US4456461A
Expired / Lapsed
US
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Separation of low boiling constituents from a mixed gas
Assignee: Phillips Petroleum Co
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Filing: 1982-09-09
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Granted: 1984-06-26
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Expires: 2002-09-09
Abstract
Abstract Lower boiling constituents are separated from a normally gaseous feed mixture predominating in higher boiling constituents and containing significant amounts of such lower boiling constituents and 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 mixture includes both vapor and liquid phases, including introducing at least a portion of the vapor of the feed mixture representing a second vapor phase into a separation contacting zone adjacent the top thereof at a second pressure substantially lower than the first pressure and a second temperature substantially lower than the first temperature and introducing at least a portion of the liquid of the feed mixture representing a second liquid phase into the separation-contacting zone at a lower intermediate point at a third pressure and a third temperature approximately equal to the first pressure and the first temperature, respectively. The second pressure thus being substantially lower than the third pressure and the second temperature thus being substantially lower than the third temperature, separating the second vapor phase and the second liquid phase in the separation-contacting zone to produce a third vapor phase substantially enriched in the higher boiling constituents and a third liquid phase substantially enriched in the lower boiling constituents, introducing the third vapor phase into a fractional distillation zone adjacent the top thereof and introducing the third liquid phase into the fractional distillation zone at an upper intermediate point, fractionally distilling the third vapor phase and the third liquid phase to produce a fourth vapor phase substantially enriched in the higher boiling constituents and a fourth liquid phase substantially enriched in lower boiling constituents, recovering the fourth vapor phase as a product and recovering the fourth liquid phase as a product. In accordance with another aspect, at least a portion of the second vapor phase and/or at least a portion of the third vapor phase is expanded in a turbo expander.
Inventors
- 👤 Ethelwolbo P. Perez
Bibliographic Details
Application Number
—
Jurisdiction
US
Data Source
google_patents
Last Synchronized
2026-11-08 13:53
CPC Classifications
C; C07; C07C; C07C7/00; C07C7/005; F; F25; F25J; F25J3/00; F25J3/02; F25J3/0204; F25J3/0209; F25J3/0228; F25J3/0233; F25J3/0238; F25J2200/00; F25J2200/04; F25J2200/40; F25J2200/70; F25J2200/78; F25J2205/00; F25J2205/02; F25J2205/04; F25J2220/00; F25J2220/60; F25J2220/66; F25J2240/00; F25J2240/02; F25J2270/00; F25J2270/04; F25J2270/12; F25J2270/60; F25J2280/00; F25J2280/02
Claims Analysis
Total Claims: 29
Claim 1
Independent Claim
361 words
A method for separating ethane and higher molecular weight hydrocarbons from a natural gas feed, predominating in methane and containing significant amounts of said ethane and higher molecular weight hydrocarbons and having a first pressure substantially above atmospheric pressure and a first temperature substantially below atmospheric temperature, at which first pressure and first temperature, said feed comprises both a vapor phase, representing a first vapor phase, and a liquid phase, representing a first liquid phase, comprising: (a) expanding at least a part of said vapor phase, in a first expansion step, to produce a first expanded fluid having a second pressure substantially lower than said first pressure and a second temperature substantially lower than said first temperature; (b) introducing all of said first expanded fluid and any unexpanded first vapor phase into a separation-contacting zone adjacent the top thereof and introducing all of said first liquid phase into said separation-contacting zone at a lower intermediate point thereof, under conditions and in proportions such that the pressure at the top of said separation-contacting zone is substantially lower than the pressure at the bottom of said separation-contacting zone and the temperature at said top of said separation-contacting zone is substantially lower than the temperature at said bottom of said separation-contacting zone; (c) separating said first expanded fluid, said unexpanded remaining portion of said first vapor phase and said first liquid phase, in said separation-contacting zone, to produce a second vapor phase and a second liquid phase; (d) introducing said second vapor phase into a fractional distillation zone adjacent the top thereof and introducing said second liquid phase into said fractional distillation zone at an intermediate point thereof below the point of introduction of said second vapor phase; (e) fractionally distilling said second vapor phase and said second liquid phase, in said frictional distillation zone, to produce a third vapor phase predominating in methane and containing insignificant amounts of ethane and higher molecular weight hydrocarbons and a third liquid phase predominating in ethane and higher molecular weight hydrocarbons and containing insignificant amounts of methane; p1 (f) recovering said third vapor phase as a product; and (g) recovering said third liquid phase as a product.
Claim 2
Independent Claim
361 words
A method for separating ethane and higher molecular weight hydrocarbons from a natural gas feed, predominating in methane and containing significant amounts of said ethane and higher molecular weight hydrocarbons and having a first pressure substantially above atmospheric pressure and a first temperature substantially below atmospheric temperature, at which first pressure and first temperature, said feed comprises both a vapor phase, representing a first vapor phase, and a liquid phase, representing a first liquid phase, comprising: (a) expanding at least a part of said vapor phase, in a first expansion step, to produce a first expanded fluid having a second pressure substantially lower than said first pressure and a second temperature substantially lower than said first temperature; (b) introducing all of said first expanded fluid and any unexpanded first vapor phase into a separation-contacting zone adjacent the top thereof and introducing all of said first liquid phase into said separation-contacting zone at a lower intermediate point thereof, under conditions and in proportions such that the pressure at the top of said separation-contacting zone is substantially lower than the pressure at the bottom of said separation-contacting zone and the temperature at said top of said separation-contacting zone is substantially lower than the temperature at said bottom of said separation-contacting zone; (c) separating said first expanded fluid, said unexpanded remaining portion of said first vapor phase and said first liquid phase, in said separation-contacting zone, to produce a second vapor phase and a second liquid phase; (d) introducing said second vapor phase into a fractional distillation zone adjacent the top thereof and introducing said second liquid phase into said fractional distillation zone at an intermediate point thereof below the point of introduction of said second vapor phase; (e) fractionally distilling said second vapor phase and said second liquid phase, in said frictional distillation zone, to produce a third vapor phase predominating in methane and containing insignificant amounts of ethane and higher molecular weight hydrocarbons and a third liquid phase predominating in ethane and higher molecular weight hydrocarbons and containing insignificant amounts of methane; p1 (f) recovering said third vapor phase as a product; and (g) recovering said third liquid phase as a product.
Claim 3
Dependent Claim
28 words
A method in accordance with claim 1 wherein the first vapor phase and the first liquid phase are produced by separating the feed, in a first separation zone.
Claim 4
Dependent Claim
48 words
A method in accordance with claim 2 wherein the feed having a first pressure substantially above atmospheric pressure and a first temperature substantially below atmospheric temperature is produced by cooling a natural gas having said first pressure and a temperature near atmospheric temperature, in a first cooling step.
Claim 5
Dependent Claim
35 words
A method in accordance with claim 3 wherein the third vapor phase is utilized to supply cooling, in the first cooling step, by passing said third vapor phase in indirect heat exchange with the feed.
Claim 6
Dependent Claim
27 words
A method in accordance with claim 1 wherein the second vapor phase is cooled, in a second cooling step, prior to introduction into the fractional distillation zone.
Claim 7
Dependent Claim
51 words
A method in accordance with claim 5 wherein the second vapor phase is thus cooled, in the second cooling step, by indirect heat exchange with at least one of (1) the third vapor phase and (2) a first side stream withdrawn from an upper intermediate point in said fractional distillation zone.
Claim 8
Dependent Claim
66 words
A method in accordance with claim 6 wherein the first side stream is withdrawn from the fractional distillation zone at an upper intermediate point above the point of introduction of the second liquid phase, passed in indirect heat exchange with the second vapor phase and returned to said fractional distillation zone with the second liquid phase, to thereby at least partially heat said fractional distillation zone.
Claim 9
Dependent Claim
37 words
A method in accordance with claim 5 wherein the second vapor phase thus cooled, in the second cooling step, is separated, in a second separation step, to produce a fourth vapor phase and a fourth liquid phase.
Claim 10
Dependent Claim
77 words
A method in accordance with claim 8 wherein at least a part of the fourth vapor phase is expanded in a second expansion step, to produce a second expanded fluid and said second expanded fluid is introduced into the top of the fractional distillation zone and the fourth liquid phase is introduced into the fractional distillation zone between the point of introduction of said second expanded fluid and the point of introduction of the second liquid phase.
Claim 11
Dependent Claim
55 words
A method in accordance with claim 1 or 9 wherein the fractional distillation zone comprises an upper rectifying section and a lower stripping section, all vapor phases introduced into said fractional distillation zone are introduced into said rectification section and all liquid phases introduced into said fractional distillation zone are introduced into said stripping section.
Claim 12
Dependent Claim
77 words
A method in accordance with claim 1 or 9 wherein the fractional distillation zone is heated at least in part by withdrawing a second side stream from said fractional distillation zone at a lower intermediate point thereof, passing the same in indirect heat exchange with part of the warmest available feed, in a first heating zone, and returning the thus heated second side stream to said fractional distillation zone at a point below its point of withdrawal.
Claim 13
Dependent Claim
159 words
A method in accordance with claim 1 or 9 wherein the fractional distillation zone and the third liquid phase are heated at least in part by passing the third liquid phase in indirect heat exchange with part of the warmest available feed, in a second heating zone, separating the thus heated third liquid phase into a fifth vapor phase and a fifth liquid phase, in a third separation zone, returning said fifth vapor phase to said fractional distillation zone above the point of withdrawal of said third liquid phase, recovering said fifth liquid phase as the product predominating in ethane and higher molecular weight hydrocarbons and containing insignificant amounts of methane, and returning said portion of said feed thus utilized to supply heat to said fractional distillation zone to the main feed stream at a point at which the temperature of said main feed stream is approximately equal to the temperature of the thus returned portion of the feed.
Claim 14
Dependent Claim
48 words
A method in accordance with claim 12 wherein the volume of the part of the feed thus utilized to supply heat to the fractional distillation zone is controlled in accordance with the temperature at which the thus heated fifth vapor phase is returned to said fractional distillation zone.
Claim 15
Dependent Claim
61 words
A method in accordance with claim 12 wherein the fifth liquid phase is passed in indirect heat exchange with the part of the feed utilized to supply heat to the fractional distillation zone, in a third heating step, prior to thus passing said part of the feed in indirect heat exchange with the third liquid phase, in the second heating step.
Claim 16
Dependent Claim
74 words
A method in accordance with claim 12 wherein the thus heated third liquid phase is further heated, in a fourth heating step, by an external source of heat and separated into a sixth vapor phase and a sixth liquid phase, the sixth vapor phase is returned to the fractional distillation zone and the sixth liquid phase is separated, in the third separation zone to produce the fifth vapor phase and the fifth liquid phase.
Claim 17
Dependent Claim
53 words
A method in accordance with claim 15 wherein the volume of the part of the feed thus utilized to supply heat to the fractional distillation unit is controlled in accordance with the temperature at which the thus warmed sixth vapor phase and the fifth vapor phase are returned to said fractional distillation zone.
Claim 18
Dependent Claim
217 words
A method in accordance with claim 1 or 9 wherein the fractional distillation zone is heated at least in part by passing a part of the warmest available feed in indirect heat exchange with a second side stream, withdrawn from said fractional distillation zone at a lower intermediate point and returned to said fractional distillation zone at a point below its point of withdrawal, in a first heating zone, with the third liquid phase, in a second heating zone, and with a fifth liquid phase, produced by separating the thus warmed third liquid phase into a fifth vapor phase and a fifth liquid phase, in a third heating step, the fifth vapor phase is returned to said fractional distillation zone at a point above the point of withdrawal of said third liquid phase, the fifth liquid phase is recovered as the product predominating in ethane and higher molecular weight hydrocarbons and containing insignificant amounts of methane, said part of said feed is returned to the main feed stream at a point at which the temperature of said main feed stream is approximately equal to the temperature of the thus returned portion of the feed, and said part of said feed is passed sequentially through said third heating step, said second heating step and said first heating step.
Claim 19
Dependent Claim
45 words
A method in accordance with claim 17 wherein the portion of the feed thus utilized to supply heat to the fractional distillation zone is cooled, with an external cooling medium, in a third cooling step, between the first heating step and the second heating step.
Claim 20
Dependent Claim
46 words
A method in accordance with claim 35 wherein the volume of the portion of the feed thus utilized to supply heat to the fractional distillation zone is controlled in accordance with the temperature at which the fifth vapor phase is returned to said fractional distillation zone.
Claim 21
Dependent Claim
74 words
A method in accordance with claim 17 wherein the thus heated third liquid phase is further heated, in a fourth heating step, by an external source of heat, and separated into a sixth vapor phase and a sixth liquid phase, the sixth vapor phase is returned to the fractional distillation zone and the sixth liquid phase is separated, in the third separation zone, to produce the fifth vapor phase and the fifth liquid phase.
Claim 22
Dependent Claim
51 words
A method in accordance with claim 20 wherein the volume of the portion of the feed thus utilized to supply heat to the fractional distillation zone is controlled in accordance with the temperature at with the fifth vapor phase and the sixth vapor phase are returned to the fractional distillation zone.
Claim 23
Dependent Claim
32 words
A method in accordance with claim 1 or 9 wherein the feed also contains significant amounts of carbon dioxide and the third liquid phase contains substantially reduced amounts of said carbon dioxide.
Claim 24
Dependent Claim
30 words
A method in accordance with claim 1 or 9 wherein the feed also contains significant amounts of nitrogen and the third vapor phase contains a major portion of said nitrogen.
Claim 25
Dependent Claim
42 words
A method in accordance with claim 1 or 9 wherein the first expansion step and the first and second expansion step, as the case may be, are performed in expansion sections of turbo expander-compressors in which said extension sections drive compressor sections.
Claim 26
Dependent Claim
37 words
A method in accordance with claim 24 wherein the third vapor phase is compressed in at least one of the compression sections of the turbo expander-compressors prior to recovery of said third vapor phase as a product.
Claim 27
Dependent Claim
41 words
A method in accordance with claim 1 or 9 wherein the second pressure is between about 150 and 250 psia below the first pressure and second temperature is between about 20° F. and about 40° F. lower than the first temperature.
Claim 28
Dependent Claim
55 words
A method in accordance with claim 1 or 9 wherein the separation-contacting zone has an extended contact surface located between the top and the bottom thereof and improved contact between rising vapors and descending liquids in said separation-contacting zone is obtained by passing said rising vapors and said descending liquids through said extended contact surface.
Claim 29
Dependent Claim
70 words
A method in accordance with claim 1 or 9 wherein the upper portion of the separation-contacting zone into which the first vapor phase is introduced has cross sectional flow restricting surfaces disposed therein and improved contact of vapors and liquids in said upper portion of said separation-contacting zone is obtained by passing said first expanded fluid and rising vapors in said separation-contacting zone through said cross sectional flow restricting surfaces.
References Cited (Backward Citations)
US4322225A
Cited
USPTO Annuity & Maintenance Windows
| Annuity Stage | Window Opens | Payment Deadline | Surcharge Period Until | Estimated Fee | Status |
|---|---|---|---|---|---|
| 3.5 Years (Year 4) | 1987-06-26 | 1987-12-26 | 1988-06-26 | $2000.00 | Window Closed / Lapsed |
| 7.5 Years (Year 8) | 1991-06-26 | 1991-12-26 | 1992-06-26 | $3760.00 | Window Closed / Lapsed |
| 11.5 Years (Year 12) | 1995-06-26 | 1995-12-26 | 1996-06-26 | $7700.00 | Window Closed / Lapsed |