018
• Published: 09/20/2018
• Est. Priority Date: 01/05/2016
• Status: Active Grant

• Current Assignee: Fluor Technologies Corporation (Fluor Corporation)
• Original Assignee: Fluor Technologies Corporation (Fluor Corporation)
• Inventors: MAK, John
• Granted Patent: US 10,704,832 B2
• Time in Patent Office: Days
• 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 2200/78 Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
• CPC Class Codes: F25J 2205/04 in the feed line, i.e. upstream of the fractionation step
• CPC Class Codes: F25J 2235/60 the fluid being (a mixture of) hydrocarbons
• CPC Class Codes: F25J 2240/40 Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
• CPC Class Codes: F25J 2245/02 Recycle of a stream in general, e.g. a by-pass stream
• CPC Class Codes: F25J 2270/90 External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
• CPC Class Codes: F25J 2280/02 Control in general, load changes, different modes ("runs"), measurements
• CPC Class Codes: F25J 2290/40 Vertical layout or arrangement of cold equipments within in the cold box, e.g. columns, condensers, heat exchangers etc.
• 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 3/0238 separation of CnHm with 2 carbon atoms or more
• CPC Class Codes: F25J 3/0242 separation of CnHm with 3 carbon atoms or more
• CPC Class Codes: F25J 3/0615 Liquefied natural gas
• CPC Class Codes: F25J 3/064 separation of CnHm with 2 carbon atoms or more
• CPC Class Codes: F25J 3/0695 Start-up or control of the process; Details of the apparatus used

Abstract

A method for operating a natural gas liquids processing (NGL) system, the system being selectively configured in either an ethane rejection configuration or an ethane recovery configuration, the method comprising, when the NGL system is in the ethane rejection configuration, collecting a reboiler bottom stream that, in the ethane rejection configuration, includes ethane in an amount of less than 5% by volume, and when the NGL system is in the ethane recovery configuration, collecting a reboiler bottom stream that, in the ethane recovery configuration, includes ethane in an amount of at least about 30% by volume.

Claims

1. A natural gas liquids processing system configured to flexibly operate in ethane rejection or ethane recovery, comprising:

a first heat exchanger configured to chill a feed gas stream to form a chilled feed gas stream;

a separator configured to separate the chilled feed gas stream into a vapor stream and a liquid stream;

an absorber column configured to produce an absorber bottom stream and an absorber overhead stream; and

a stripper column coupled to the liquid stream and configured to receive the absorber bottom stream and to produce a stripper bottom stream and a stripper overhead stream;

wherein the vapor stream is coupled to a top of the absorber column and to a bottom of the absorber column;

wherein the stripper overhead stream is coupled to the top of the absorber column and to the bottom of the absorber column;

wherein the system is configured, during ethane rejection, to direct the stripper overhead stream to the top of the absorber column and to direct the vapor stream to the bottom of the absorber column;

wherein the system is configured, during ethane recovery, to direct the vapor stream the top of the absorber column and to direct the stripper overhead stream to the bottom of the absorber column.

2. The system of claim 1, further comprising:

a valve coupled between the first heat exchanger and the absorber column and configured to;

during ethane rejection, reduce a pressure of the stripper overhead stream so that the stripper overhead stream enters the absorber column as a two-phase reflux stream; and

during ethane recovery, reduce a pressure of the vapor stream so that the vapor stream enters the absorber column as a liquid.

3. The system of claim 2, wherein the first heat exchanger is further configured to:

during ethane rejection, chill the stripper overhead stream and heat the liquid stream in the first heat exchanger; and

during ethane recovery, chill the vapor stream in the first heat exchanger.

4. The system of claim 1, wherein the separator is a lower portion of an integrated separator column, the stripper column is an intermediate portion of the integrated separator column, and the absorber column is an upper portion of an integrated separator column.

5. The system of claim 4, further comprising:

a first isolation barrier placed in the integrated separator column and configured to prevent fluid flow between the separator and the stripper column within the integrated separator column; and

a second isolation barrier placed in the integrated separator column and configured to prevent fluid flow between the stripper column and the absorber column within the integrated separator column.

6. The system of claim 1, further comprising:

a compressor;

a second heat exchanger; and

an air cooler;

wherein the first heat exchanger is configured to heat the absorber overhead stream to form a heated residue gas stream;

wherein the compressor is configured to compress the heated residue gas stream to form a compressed residue gas stream;

wherein the second heat exchanger is configured to cool the compressed residue gas stream to form a cooled compressed residue gas stream;

wherein the air cooler is configured to cool the cooled compressed residue gas stream to form a sales gas stream.

7. The system of claim 6, further comprising:

a reboiler configured to heat the stripper bottom stream to form a reboiler overhead stream and a reboiler bottom stream; and

a third heat exchanger configured to cool the boiler bottom stream to form an NGL product stream.

8. The system of claim 7, wherein, during ethane rejection, the sales gas stream comprises 90 to 99% of the ethane recovered from the feed gas stream and the NGL product stream comprises 90 to 99% of the propane and heavier hydrocarbons recovered from the feed gas stream.

9. The system of claim 7, wherein, during ethane recovery, the NGL product stream comprises 50 to 70% of the ethane recovered from the feed gas stream.

10. The system of claim 1, further comprising:

a first plurality of valves placed in the stripper overhead stream and configured to;

during ethane rejection, direct the stripper overhead stream to the top of the absorber column; and

during ethane recovery, direct the stripper overhead stream to the bottom of the absorber column.

11. The system of claim 10, further comprising:

a second plurality of valves paced in the vapor stream and configured to;

during ethane rejection, direct the vapor stream to the bottom of the absorber column; and

during ethane recovery, direct the vapor stream the top of the absorber column.

12. A method of flexibly operating a natural gas liquids processing system in ethane rejection or ethane recovery, comprising:

chilling a feed gas stream to form a chilled feed gas stream;

separating the chilled feed gas stream into a vapor stream and a liquid stream;

receiving, by an absorber column, the vapor stream and a stripper overhead stream;

producing, by the absorber column, an absorber overhead stream and an absorber bottom stream;

receiving, by a stripper column, the liquid stream and the absorber bottom stream;

producing, by the stripper column, the stripper overhead stream and a stripper bottom stream;

during ethane rejection;

directing the stripper overhead stream to the top of the absorber column;

directing the vapor stream to a bottom of the absorber column; and

during ethane recovery;

directing the vapor stream the top of the absorber column;

directing the stripper overhead stream to the bottom of the absorber column.

13. The method of claim 12, wherein the vapor stream is coupled to a top of the absorber column and to a bottom of the absorber column;

wherein the stripper overhead stream is coupled to the top of the absorber column and to the bottom of the absorber column;

14. The method of claim 12, further comprising:

during ethane rejection, reducing a pressure of the stripper overhead stream so that the stripper overhead stream enters the absorber column as a two-phase reflux stream; and

during ethane recovery, reducing a pressure of the vapor stream so that the vapor stream enters the absorber column as a liquid.

15. The method of claim 14, further comprising:

during ethane rejection, chilling the stripper overhead stream and heating the liquid stream; and

during ethane recovery, chilling the vapor stream.

16. The method of claim 12, wherein the separator is a lower portion of an integrated separator column, the stripper column is an intermediate portion of the integrated separator column, and the absorber column is an upper portion of an integrated separator column.

17. The method of claim 12, further comprising:

heating the absorber overhead stream to form a heated residue gas stream;

compressing the heated residue gas stream to form a compressed residue gas stream;

cooling the compressed residue gas stream to form a cooled compressed residue gas stream;

cooling the cooled compressed residue gas stream to form a sales gas stream;

heating the stripper bottom stream to form a reboiler overhead stream and a reboiler bottom stream; and

cooling the boiler bottom stream to form an NGL product stream.

18. The method of claim 17, wherein:

during ethane rejection, the sales gas stream comprises 90 to 99% of the ethane recovered from the feed gas stream and the NGL product stream comprises 90 to 99% of the propane and heavier hydrocarbons recovered from the feed gas stream; and

during ethane recovery, the NGL product stream comprises 50 to 70% of the ethane recovered from the feed gas stream.

19. The method of claim 12, further comprising:

directing, by a first plurality of valves during ethane rejection, the stripper overhead stream to the top of the absorber column; and

directing, by the first plurality of valves during ethane recovery, the stripper overhead stream to the bottom of the absorber column.

20. The method of claim 19, further comprising:

directing, by a second plurality of valves during ethane rejection, the vapor stream to the bottom of the absorber column; and

directing, by the second plurality of valves during ethane recovery, the vapor stream the top of the absorber column.