EP4001812A1 - Verbesserung der c3+-rückgewinnung - Google Patents

Verbesserung der c3+-rückgewinnung Download PDF

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Publication number
EP4001812A1
EP4001812A1 EP20207964.6A EP20207964A EP4001812A1 EP 4001812 A1 EP4001812 A1 EP 4001812A1 EP 20207964 A EP20207964 A EP 20207964A EP 4001812 A1 EP4001812 A1 EP 4001812A1
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EP
European Patent Office
Prior art keywords
stream
carbon atoms
hydrocarbons containing
feed gas
gas stream
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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EP20207964.6A
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English (en)
French (fr)
Inventor
Pascal Marty
Martin Raventos
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Priority to EP20207964.6A priority Critical patent/EP4001812A1/de
Publication of EP4001812A1 publication Critical patent/EP4001812A1/de
Withdrawn legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/061—Natural gas or substitute natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0252—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of hydrogen
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/062—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/0635—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/0645—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/0655—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of hydrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/80—Processes or apparatus using other separation and/or other processing means using membrane, i.e. including a permeation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/04—Mixing or blending of fluids with the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons

Definitions

  • NGLs C3+ components
  • Most traditional plants remove NGLs via cryogenic plants but those technologies usually are very expensive and consume a lot of power required by external refrigeration cycles.
  • a less costly technology that can be used to concentrate NGLs is membrane technology.
  • Feed gas stream 101 is compressed in feed compressor 102, then introduced into first phase separator 103.
  • the compressed feed gas stream may be cooled in a heat exchanger (not shown) prior to admission into first phase separator 103.
  • First phase separator 103 produces first condensate stream 104 and damp gas stream 105. Damp gas stream 105 is then introduced into first dehydration unit 106.
  • the dehydrated gas stream is cooled in heat exchanger 107, wherein it forms at least partially condensed stream 108. At least partially condensed stream is then introduced into second phase separator 109. Second phase separator 109 produces C3+ rich liqud stream 110 and C3+ lean gas stream 111. C3+ rich liquid stream 110 is then warmed in heat exchanger 107, producing warmed C3+ rich liquid stream 123. Warmed C3+ rich liquid stream 123 is then introduced into separator drum 112.
  • Separator drum 112 may be a flash drum or a distillation column.
  • Separator drum 112 produces overhead gas stream 113 which is enriched in methane, and C3+ liquid product stream 114.
  • C3+ lean gas stream 111 then enters membrane separator 115, thereby producing permeate stream 116 and retentate stream 117.
  • Permeate stream 116 may be combined with feed gas stream 101 (not shown).
  • Retentate stream 117 then combined with overhead gas stream 113, thus producing first combined stream 118.
  • First combined stream 118 is heated in heat exchanger 107 then dried in second dehydration unit 119. Dried retentate stream is then introduced into third phase separator 120.
  • Third phase separator 120 produces second condensate stream 121 and fuel gas stream 122.
  • ambient temperature is defined as the temperature of the surrounding air. Ambient temperature may be defined as between 32 and 150 F. Ambient temperature may be defined as between 32 and 100 F. Ambient temperature may be defined as between 50 and 80 F. Ambient temperature may be defined as between 65 and 75 F.
  • feed gas stream 101 is compressed in feed compressor 102, then introduced into first phase separator 103.
  • the compressed feed gas stream may be cooled in a heat exchanger (not shown) prior to admission into first phase separator 103.
  • First phase separator 103 produces first condensate stream 104 and damp gas stream 105.
  • First condensate stream 104 comprises condensed water.
  • Damp gas stream 105 is then introduced into dehydration unit 106. Dehydration 106 is necessary to avoid freezing and hydrate formation in the cold part of the process. Unless the moisture content in the feed gas stream is sufficiently low, in which case first phase separator 103 is not required.
  • Dehydration unit 106 is shown downstream of first phase separator 103 (which is the preferable location) but may be upstream of first phase separator 103. Dehydration unit 106 may be upstream of feed compressor 102, downstream of compressor 102, or at a point between stages. These variations are not shown in the figure in the interest of maintaining clarity, but the skilled artisan would recognize these placements.
  • Compressed, dehydrated gas stream 209 is then cooled in heat exchanger 107, wherein it forms partially condensed cooled stream 108.
  • Stream 108 is then introduced into second phase separator 109, which produces C3+ rich liquid stream 110 and C3+ lean gas stream 111.
  • heat exchanger 107 may consist of two or more thermally separate heat exchangers as the design permits (not shown). One or more of these heat exchangers may be of the brazed aluminum design. One or more of these heat exchangers may be of the shell and tube design.
  • stream 108 is expanded to a lower pressure across second JT expansion valve 207 to produce partially condensed stream 208, which is then introduced into phase separator 109.
  • cooled stream 108 need not be partially condensed.
  • C3+ rich liquid stream 110 is warmed in heat exchanger 107, thus producing warmed C3+ rich liquid stream 123.
  • Warmed C3+ rich liquid stream 123 is then introduced into separator drum 112.
  • Separator drum 112 may be a flash drum or a distillation column. Separator drum 112 produces overhead gas stream 113 which is enriched in hydrocarbons containing no more than 3 carbon atoms, and C3+ liquid product stream 114.
  • C3+ lean gas stream 111 is then warmed in heat exchanger 107, thus producing warmed C3+ lean gas stream 201.
  • Warmed C3+ lean gas stream 201 is at approximately ambient temperature.
  • Warmed C3+ lean gas stream 201 then enters membrane separator 115, thereby producing permeate stream 116 and retentate stream 117.
  • Permeate stream 116 may be combined with feed gas stream 101 (not shown) to increase the recovery of C3+ hydrocarbons in C3+ product stream 114.
  • feed 101 is available at high pressure. In that case, permeate 116 pressure would be increased through dedicated compressor (not shown).
  • the flux and selectivity vectors are better known for membranes at ambient temperature.
  • the possibility to bypass the heat exchanger if membrane separator 115 is to be operated at sub-ambient temperatures allows fine tuning of the required selectivities between components and the off-gas composition.
  • Retentate stream 117 is cooled in heat exchanger 107, thus producing cooled retentate stream 202.
  • Cooled retentate stream 202 is expanded across first JT valve 203, thus producing expanded retentate stream 204.
  • Expanded retentate stream 204 is then combined with overhead stream enriched in hydrocarbons containing no more than 3 carbon atoms 113 (after expansion to pressure of stream 204 / not shown), thereby producing a second combined stream 205, which provides cold to the end of heat exchanger 107.
  • Second combined stream 205 is then warmed up to ambient temperature in heat exchanger 107 thus producing fuel gas stream 206. At least a portion of fuel gas stream 206 may be used for the regeneration of driers 106 (not shown).
  • feed gas stream 101 is compressed in feed compressor 102, then introduced into first phase separator 103.
  • the compressed feed gas stream may be cooled in a heat exchanger (not shown) prior to admission into first phase separator 103.
  • First phase separator 103 produces first condensate stream 104 and damp gas stream 105.
  • Damp gas stream 105 is then introduced into dehydration unit 106. Dehydration is necessary to avoid freezing and hydrate formation in the cold part of the process unless the moisture content in the feed gas stream is sufficiently low, in which case the first separator 103 is not required.
  • Dehydration unit 106 is shown downstream of first phase separator 103 but may be upstream of first phase separator 103. Dehydration unit 106 may be upstream of feed compressor 102, downstream of compressor 102, or at a point between stages. These variations are not shown in the figure in the interest of maintaining clarity, but the skilled artisan would recognize these placements.
  • Compressed, dehydrated gas stream 209 is then cooled in heat exchanger 107, wherein it forms partially condensed cooled stream 108.
  • Stream 108 is then introduced into second phase separator 109, which produces C3+ rich liquid stream 110 and C3+ lean gas stream 111.
  • heat exchanger 107 may consist of two or more thermally separate heat exchangers as the design permits (not shown). One or more of these heat exchangers may be of the brazed aluminum design. One or more of these heat exchangers may be of the shell and tube design.
  • stream 108 is expanded to a lower pressure across second JT expansion valve 207 to produce partially condensed stream 208, which is then introduced into phase separator 109.
  • cooled stream 108 need not be partially condensed.
  • C3+ rich liquid stream 110 is then warmed in heat exchanger 107, thus forming warmed C3+ rich liquid stream 307.
  • Warmed C3+ rich liquid stream 307 is then combined with C3+further enriched liquid stream 304 (below), thus forming combined C3+ lean gas stream 308.
  • Combined C3+ lean gas stream 308 is then introduced into separator drum 112.
  • Separator drum 112 may be a flash drum or a distillation column.
  • Distillation column 112 produces overhead gas stream 113 which is enriched in hydrocarbons containing no more than 3 carbon atoms, and C3+ liquid product stream 114.
  • the light ends in overhead gas stream 113 may comprise C2+ hydrocarbons.
  • overhead gas stream 113 is combined with fuel gas stream 206 (below)
  • C3+ lean gas stream 111 is expanded through first JT valve 203 thus producing partially condensed stream 111b.
  • Partially condensed stream 111b is combined with overhead stream enriched in hydrocarbons containing no more than 3 carbon atoms 113 (after expansion at pressure of stream 111b / not shown), thus forming third combined stream 301.
  • Third combined stream 301 is then introduced into fourth phase separator 302.
  • Fourth phase separator 302 produces C3+ further enriched liquid stream 304 and C3+ depleted gas stream 303.
  • C3+ depleted gas stream 303 is then introduced into expander 305, thus producing expanded stream 306
  • Power generated by expander 305 may be used to at least partially drive the feed compressor 102, thus reducing the power consumption and increasing the overall efficiency of the process.
  • Expanded stream 306 is then warmed in heat exchanger 107 thus producing fuel gas stream 206.
  • Expanded stream 306 may be at a temperature of approximately -88C and may be heated up to approximately ambient temperature in heat exchanger 107. This addition of refrigeration into heat exchanger 107 thus allows the compressed feed gas to reach even lower temperatures before its expansion into second phase separator 109, which results in a higher net NGL recovery rate.
  • At least a portion of fuel gas stream 206 may be used for the regeneration of driers 106 (not shown).
  • external refrigeration cycle 400 may be included to add at least a portion of the required refrigeration.
  • External refrigeration cycle 400 may be a propane cycle.
  • the feed gas is precooled in the main heat exchanger and the condensed liquids are separated in a "cold separator".
  • the remaining gas is expanded in a turbine, whereas the liquids are expanded across a valve.
  • Both expanded streams are typically fed to an absorption or distillation column.
  • This concept is not well suited for the case under consideration (low pressure refinery off-gas, rich in hydrogen, with moderate to high amounts of C3-C4).
  • the turbine is used indirectly for reaching lower temperatures at the NGL separation stage, by expanding a product (fuel gas) and using it as cooling medium in the exchange line. This scheme is able to reach higher C3 recovery rates with lower energy consumption as compared to the previously described alternatives.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP20207964.6A 2020-11-17 2020-11-17 Verbesserung der c3+-rückgewinnung Withdrawn EP4001812A1 (de)

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5421167A (en) * 1994-04-01 1995-06-06 The M. W. Kellogg Company Enhanced olefin recovery method
DE102005010054A1 (de) * 2005-03-04 2006-09-07 Linde Ag Verfahren zum gleichzeitigen Gewinnen einer Helium- und einer Stickstoff-Reinfraktion
WO2016092178A1 (fr) * 2014-12-11 2016-06-16 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil pour séparer un gaz d'alimentation contenant au moins 20% mol. de co2 et au moins 20% mol. de méthane, par condensation partielle et/ou par distillation
WO2016156691A1 (fr) * 2015-04-02 2016-10-06 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé de traitement du gaz naturel pour minimiser la perte d'éthane
US20200308494A1 (en) * 2019-03-27 2020-10-01 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude C3+ recovery with membranes

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5421167A (en) * 1994-04-01 1995-06-06 The M. W. Kellogg Company Enhanced olefin recovery method
DE102005010054A1 (de) * 2005-03-04 2006-09-07 Linde Ag Verfahren zum gleichzeitigen Gewinnen einer Helium- und einer Stickstoff-Reinfraktion
WO2016092178A1 (fr) * 2014-12-11 2016-06-16 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil pour séparer un gaz d'alimentation contenant au moins 20% mol. de co2 et au moins 20% mol. de méthane, par condensation partielle et/ou par distillation
WO2016156691A1 (fr) * 2015-04-02 2016-10-06 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé de traitement du gaz naturel pour minimiser la perte d'éthane
US20200308494A1 (en) * 2019-03-27 2020-10-01 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude C3+ recovery with membranes

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