Improved feed processing for nitrogen rejection unit

Abstract: A system comprising a stripping column (104) and a nitrogen rejection unit (500) wherein a significant portion (300) of the feed to the nitrogen rejection unit (500) is provided at an increased pressure thus reducing product compression requirements.

Description: Technical Field This invention relates generally to the separation of nitrogen and methane by cryogenic rectification and more particularly to the cryogenic processing of the feed for the nitrogen-methane separation. Background Art One problem often encountered in the production of natural gas from underground reservoirs is nitrogen contamination. The nitrogen may be naturally occurring and/or may have been injected into the reservoir as part of an enhanced oil recovery (EOR) or enhanced gas recovery (EGR) operation. Natural gases which contain a significant amount of nitrogen may not be saleable, since they do not meet minimum heating value specifications and/or exceed maximum inert content requirements. As a result, the feed gas will generally undergo processing, wherein heavier components such as natural gas liquids are initially removed, and then the remaining stream containing primarily nitrogen and methane, and also possibly containing lower boiling or more volatile components such as helium, hydrogen and/or neon, is separated cryogenically. A common process for separation of nitrogen from natural gas employs a double column distillation cycle, similar to that used for fractionation of air into nitrogen and oxygen. A problem often encountered in the cryogenic separation of nitrogen and methane is the loss of some methane with the nitrogen overhead from the nitrogen rejection unit. This is especially the case where the nitrogen concentration in the feed is less than about 30 percent. In such situations there is less nitrogen available for reflux and thus the separation of the nitogen and methane is carried out to a lesser extent than is desirable. The problem of inadequate nitrogen reflux in a nitrogen rejection unit has been addressed by recirculating some of the nitrogen product from the separation back to the nitrogen rejection unit. Although such a system is effective in upgrading the reflux available for separation, it is disadvantageous because nitrogen which has already been separated from the nitrogen-methane mixture is returned and must be separated a second time. A process for recovering helium from a natural gas stream is known from WO 88/08948. In this process the natural gas is cooled by indirect heat exchange to condense a portion of the methane and condensable C₂ and higher hydrocarbons contained therein. The partially condensed natural gas stream then is separated to recover both a first liquid phase effluent stream comprised of a condensed portion of the methane and condensable C₂ and higher hydrocarbon compounds and a first vaporous phase comprised of helium, nitrogen and the remaining balance of the methane and condensable C₂ and higher hydrocarbon compounds. This first vaporous phase then is cooled to condense a major portion of the remaining methane and substantially all of the remaining C₂ and higher hydrocarbons. Separation of this further cooled first vaporous phase provides a second liquid phase effluent stream comprised of a condensed major portion of the remaining methane and the remaining balance of the C₂ and higher hydrocarbon compounds and a second vaporous phase comprised of helium, nitrogen and a remaining minor portion of the methane. The second vaporous phase is further cooled by indirect heat exchange, its pressure reduced and subjected to a final separation. In this final separation, a gaseous product stream comprising at least 50 volume percent of helium, the balance being substantially nitrogen, and a third liquid phase effluent stream comprising the remaining minor portion of the methane and a major portion of nitrogen individually are recovered. The process further comprises the combining of the first and second liquid phase effluent stream and the subsequent separation of said streams into a natural gas liquids stream and a residue gas stream. A recent significant advancement in the cryogenic separation of nitrogen and methane is disclosed and claimed in US-A-4 664 686. In this system a stripping column is provided upstream of the nitrogen rejection unit. The feed, containing nitrogen and methane, is partially condensed, and the partially condensed feed is phase-separated into a first vapor and a first liquid. The first liquid is passed into the stripping column to be separated into methane-richer and nitrogen-richer fractions. The first vapor and the nitrogen-richer fraction are passed as a double feed stream into the nitrogen rejection unit, wherein the first vapor stream has a pressure higher than that of the nitrogen-richer fraction and bypasses the stripping column whereas the stream of nitrogen-richer fraction is connecting the stripping column with the nitrogen rejection unit. The stripping column serves to increase the nitrogen content of the feed to the nitrogen rejection unit thus eliminating the need for nitrogen recompression and recirculation. Another advantage of this stripping column process is that a large fraction of the methane is recoverable directly from the stripping column at an elevated pressure thereby reducing subsequent compression requirements. Still another advantage of this process is that tolerance to carbon dioxide presence in the feed is improved. The stripping column of a nitrogen rejection system may have an optimum operating pressure lower than that of the feed. This reduces the pressure at which the nitrogen rejection unit can operate and thus reduces the potential pressure of its methane product. It would be desirable to have a nitrogen rejection unit which can produce higher pressure methane product and thus reduce product compression requirements. Accordingly, it is an object of this invention to provide an improved stripping column/nitrogen rejection unit wherein the nitrogen rejection unit operation is still more decoupled from the stripping column operation so that a more significant portion of the feed into the nitrogen rejection unit may be at a higher pressure and methane product from the nitrogen rejection unit may be produced at a still higher pressure than would be possible with the method and apparatus known from US-A-4 664 686. Summary Of The Invention The above and other objects which will become apparent to one skilled in the art upon a reading of this disclosure are attained by the present invention which in general involves the processing of the feed in such a way that a significant portion of the feed can bypass the stripping column and thus be directed into the nitrogen rejection unit at the higher feed pressure. In particular, one aspect of the invention is a: Method for cryogenic processing of a feed containing nitrogen and methane comprising. (A) partially condensing a feed comprising nitrogen and methane to produce a first vapor and a first liquid; (B) passing first liquid into a stripping column; (C) separating the fluids passed into the stripping column into methane-richer and nitrogen-richer fractions, at least some of the methane-richer fraction being recovered as product methane, and at least some of the nitrogen-richer fraction being passed into a nitrogen rejection unit; and (D) partially condensing first vapor characterized by (E) passing second liquid, obtained in partial condensing step (D), into the stripping column; and (F) passing second vapor, obtained in partial condensing step (D), into the nitrogen rejection unit for separation into nitrogen-enriched and methane-enriched components. Another aspect of the invention is an: Apparatus for cryogenic processing of a feed containing nitrogen and methane comprising: (A) means to partially condense feed containing nitrogen and methane to produce a first vapor and a first liquid; (B) a stripping column and means to pass first liquid into the stripping column; (C) means to partially condense the first vapor; (D) a nitrogen rejection unit; and (E) means to pass fluid from the stripping column to the nitrogen rejection unit; characterized by (F) means to pass a second liquid, produced by said first vapor partial condensing means, into the stripping column; and (G) means to pass a second vapor, produced by said first vapor partial condensing means, into the nitrogen rejection unit. The term "column" is used herein to mean a distillation, rectification or fractionation column, i.e., a contacting column or zone wherein liquid and vapor phases are counter-currently contacted to effect separation of a fluid mixture, as for example, by contacting of the vapor and liquid phases on a series of vertically spaced trays or plates mounted within the column, or on packing elements, or a combination thereof. For an expanded discussion of fractionation columns see the Chemical Engineer's Handbook, Fifth Edition, edited by R. H. Perry and C. H. Chilton, McGraw-Hill Book Company, New York Section 13, "Distillation" B. D. Smith et al, page 13-3, The Continuous Distillation Process . The term "double column", is used herein to mean high pressure column having its upper end in heat exchange relation with the lower end of a low pressure column. An expanded discussion of double columns appears in Ruheman, "The Separation of Gases" Oxford University Press, 1949, Chapter VII, Commercial Air Separation. The terms "nitrogen rejection unit" and "NRU" are used herein to mean a facility wherein nitrogen and methane are separated by cryogenic rectification, comprising a column and the attendant interconnecting equipment such as liquid pumps, phase separators, piping, valves and heat exchangers. The term "indirect heat exchange" is used herein to mean the bringing of two fluid streams into heat exchange relation without any physical contact or intermixing of the fluids with each other. As used herein the term "phase separator" means a device, such as a vessel with top and bottom outlets, used to separate a fluid mixture into its gas and liquid fractions. The term "stripping column" is used herein to mean a column where feed is introduced into the upper portion of the column and more volatile components are removed or stripped from descending liquid by rising vapor. As used herein the term "structured packing" means packing wherein individual members have specific orientation relative to each other and to the column axis. Brief Description Of The Drawing The sole Figure is a schematic flow diagram of one preferred embodiment of the improved NRU feed processing system of this invention. Detailed Description The invention will be described in detail with reference to the Drawing. Referring now to the Figure, natural gas feed 201 is partially condensed and then passed into phase separator 103. The Figure illustrates a preferred embodiment of the invention wherein natural gas feed 201 is divided into first portion 205 and second portion 202. The concentrations of nitrogen and methane in the feed may vary considerably; however generally the nitrogen concentration in the feed will be within the range of from 5 to 80 percent and the methane concentration in the feed will be within the range of from 20 to 95 percent. The feed may also contain some higher boiling hydrocarbons such as ethane although most of the higher boiling hydrocarbons will have been removed from the natural gas feed stream. The feed may also contain one or more lower boiling or more volatile components such as helium, hydrogen or neon. Generally the pressure of feed stream 201 will be within the range of from 34 to 69 bar (500 to 1000 pounds per square inch absolute (psia)), although the feed pressure may be as high as the critical pressure of the feed mixture. Both first portion 205 and second portion 202 may be partially condensed by indirect heat exchange with at least one of the nitrogen-enriched and methane-enriched components and by liquid from stripping column 104. In the embodiment illustrated in the Figure, first portion 205 is partially condensed by indirect heat exchange in heat exchanger 101 against return streams, and second portion 202 is partially condensed by indirect heat exchange in heat exchanger 102 against stripping column liquid as will be more fully described later. The resulting streams 206 and 204 are combined into stream 208 and passed into phase separator 103. Within phase separator 103 the feed is separated into first vapor having a higher nitrogen concentration, and first liquid having a higher methane concentration, than does feed 201. First liquid is passed out of separator 103 as stream 209, throttled through valve 105 and passed as stream 210 into stripping column 104 which is operating at a pressure generally within the range of from 14 to 41 bar (200 to 600 psia) and preferably within the range of from 21 to 40 bar (300 to 550 psia). First vapor is passed out of separator 103 as stream 211 and partially condensed by indirect heat exchange in heat exchanger 106 against return streams. Resulting two phase stream 212 is passed into phase separator 107 and separated into second vapor having a higher nitrogen concentration, and second liquid having a higher methane concentration than does the first vapor. Second liquid is passed out of separator 107 as stream 213, flashed across valve 108 and passed as stream 214 into stripping column 104. Preferably, as illustrated in the Figure, stream 214 is passed into stripping column 104 at a point higher than the point where stream 210 is introduced into the column. Within stripping column 104 the feeds 210 and 214 are separated into a fraction richer in nitrogen and a fraction richer in methane by the stripping of more volatile components from descending liquid into upflowing vapor. The upflowing vapor is generated by withdrawal of liquid from column 104 as stream 273 and the vaporization of some or all of that liquid by passage through heat exchanger 102 against partially condensing feed second portion 202. Resulting stream 274 is returned to column 104. The vapor portion of stream 274 provides the upflowing vapor to carry out the stripping. Methane-richer fraction is removed from column 104 as stream 275. The major portion 244 is flashed across valve 110, passed as stream 245 to heat exchanger 101, vaporized by passage through heat exchanger 101, and recovered as high pressure gas 246 generally having a methane concentration up to about 99 percent. The minor portion 399 is flashed across valve 109 and passed as stream 400 to and through heat exchanger 106 to cool and partially condense first vapor 211. In the preferred embodiment illustrated in the Figure, stream 400 is combined with methane product from the NRU to form stream 419 prior to passage through heat exchanger 106. Resulting stream 420 is passed through heat exchanger 101 and recovered as lower pressure methane gas 421. In some cases, it may be advantageous to bring out stream 400 separately at a pressure higher than stream 418 and save on methane recompression energy. Nitrogen-richer fraction is removed from column 104 as stream 280 and passed into NRU 500 for separation into nitrogen-enriched and methane-enriched components. NRU 500 may be any system capable of separating nitrogen and methane. Generally NRU 500 comprises a double column cryogenic plant or a single column cryogenic plant. Second vapor is removed from separator 107 and passed as stream 300 into NRU 500. Stream 300 is generally at about the same pressure as is feed 201 except for pressure drop due to line losses. In addition, the pressure of stream 300 exceeds the pressure of stream 280 which is generally at the operating pressure of stripping column 104. Stream 300 will generally be about 50 percent of the total feed into the NRU. In this way a significant portion of the feed into the NRU is at a higher pressure than would be the case with conventional NRU feed processing. Within NRU 500 the feeds are separated into nitrogen-enriched and methane-enriched components. Methane-enriched component is removed from NRU 500 as stream 418, preferably combined with stream 400 to produce stream 419, warmed by passage through heat exchanger 106 to effect the partial condensation of first vapor 211, passed as stream 420 through heat exchanger 101 and recovered as lower pressure methane gas product 421. Nitrogen-enriched component is removed from NRU 500 as stream 437, warmed by passage through heat exchanger 101 and removed from the system as stream 439. Nitrogen-enriched component 439 may be recovered, released to the atmosphere, or injected into an oil or gas reservoir as part of a secondary recovery operation. Because of the higher pressure at which the NRU can operate with the feed processing system of this invention, the product methane can be recovered at a higher pressure than would otherwise be the case. This reduces the product gas compression requirements which might be needed to, for example, compress methane gas to conform to pipeline requirements. Generally the system of this invention will enable a product gas compression requirement reduction of five percent or more. Although the invention has been described in detail with reference to a certain specific embodiment, those skilled in the art will recognize that there are other embodiments of this invention within the spirit of the claims.

Claims: Method for cryogenic processing of a feed containing nitrogen and methane comprising : (A) partially condensing a feed (201) comprising nitrogen and methane to produce a first vapor (211) and a first liquid (209, 210); (B) passing first liquid (209, 210) into a stripping column (104); (C) separating the fluids passed into the stripping column (104) into methane-richer and nitrogen-richer fractions (275, 280), at least some of the methane-richer fraction (275) being recovered as product methane (246), and at least some of the nitrogen-richer fraction (280) being passed into a nitrogen rejection unit (500); and (D) partially condensing first vapor (211); characterized by (E) passing second liquid (213, 214), obtained in partial condensing step (D), into the stripping column (104); and (F) passing second vapor (300), obtained in partial condensing step (D), into the nitrogen rejection unit (500) for separation into nitrogen-enriched and methane-enriched components (437, 418). The method of claim 1 wherein the second liquid (213, 214) is passed into the stripping column (104) at a point higher than the point where first liquid (209, 210) is passed into the stripping column. The method of claim 1 wherein the feed (201) is divided into first and second portions (205, 202) and each of the first and second portions are partially condensed by indirect heat exchange with at least one of the nitrogen-enriched component, methane-enriched component and liquid from the stripping column (104). The method of claim 1 wherein the first vapor (211) is partially condensed, at least in part, by indirect heat exchange with methane-enriched component (419). The method of claim 1 wherein the second vapor (300) comprises about 50 percent of the total feed into the nitrogen rejection unit (500). Apparatus for cryogenic processing of a feed containing nitrogen and methane comprising: (A) means (101, 102) to partially condense feed (201) containing nitrogen and methane to produce a first vapor (211) and a first liquid (209, 210); (B) a stripping column (104) and means to pass first liquid (209, 210) into the stripping column (104); (C) means (106) to partially condense the first vapor (211); (D) a nitrogen rejection unit (500); and (E) means to pass fluid (280) from the stripping column (104) to the nitrogen rejection unit (500); characterized by (F) means to pass a second liquid (213, 214), produced by said first vapor partial condensing means (106), into the stripping column (104); and (G) means to pass a second vapor (300), produced by said first vapor partial condensing means (106), into the nitrogen rejection unit (500). The apparatus of claim 6 wherein the means to pass second liquid (213, 214) into the stripping column (104) communicates with the stripping column at a point higher than the point where first liquid (209, 210) is passed into the stripping column. The apparatus of claim 6 further comprising means to recover fluid from the stripping column (104). The apparatus of claim 6 further comprising means to recover fluid from the nitrogen rejection unit (500). The apparatus of claim 6 wherein the nitrogen rejection unit (500) comprises a double column. The apparatus of claim 6 wherein the nitrogen rejection unit (500) comprises a single column. The apparatus of claim 6 wherein the stripping column (104) has column internals comprising structured packing. The apparatus of claim 6 wherein the nitrogen rejection unit (500) comprises at least one column and the nitrogen rejection unit has column internals comprising structured packing.

Inventors: MALONEY JAMES JOSEPH, PAHADE RAVINDRA FULCHAND, MALONEY, JAMES JOSEPH, PAHADE, RAVINDRA FULCHAND
Applicants: PRAXAIR TECHNOLOGY INC, PRAXAIR TECHNOLOGY, INC.
Application year: 1991
Main classification: F25J3
IPC codes: F25J3