US20150052938A1 - Combined removal of heavies and lights from natural gas - Google Patents

Combined removal of heavies and lights from natural gas Download PDF

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Publication number
US20150052938A1
US20150052938A1 US14/462,624 US201414462624A US2015052938A1 US 20150052938 A1 US20150052938 A1 US 20150052938A1 US 201414462624 A US201414462624 A US 201414462624A US 2015052938 A1 US2015052938 A1 US 2015052938A1
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Prior art keywords
fraction
removal stage
process according
pressure
heavies
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English (en)
Inventor
Heinz Bauer
Hartmut WALZ
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Linde GmbH
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Linde GmbH
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Assigned to LINDE AKTIENGESELLSCHAFT reassignment LINDE AKTIENGESELLSCHAFT ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: BAUER, HEINZ, WALZ, HARTMUT
Publication of US20150052938A1 publication Critical patent/US20150052938A1/en
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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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. 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
    • F25J3/0228—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
    • 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
    • F25J3/0228—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
    • F25J3/0238—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 2 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
    • F25J3/02—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
    • F25J3/0257—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 nitrogen
    • 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
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual 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
    • F25J2200/30—Processes or apparatus using separation by rectification using a side column in a single pressure 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
    • F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
    • 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
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F25J2200/96—Dividing wall column
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/66—Separating acid gases, e.g. CO2, SO2, H2S or RSH
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. 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
    • F25J2270/02—Internal 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
    • F25J2270/88—Quasi-closed internal refrigeration or heat pump cycle, if not otherwise provided
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/40—Vertical layout or arrangement of cold equipments within in the cold box, e.g. columns, condensers, heat exchangers etc.

Definitions

  • the invention relates to a process for removing heavies and lights from a hydrocarbon-rich feed fraction, preferably from natural gas, wherein
  • Natural gas consists not only of methane, its main component, but generally also of components having a higher boiling point, for example ethane, propane and higher alkanes—hereinafter referred to as heavies—and also of components having a lower boiling point, for example nitrogen, hydrogen and helium—hereinafter referred to as lights.
  • heavies components having a higher boiling point
  • lights also of components having a lower boiling point, for example nitrogen, hydrogen and helium
  • the heating value or Wobbe Index reduced by the removal of heavies, to be pushed back up by the removal of inert lights—meaning nitrogen and helium.
  • U.S. Pat. No. 4,504,295 discloses a process of the type in question for removal of heavies and lights from natural gas by combining known processes for removing heavies and lights.
  • the energy consumption of the single-column process for removing lights which is described in the US patent cited above is generally higher than that achieved on using a more capital-intensive double-column process.
  • double-column processes require an upstream enrichment column when the nitrogen concentration of the feed fraction is less than 25 mol %.
  • the operating pressure required for this enrichment column is generally not less than 5 bar above the operating pressure of the methane/ethane (demethanizer) separation column used to remove the heavies. This accordingly makes it necessary to compress the gas between removing the heavies and the lights, or alternatively to perform a total condensation with a subsequent pump in order that the required pressure profile may be established.
  • the invention accordingly combines a preferably carbon dioxide-lean, open loop refrigeration cycle, wherein the refrigerant is vaporized to two different pressure levels, with the physical link between the removal of heavies in the 1st removal stage and the removal of lights in the 2nd removal stage, while the fraction withdrawn from the 1st removal stage and supplied to the 2nd removal stage is not subjected to any pressure elevation.
  • FIG. 1 illustrates an embodiment in which the second removal stage is realized in a single column T 2 with a dividing wall
  • FIG. 2 illustrates an embodiment in which the second removal stage is realized in three interconnected columns T 2 ′, T 3 and T 4 .
  • a natural gas stream comprising lights and heavies and generally having a pressure between 35 and 50 bar passes via line 1 through heat exchangers E 1 and E 2 and is partially condensed therein against process streams as more particularly discussed herein below.
  • the natural gas stream 2 withdrawn from heat exchanger E 2 is separated in separator D 1 into a liquid phase 3 and a gas phase 4 .
  • the former is fed via expansion valve V 1 to the methane/ethane separation column T 1 (demethanizer), which embodies the 1st removal stage, in the upper region thereof.
  • the aforementioned gas phase 4 is expanded in expander X 1 and likewise applied to column T 1 in the head region thereof.
  • a substream of gas phase 4 generated in separator D 1 is applied to column T 1 as reflux via expansion valve V 4 after splitting into the two substreams 5 and 6 , which are condensed in heat exchangers E 5 and E 2 , respectively.
  • column T 1 is operated at a pressure of at least 25 bar, preferably at least 28 bar.
  • the operating pressure of the 1st removal stage T 1 is 25 to 35 bar.
  • the requisite lateral heaters a/b of column T 1 are only depicted schematically.
  • a heavies-rich liquid fraction 8 is withdrawn from the base of column T 1 and sent to its further use, for example its separation into ethane and a further fraction consisting of propane and higher hydrocarbons.
  • the ethane fraction is frequently used as ethylene plant feed, while the propane-containing fraction is subjected to various chemical operations.
  • a substream 9 of liquid fraction 8 is vaporized in reboiler E 3 and returned to column T 1 .
  • the heavies-depleted gas fraction 10 obtained at the top of the first removal stage T 1 is partially condensed in heat exchanger E 4 and fed via expansion valve V 6 to the 2nd column or removal stage T 2 .
  • the above-described fraction 10 experiences no pressure elevation due to a pump or a compressor between its withdrawal from the 1st removal stage T 1 and its feeding into the 2nd removal stage T 2 .
  • the operating pressure of the 2nd removal stage T 2 is 22 to 32 bar.
  • a rectificatory separation takes place in column T 2 into a methane-rich liquid fraction 11 , which is withdrawn from the base of column T 2 , and a lights-rich gas fraction 12 , which is withdrawn from the head region of column T 2 .
  • the aforementioned methane-rich liquid fraction 11 is expanded in valve V 7 to a pressure from 3 to 15 bar, preferably from 5 to 10 bar below the operating pressure of column T 1 .
  • This methane-rich fraction is then fully vaporized in heat exchanger E 4 , subsequently warmed in heat exchangers E 2 and E 1 and discharged as methane-rich product stream 11 ′.
  • the lights-rich gas fraction 12 withdrawn from the head region of column T 2 is warmed in heat exchanger E 6 and subsequently sent to its further use, for example the recovery of helium, via line 12 ′.
  • a substream 13 of the aforementioned methane-rich liquid fraction is at least partly vaporized in heat exchanger E 5 and then applied to column T 2 in the lower region thereof.
  • the second removal stage or column T 2 preferably includes a dividing wall T, this being at least disposed in that region of column T 2 where the column is fed with the heavies-depleted fraction 10 and a carbon dioxide-lean fraction 25 , which will be more particularly discussed herein below, is withdrawn.
  • Dividing wall T prevents physical contact between the two aforementioned fractions.
  • the reflux for the second removal stage or column T 2 is produced via an open loop refrigeration cycle.
  • the refrigerant of this refrigeration cycle has a methane content of at least 80 mol %, preferably at least 85 mol %. It is particularly advantageous for the composition of the refrigerant of this refrigeration cycle to essentially correspond to the composition of the aforementioned carbon dioxide-lean fraction 25 .
  • the refrigerant used for the open loop refrigeration cycle is the aforementioned carbon dioxide-lean, methane-rich fraction 25 .
  • the fully condensed refrigerant 21 is then fed to the buffer container D 4 .
  • the two refrigerant substreams 22 and 24 are removed therefrom.
  • the latter substream is subcooled in heat exchanger E 5 and then expanded via valve V 12 into column T 2
  • refrigerant substream 22 is subcooled in heat exchanger E 6 and fed via expansion valve V 11 to the head condenser E 7 of column T 2 .
  • From this head condenser it is withdrawn via line 23 , warmed in heat exchanger E 6 and then fed to the first stage of cycle compressor C 1 .
  • the latter can be connected together via control valve V 14 .
  • Refrigerant streams 22 and 25 are vaporized against reflux streams 14 and 15 , respectively, in head condenser E 7 and side condenser E 8 such that the pressure of refrigerant 25 vaporized in side condenser E 8 is at least three times, preferably five times the pressure of refrigerant 22 vaporized in head condenser E 7 .
  • the effect of the rectification in column T 2 and also of dividing wall T disposed therein is that the carbon dioxide concentration in the carbon dioxide-lean refrigerant fraction withdrawn via line 25 is below 50 vppm, preferably below 5 vppm.
  • head condenser E 7 By providing dividing wall T it is possible for head condenser E 7 to be provided with a refrigerant fraction which does not cause solids formation by carbon dioxide even at an operating temperature below ⁇ 150° C., preferably below ⁇ 155° C. This ensures that the lights-rich gas fraction 12 withdrawn from the head region of column T 2 has a methane content of less than 2% by volume, preferably less than 1% by volume.
  • the energy consumption of compressor unit C 1 decreases by at least 30% compared with a process where side condenser E 8 is eschewed.
  • the choice of operating pressure for the first removal stage T 1 ensures that the lights-rich gas fraction 12 which is withdrawn from the head region of column T 2 and which has a nitrogen content of more than 90 mol %, preferably more than 95 mol %, can be at least partly condensed against the refrigerant without causing a pressure below atmospheric pressure on the suction side of cycle compressor C 1 .
  • a substream of the heavies-depleted gas fraction 10 obtained in the first removal stage T 1 is at least temporarily admixed via line 50 , in which a control valve V 5 is provided, to the methane-rich liquid fraction 11 obtained in the second removal stage T 2 .
  • the interconnected system described above serves to split the column T 2 depicted in FIG. 1 into smaller, more easily transported, more efficiently operated and more quickly assembled units.
  • the process provided by the present invention for removing heavies and lights from a hydrocarbon-rich feed fraction, preferably from natural gas, has an energy consumption which corresponds to that of a double column arrangement while eschewing the undesired elevation of pressure between the removal of heavies and lights.

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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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US14/462,624 2013-08-20 2014-08-19 Combined removal of heavies and lights from natural gas Abandoned US20150052938A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102013013883.3A DE102013013883A1 (de) 2013-08-20 2013-08-20 Kombinierte Abtrennung von Schwer- und Leichtsiedern aus Erdgas
DE102013013883.3 2013-08-20

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DE (1) DE102013013883A1 (ru)
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Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20170023294A1 (en) * 2015-07-22 2017-01-26 Butts Properties, Ltd. System and Method for Separating Wide Variations in Methane and Nitrogen
US20190056176A1 (en) * 2015-12-23 2019-02-21 Linde Aktiengesellschaft Process and device for the cryogenic separation of synthesis gas
WO2019175167A1 (en) * 2018-03-13 2019-09-19 Reslinde Aktiengesellschaft Method for operating a natural gas processing plant
US20210156613A1 (en) * 2018-04-09 2021-05-27 Linde Engineering North America, Inc. Methods and systems for removing nitrogen from natural gas
US11207611B1 (en) 2018-07-03 2021-12-28 Burns & Mcdonnell Engineering Company, Inc. Process for separating hydrocarbons in a liquid feed utilizing an externally heated reboiler connected to a divided wall column as the primary source of heat energy
US11378333B2 (en) 2019-12-13 2022-07-05 Bcck Holding Company System and method for separating methane and nitrogen with reduced horsepower demands
US11650009B2 (en) 2019-12-13 2023-05-16 Bcck Holding Company System and method for separating methane and nitrogen with reduced horsepower demands
US11686528B2 (en) * 2019-04-23 2023-06-27 Chart Energy & Chemicals, Inc. Single column nitrogen rejection unit with side draw heat pump reflux system and method
TWI850366B (zh) 2019-04-23 2024-08-01 美商圖表能源與化學有限公司 用於從天然氣流體進給流中除去氮的系統及方法

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