Recovery of NGL's and rejection of N.sub.2 from natural gas

• US 4,746,342 A
• Filed: 07/10/1987
• Issued: 05/24/1988
• Est. Priority Date: 11/27/1985
• Status: Expired due to Term

• Current Assignee: Phillips Petroleum Company (ConocoPhillips)
• Original Assignee: Phillips Petroleum Company (ConocoPhillips)
• Inventors: Gray, Michael L., DeLong, Bradley W.
• Primary Examiner(s): Capossela, Ronald C.
• Application Number:
  US07/071,839
• Time in Patent Office: 319 Days
• Field of Search: 62/24, 62/27, 62/32, 62/34, 62/36, 62/38, 62/39, 62/42
• US Class Current: 62/622
• 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 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 2230/30 Compression of the feed stream
• 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 2245/02 Recycle of a stream in general, e.g. a by-pass stream
• 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 2270/88 Quasi-closed internal refrigeration or heat pump cycle, if not otherwise provided
• 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 3/0257 separation of nitrogen from air F25J3/04, production of nitrogen in general C01B21/00
• CPC Class Codes: Y10S 62/927 Natural gas from nitrogen

Abstract

A super-pressured, sub-cooled feed gas, predominating in methane and containing significant amounts of ethane and higher hydrocarbons and nitrogen, is separated by passing the feed gas through at least one separation step to separate a vapor phase and a liquid phase, fractionating the liquid phase to recover ethane and higher hydrocarbons as a liquid and a pipeline gas as a vapor phase product, the vapor phase from the separation step is then sequentially fractionated in second, third and fourth fractionation steps to produce liquid phase from the second fractionation step, which is recycled to the first fractionation step as a reflux, a liquid phase from the third fractionation step which is recovered as a product pipeline gas, a liquid phase from the fourth fractionation step which is recovered as an in-plant fuel and a vapor phase from the fourth fractionation step which is vented to the atmosphere as substantially pure nitrogen. The vapor phase from the first fractionation step and the liquid phases from the third and fourth fractionation step and the vapor from the fourth fractionation step are passed in indirect heat exchange with portions of the feed gas to cool the same and portions of the vapor phase from the separation step, the second fractionation step and the third fractionation step are utilized in reboilers to heat the second, third and fourth fractionation steps.

Claims

1. A method of separating a super-pressured sub-cooled feed gas, predominating in methane and containing significant amounts of ethane and higher hydrocarbons and nitrogen, said feed gas being at a pressure substantially above atmospheric pressure and a temperature substantially below atmospheric temperature sufficient to form a vapor phase and liquid phase, comprising:

(a) separating said feed gas, in at least one separation step, to produce a methane- and nitrogen-enriched first vapor phase and an ethane and higher hydrocarbon-enriched first liquid phase;

(b) fractionating said first liquid phase, in a first fractionation zone, under conditions sufficient to produce a product, methane-enriched, second vapor phase and a product, ethane and higher hydrocarbon-enriched, second liquid phase;

(c) fractionating said first vapor phase, in a second fractionation zone, under conditions sufficient to produce a nitrogen-enriched, third vapor phase and a methane-enriched, third liquid phase; and

(d) fractionating said third vapor phase, in a third fractionation zone, under conditions sufficient to produce a product, nitrogen-enriched, fourth vapor phase and a product, methane-enriched fourth liquid phase.

2. A method in accordance with claim 1 wherein said third liquid phase is introduced into said first fractionation zone as a reflux therefor.

3. A method in accordance with claim 2 wherein said third liquid phase is passed in indirect heat exchange with said first vapor phase before said third liquid phase is thus introduced into said first fractionation zone as reflux therefor.

4. A method in accordance with claim 3 wherein:

(a) said fourth vapor phase and said fourth liquid phase are passed in indirect heat exchange with said third vapor phase; and

(b) said fourth vapor phase, said fourth liquid phase and said second vapor phase are passed in indirect heat exchange with said first vapor phase and thereafter with said feed gas to cool said third vapor phase, said first vapor phase and said feed gas.

5. A method in accordance with claim 1 wherein:

(a) said fourth vapor phase and said fourth liquid phase are passed in indirect heat exchange with said third vapor phase; and

(b) said fourth vapor phase, said fourth liquid phase and said second vapor phase are passed in indirect heat exchange with said first vapor phase and thereafter with said feed gas to cool said third vapor phase, said first vapor phase and said feed gas.

6. A method in accordance with claim 1 wherein prior to separating said feed gas, said feed gas is compressed in at least one compression stage, a portion of said feed gas is thereafter withdrawn, the thus withdrawn portion of said feed gas is passed through at least one expansion stage where it is reduced in pressure by an amount sufficient to significantly reduce the temperature thereof, the thus expanded withdrawn portion of said feed gas, whose temperature has been reduced, is passed in indirect heat exchange with said feed gas in at least one cooling stage, to further cool said feed gas, and then said expanded withdrawn portion of said feed gas, which has thus been passed in indirect heat exchange with said feed gas, is recycled and recombined with said feed gas prior to said at least one compression stage.

7. A method in accordance with claim 6 wherein:

(a) said fourth liquid phase and said fourth vapor phase are passed in indirect heat exchange with said third vapor phase;

(b) said fourth liquid phase, said fourth vapor phase and said second vapor phase are passed in indirect heat exchange with said first vapor phase; and

(c) said fourth liquid phase, said fourth vapor phase, said second vapor phase and said expanded withdrawn portion of said feed gas are passed in indirect heat exchange with said feed gas to cool said third vapor phase, said first vapor phase and said feed gas.

8. A method in accordance with claim 6 whereby energy is produced in said at least one expansion stage and said energy is applied to said at least one compression stage, to provide at least part of the energy consumed in said at least one compression stage.

9. A method in accordance with claim 8 wherein said feed gas is cooled in a first cooling stage and thereafter a second cooling stage by passing in indirect heat exchange the thus expanded said withdrawn portion of said feed gas through said second cooling stage and thereafter said first cooling stage.

10. A method in accordance with claim 9 wherein:

(a) said fourth liquid phase and said fourth vapor phase are passed in indirect heat exchange with said third vapor phase;

(b) said fourth liquid phase, said fourth vapor phase and said second vapor phase are passed in indirect heat exchange with said first vapor phase; and

(c) said fourth liquid phase, said fourth vapor phase, said second vapor phase and said expanded withdrawn portion of said feed gas are passed through said second cooling stage and thereafter through said first cooling stage in indirect heat exchange with said feed gas to cool said third vapor phase, said first vapor phase and said feed gas.

11. A method in accordance with claim 9 wherein said feed gas is passed in indirect heat exchange through said first cooling stage and thereafter with fluids in said first fractionation zone and thereafter through said second cooling stage.

12. A method in accordance with claim 6 wherein said fourth vapor phase is fractionated in a fourth fractionation zone, under conditions sufficient to produce a product, fifth vapor phase, further enriched in nitrogen and a product, fifth liquid phase further enriched in methane.

13. A method in accordance with claim 12 wherein:

(a) said fifth liquid phase and said fifth vapor phase are passed in indirect heat exchange with said fourth vapor phase;

(b) said fifth liquid phase, said fifth vapor phase and said fourth liquid phase are passed in indirect heat exhange with said third vapor phase;

(c) said fifth liquid phase, said fifth vapor phase, said fourth liquid phase and said second vapor phase are passed in indirect heat exchange with said first vapor phase; and

(d) said fifth liquid phase, said fifth vapor phase, said fourth liquid phase, said second vapor phase and said expanded withdrawn portion of said feed gas are passed in indirect heat exchange with said feed gas.