Cryogenic gas processing

• US 4,444,577 A
• Filed: 09/09/1982
• Issued: 04/24/1984
• Est. Priority Date: 09/09/1982
• Status: Expired due to Term

• Current Assignee: Phillips Petroleum Company (ConocoPhillips)
• Original Assignee: Phillips Petroleum Company (ConocoPhillips)
• Inventors: Perez, Ethelwolbo P.
• Primary Examiner(s): Sever, Frank
• Application Number:
  US06/416,202
• Time in Patent Office: 593 Days
• Field of Search: 62/38, 62/39, 62/9, 62/11, 62/23, 62/24, 62/27-29, 62/31, 62/32, 62/34, 62/42, 62/30, 55/27, 55/68
• US Class Current: 62/622
• CPC Class Codes: C07C 7/005 Processes comprising at least two steps in series
• CPC Class Codes: F25J 2200/02 in a single pressure main column system
• CPC Class Codes: F25J 2200/74 Refluxing the column with at least a part of the partially condensed overhead gas
• CPC Class Codes: F25J 2205/04 in the feed line, i.e. upstream of the fractionation step
• CPC Class Codes: F25J 2210/06 Splitting of the feed stream, e.g. for treating or cooling in different ways
• CPC Class Codes: F25J 2215/02 Mixing or blending of fluids to yield a certain product
• CPC Class Codes: F25J 2220/66 Separating acid gases, e.g. CO2, SO2, H2S or RSH
• 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 2240/40 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 2270/04 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 3/0209 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

Abstract

Higher boiling constituents are separated from a normally gaseous feed mixture, predominating in lower boiling constituents and containing significant amounts of such higher boiling constituents, such as natural gas by fractionally distilling a feed mixture having a temperature substantially below atmospheric temperature at a pressure substantially above atmospheric pressure at which temperature and pressure the feed mixture comprises both vapor and liquid phases to produce a first vapor phase substantially enriched in lower boiling constituents and a first liquid phase substantially enriched in higher boiling constituents, expanding at least a part of the first vapor phase to reduce the pressure and temperature and produce an expanded fluid stream comprising a second vapor phase and a second liquid phase, separating the second vapor phase from the second liquid phase, recycling the second liquid phase to the fractional distillation step as a reflux, recovering the second vapor phase as a product and recovering the first liquid phase as a product. In another embodiment, at least a part of the feed mixture is expanded prior to fractional distillation. In other embodiments, the feed mixture is separated into a vapor phase and a liquid phase and at least a part of the vapor phase is expanded and/or the feed mixture is first cooled by indirect heat exchange with the second vapor phase prior to recovery of the latter as a product.

Claims

1. A method for separating ethane and higher molecular weight hydrocarbons from a natural gas feed, predominating in methane and containing significant amounts of ethane and higher molecular weight hydrocarbons and carbon dioxide, having a first pressure substantially above atmospheric pressure and a first temperature substantially below atmospheric temperature and at which first pressure and first temperature said feed comprises both vapor and liquid phases, comprising:

(a) separating said feed, in a separation zone, to separate the vapor phase of said feed, as a first vapor phase, and the liquid phase of said feed, as a first liquid phase;

(b) expanding at least a part of said first vapor phase to reduce the pressure thereof to a second lower pressure and reduce the temperature thereof to a second lower temperature and produce a first expanded fluid stream;

(c) fractionally distilling said first expanded fluid stream, any unexpanded remaining portion of said first vapor phase and said first liquid phase, in a fractionation zone, to produce a second vapor phase, significantly enriched in methane and carbon dioxide, and a second liquid phase, predominating in ethane and higher molecular weight hydrocarbons and containing insignificant amounts of methane;

(d) expanding at least a portion of said second vapor phase to reduce the pressure thereof to a third lower pressure and reduce the temperature thereof to a third lower temperature and produce a second expanded fluid stream, as a third vapor phase, predominating in methane, significantly enriched in carbon dioxide and containing insignificant amounts of ethane in higher molecular weight hydrocarbons, and a third liquid phase;

(e) separating said second expanded fluid stream, in a separation zone, to separate said third vapor phase and said third liquid phase;

(f) recycling said third liquid phase to said fractionation zone, as a reflux;

(g) recovering said third vapor phase as a product; and

(h) recovering said second liquid phase as a product;

(i) maintaining the temperature and pressure at all times throughout the process substantially within the liquid range of carbon dioxide.

2. A method in accordance with claim 1 wherein the pressure of the third vapor phase is controlled by withdrawing a portion of the feed, in accordance with the pressure of said feed, and adding thus withdrawn portion of the feed to the product third vapor phase.

3. A method in accordance with claim 1 wherein the fractionation zone comprises and upper rectifying section and a lower stripping section.

4. A method in accordance with claim 3 wherein the feed is introduced into the fractionation zone at a point at least as low as the top of the stripping section and the third liquid phase is recycled to the rectifying section of said fractionation zone.

5. A method in accordance with claim 3 wherein the expanded portion of the first vapor phase and any unexpanded remaining portion of the first vapor phase is introduced to the fractionation zone between the rectifying section and the stripping section and the first liquid phase is introduced into the upper portion of said stripping section below the point of introduction of said expanded frist vapor phase and any unexpanded remaining portion of said first vapor phase.

6. A method in accordance with claim 1 wherein the volume of the first vapor phase thus expanded is controlled in accordance with the pressure of said first vapor phase.

7. A method in accordance with claim 1 wherein the volume of the second vapor phase thus expanded is controlled in accordance with he pressure of said second vapor phase.

8. A method in accordance with claim 1 wherein the bottom of the fractionation zone is heated, at least in part, by withdrawing a side stream adjacent the bottom of said fractionation zone, passing the thus withdrawn side stream in indirect heat exchange with a portion of the feed and returning the thus withdrawn and heated side stream to said fractionation zone at a point below the point of withdrawal.

9. A method in accordance with claim 8 wherein the volume of the feed thus heat exchanged with the side stream withdrawn from the fractionation zone is controlled in accordance with the temperature of said feed.

10. A method in accordance with claim 1 or 8 wherein a lower intermediate portion of the fractionation zone is heated, at least in part, by withdrawing a second side stream from said lower intermediate portion of said fractionation zone, passing the thus withdrawn second side stream in indirect heat exchange with a portion of the feed and returning the thus withdrawn and heated second side stream to said lower intermediate portion of said fractionation zone at a point below the point of withdrawal.

11. A method in accordance with claim 1 or 8 wherein a portion of the first liquid phase is heated prior to fractionally distilling the same by withdrawing a portion of said first liquid phase, passing the thus withdrawn portion of said first liquid phase in indirect heat exchange with a portion of said feed and passing the thus withdrawn and heated portion of said first liquid phase to the fractionation zone.

12. A method in accordance with claim 1 wherein at least a portion of the first vapor phase is thus expanded by passing the same through a first expansion section of a first expander-compressor, the compression section of said first expander-compressor is driven by said first expansion section, the third vapor phase is thus expanded by passing the same through a second expansion section of a second expander-compressor, the second compression section of said second expander-compressor is driven by said second expansion section and at least a part of the fourth vapor phase is compressed in at least one of said first compression section and said second compression section.

13. A method for separating ethane and higher molecular weight hydrocarbons from a natural gas feed, predominating in methane and containing significant amounts of ethane and higher molecular weight hydrocarbons and carbon dioxide, having a first pressure substantially above atmospheric pressure and a first temperature near atmospheric temperature, comprising:

(a) cooling said feed to reduce the temperature thereof to a second lower temperature substantially below atmospheric temperature and at which first pressure and second temperature said feed comprises both vapor and liquid phases;

(b) separating the thus cooled feed, in a separation zone, to separate the vapor phase of said feed, as a first vapor phase, and the liquid phase of said feed, as a first liquid phase;

(c) expanding at least a portion of said first vapor phase to reduce the pressure thereof to a second lower pressure and reduce the temperature thereof to a third lower temperature and produce a first expanded fluid stream;

(d) fractionally distilling said first expanded fluid stream, any unexpanded remaining portion of said first vapor phase and said first liquid phase, in a fractionation zone, to produce a second vapor phase, significantly enriched in methane and carbon dioxide, and a second liquid phase, predominating in ethane and higher molecular weight hydrocarbons and containing insignificant amounts of methane;

(e) expanding at least a portion of said second vapor phase to reduce the pressure thereof to a third lower pressure and reduce the temperature thereof to a fourth lower temperature and produce a second expanded fluid stream, as a third vapor phase, predominating in methane, significantly enriched in carbon dioxide and containing insignificant amounts of ethane and higher molecular weight hydrocarbons, and a third liquid phase;

(f) separating said second expanded fluid stream, in a separation zone, to separate said third vapor phase and said third liquid phase;

(g) recycling said third vapor phase to said fractionation zone, as a reflux;

(h) recovering said third vapor phase as a product; and

(i) recovering said second liquid phase as a product;

(j) maintaining the temperature and pressure at all times throughout the process substantially within the liquid range of carbon dioxide.

14. A method in accordance with claim 13 wherein the pressure of the third vapor phase is controlled by withdrawing a portion of the feed and adding the thus withdrawn portion of the feed to said third vapor phase in accordance with the pressure of said feed.

15. A method in accordance with claim 13 wherein the fractionation zone comprises an upper rectifying section and a lower stripping section.

16. A method in accordance with claim 15 wherein the feed is introduced into the fractionation zone at a point at least as low as the top of the stripping section and the third liquid phase is recycled to the rectifying section of the fractionation zone.

17. A method in accordance with claim 15 wherein the expanded first vapor phase of the feed and the unexpanded remaining portion of the first vapor phase of the feed is introduced to the fractionation zone between the rectifying section and the stripping section and the first liquid phase of the feed is introduced into the upper portion of the stripping section below the point of introduction of said expanded first vapor phase and said unexpanded remaining portion of said first vapor phase.

18. A method in accordance with claim 13 wherein the volume of the first vapor phase thus expanded is controlled in accordance with the pressure of said first vapor phase.

19. A method in accordance with claim 13 wherein the volume of the second vapor phase thus expanded is controlled in accordance with the pressure of said second vapor phase.

20. A method in accordance with claim 13 wherein the bottom of the fractionation zone is heated, at least in part, by withdrawing a side stream adjacent the bottom of said fractionation zone, passing the thus withdrawn side stream in indirect heat exchange with an uncooled portion of the feed and returning the thus withdrawn and heated side stream to the fractionation zone at a point below the point of withdrawal.

21. A method in accordance with claim 13 or 20 wherein a lower intermediate portion of the fractionation zone is heated, at least in part, by withdrawing a second side stream from said lower intermediate portion of said fractionation zone, passing the thus withdrawn second side stream in indirect heat exchange with an uncooled portion of the feed and returning the thus withdrawn and heated second side stream to said lower intermediate portion of said fractionation zone at a point below the point of withdrawal.

22. A method in accordance with claim 20 wherein the volume of feed thus used to heat the side stream from the fractionation zone is controlled in accordance with the temperature of said feed.

23. A method in accordance with claim 13 or 20 wherein a portion of the first liquid phase is heated prior to fractionally distilling the same by withdrawing a portion of said first liquid phase, passing the thus withdrawn portion of said first liquid phase in indirect heat exchange with an uncooled portion of said feed and passing the thus withdrawn and heated portion of said first liquid phase to the fractionation zone.

24. A method in accordance with claim 13 wherein the at least a portion of the first vapor phase is thus expanded by passing the same through a first expansion section of a first expander-compressor, the compression section of said first expander-compressor is driven by said first expansion section, the third vapor phase is thus expanded by passing the same through a second expansion section of a second expander-compressor, the second compression section of said second expander-compressor is driven by said second expansion section and at least part of the fourth vapor phase is compressed in at least one of said first compression section and said second compression section.

25. A method in accordance with claim 13 wherein the feed is cooled, at least in part, by indirect heat exchange with at least a portion of the third vapor phase.