EP1861671B1 - Procédé et dispositif pour séparer des liquides de gaz naturel à partir d'un courant de gaz naturel liquéfié - Google Patents

Procédé et dispositif pour séparer des liquides de gaz naturel à partir d'un courant de gaz naturel liquéfié Download PDF

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Publication number
EP1861671B1
EP1861671B1 EP06708800.5A EP06708800A EP1861671B1 EP 1861671 B1 EP1861671 B1 EP 1861671B1 EP 06708800 A EP06708800 A EP 06708800A EP 1861671 B1 EP1861671 B1 EP 1861671B1
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Prior art keywords
stream
heat exchanger
exchanger arrangement
natural gas
feeding point
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German (de)
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EP1861671A1 (fr
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Paramasivam Senthil c/o Shell Offshoring - Wipro Technologies KUMAR
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Shell Internationale Research Maatschappij BV
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Shell Internationale Research Maatschappij BV
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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
    • F25J3/02—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
    • F25J3/0214—Liquefied 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
    • F25J3/0242—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
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F25J2200/92—Details relating to the feed point
    • 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
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • 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
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
    • 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
    • F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass 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
    • F25J2270/88—Quasi-closed internal refrigeration or heat pump cycle, if not otherwise provided

Definitions

  • the present invention relates to a method and apparatus for deriching a stream of liquefied natural gas (LNG) by extracting a natural gas liquid from the stream of liquefied natural gas.
  • LNG liquefied natural gas
  • the resulting stream of deriched liquefied natural gas can be in liquid and/or vapour phase for instance utilizing subsequent regasification.
  • deriching is used in the present specification and claims as an opposite term for enriching, and is understood to include a meaning of removing hydrocarbon compounds higher than methane, i.e. "stripping" or "making leaner".
  • natural gas liquid is understood to include hydrocarbon compounds higher than methane, including ethane, ethylene, propane, propylene, butane and isomeric variations thereof, and butylenes and isomeric variations thereof.
  • liquefied natural gas typically contains higher hydrocarbon compounds including ethane, propane, and various isomeric forms of butane. These additional compounds have higher heating values than methane. Different specifications of liquefied natural gas, in particular with regard to heating value, are demanded in various markets.
  • US patent 6,604,380 discloses such a method for the recovery of natural gas liquids.
  • a liquefied natural gas feed stream is split.
  • one portion of the split stream is heated in a heat exchanger whereby it is partially vapourised and then fed to a feed separator.
  • a natural gas liquid rich bottom stream is removed from the feed separator and routed to a second separation method including a stabilizer.
  • the other portion of the split stream bypasses the heat exchanger and is fed at a very low temperature of around -157 °C (-250 °F) as an external reflux into the second separation method.
  • the methane-rich overhead vapour streams are drawn from the feed separator and the stabilizer, and combined and directed through the heat exchanger where it is cooled against the one portion of the split feed stream.
  • WO 2004/109180 discloses a method of processing LNG in a plant in which a heat source vaporizes pressurized LNG which is subsequently expanded to produce work in an open power cycle.
  • One or more of the above and other objects may be achieved according to the present invention by providing a method of deriching a stream of liquefied natural gas by extracting a natural gas liquid from the stream of liquefied natural gas, the method at least comprising the steps of:
  • An advantage of the present invention is that it provides more flexibility in choosing the temperature profile in the distillation column, which facilitates efficient control of the method conditions in the distillation column.
  • the overhead vapour stream from the distillation column is partially condensed during the cooling in the second heat exchanger arrangement and the intermediate deriched stream comprises an intermediate condensate which can be passed to the distillation column via the third feeding point, and an intermediate vapour which can be passed to the first heat exchanger arrangement.
  • a further advantage is that the intermediate condensate is enriched in heavier components including natural gas liquids. Instead of submitting this condensate to the first heat exchanger arrangement it is re-submitted to the distillation column as an internal reflux. Hence the recovery of the natural gas liquid is significantly improved.
  • an intermediate temperature can be chosen in the intermediate deriched stream that allows to tailor the composition of the condensate.
  • Another advantage of the invention is that the heating and cooling upstream respectively downstream of the distillation column is performed in at least two stages.
  • the resulting intermediate streams between the at least two stages are thus available for use in the method in addition to the fully heated respectively cooled streams.
  • One way of utilizing the intermediate feed stream is as an external reflux having a temperature that is lower than that of the portion being fed to the distillation column via the second feeding point but not as low as that of the original feed stream.
  • an external reflux stream having a temperature as low as of liquefied natural gas (approximately of around -157 °C, or less than -140 °C) is not generally required for an efficient separation of natural gas liquid components from liquefied natural gas.
  • An advantage of the invention is that the temperature of the external reflux can be chosen higher than the temperature of the feed stream, for instance higher than -140 °C.
  • equipment such as the distillation column or a reboiler (if provided), can be smaller sized, and less power needs to be dissipated in a reboiler.
  • the high-quality cold in the feed stream thus becomes available fully for recondensating the deriched natural gas.
  • the intermediate feed stream can either be fully liquid or partly vapourized.
  • the heating of the feed stream in the first heat exchanger arrangement comprises partly vapourizing the feed stream whereby the intermediate feed stream comprises a mixture of liquid intermediate feed fraction and vaporous intermediate feed fraction
  • the intermediate feed stream comprises a mixture of liquid intermediate feed fraction and vaporous intermediate feed fraction
  • the vaporous intermediate feed fraction because of it relatively low temperature compared to the temperature after the second heating, is already relatively lean from natural gas liquids and does not have to be further distilled. It can be mixed in with a final product stream.
  • the present invention provides a deriched natural gas stream obtained by the method according to the present invention as well as an apparatus suitable for performing the method according to the present invention.
  • Preferred embodiments for the apparatus are derivable from preferred embodiments of the method and/or from the detailed description of embodiments set out below.
  • Figure 1 schematically shows an apparatus for deriching a stream of liquefied natural gas by extracting a natural gas liquid from the stream of liquefied natural gas.
  • a feed line 1 is connectable to a source of the liquefied natural gas.
  • An optional pump 3 is provided in the feed line 1, of which the high-pressure outlet is in fluid communication with a first heat exchanger arrangement 5 via line 2.
  • An intermediate feed line 7 fluidly connects a first outlet 6 of the first heat exchanger arrangement 5 with a distributor 14.
  • the distributor 14 has two outlets connected to lines 17 and 19. If desired, the distributor 14 may have more than two outlets.
  • Line 17 connects to a distillation column 21 via an optional first control valve 23 and a first feeding point 25 provided in an upper part of the distillation column 21.
  • the other line, line 19, also connects to the distillation column 21 but via a second heat exchanger arrangement 26, line 20, which can be optionally provided with a second control valve 27, and a second feeding point 29.
  • the first outlet 6 of the first heat exchanger arrangement 5 is in fluid communication with the second heat exchanger arrangement 26.
  • Line 17 bypasses the second heat exchanger arrangement 26.
  • the second feeding point 29 of the distillation column 21 is preferably located gravitationally lower than the first feeding point 25.
  • the distillation column 21 has a lower portion provided with a discharge opening 31 for withdrawing a liquid stream 35 from the distillation column 21.
  • An optional reboiler 33 may be provided in line 35 connecting to the discharge opening 31.
  • a reboil return line 37 feeds back from the reboiler 33 into the lower portion of the distillation column 21.
  • the optional reboiler 33 may be integrated with the distillation column 21 instead of the shown external arrangement.
  • a line 38 connects to line 35 or to the optional reboiler 33 for discharging the natural gas liquid.
  • the distillation column 21 also has an upper portion provided with an overhead vapour outlet 39.
  • the overhead vapour outlet 39 is in fluid communication with the first heat exchanger arrangement 5 via the second heat exchanger arrangement 26.
  • Line 40 extends between the overhead vapour outlet 39 and the second heat exchanger arrangement 26, and is connected to line 48 that extends between the second heat exchanger arrangement 26 and the first heat exchanger arrangement 5, and is connected to line 55 downstream of the first heat exchanger arrangement 5 via a second outlet 41 of the first heat exchanger arrangement 5.
  • An optional pump 65 can be included in line 55, which discharges into line 67, for increasing the pressure to produce a deriched liquefied natural gas stream at a pressure according to a local specification.
  • Line 67 can be connected to any type of re-gasification system, including systems known from an article "Integrated gas processing with various LNG sources” by Joseph Cho et al, as published in LNG Journal January/February 2005 pp 23-27 .
  • the above-described apparatus is capable of deriching a stream of liquefied natural gas by extracting a natural gas liquid from the stream of liquefied natural gas.
  • An optional bypass line 59 can be provided to fluidly connect line 1 or the high-pressure outlet of pump 3 upstream of the first heat exchanger arrangement 5 with line 55 downstream of the first heat exchanger arrangement 5.
  • the optional bypass line 59 can be provided with a control valve 61. With the bypass line 59 the deriching arrangement can be bypassed and the extraction of the natural gas liquid avoided.
  • the apparatus of Figure 1 works as follows.
  • a feed stream containing the stream of liquefied natural gas is supplied via feed line 1 and heated in the first heat exchanger arrangement 5 against an intermediate deriched stream in line 48 to form an intermediate feed stream 7.
  • the intermediate feed stream 7 is split in the distributor 14 into at least a first portion 17 and a second portion 19.
  • the first portion 7 is passed to the distillation column 21 and fed into it via the first feeding point 25.
  • Pressure and temperature can be controlled utilizing control valve 23.
  • the second portion 19 of the intermediate feed stream 7 is passed to the second heat exchanger arrangement 26 wherein it is further heated, against an overhead stream in line 40.
  • the resulting further heated stream is then supplied to the distillation column 21 via line 20 and the second feeding point 29. Pressure can be controlled employing control valve 27.
  • the second portion 19 of the intermediate feed stream 7 is at least partially vapourised. It is generally recommended to vapourize to a molar fraction of at least 60%.
  • the first portion 17 acts as an external reflux stream in the distillation process. It helps scrubbing the natural gas liquid from vapour generated from the second portion 19 as well as in optional reboiler 33. The scrubbing is facilitated by the preference that the first feeding point 25 is located gravitationally higher than the second feeding point 29.
  • a liquid stream containing the natural gas liquid is then withdrawn from a lower portion of the distillation column 21 via the discharge opening 31 into line 35.
  • the liquid stream is heated and partly fed back via line 37 to the lower portion of the distillation column 21 to allow some vapour to form containing relatively lighter molecules.
  • the remainder is discharged as natural gas liquid into line 38.
  • an overhead vapour stream 40 is withdrawn from an upper portion of the distillation column 21.
  • the overhead vapour stream 40 is a deriched stream containing mainly methane and sometimes also other components such as for instance ethane and a remainder of propane.
  • the overhead vapour stream 40 is passed to the second heat exchanger arrangement 26 where it is cooled against the intermediate feed stream to form an intermediate deriched stream 48 of which at least a portion is thereafter passed to the first heat exchanger arrangement 5 and further cooled against the feed stream 1 to form a product stream 55 of deriched natural gas.
  • the product stream 55 can be fully re-condensed.
  • the product stream 55 is combined with a bypass stream drawn from the feed stream 2 via line 59.
  • the pressure of the product stream in line 55 can then be raised to a desired pressure level by means of the optional pump 65, which is generally more energy efficient as the stream in line 55 generally tends to be fully condensed.
  • the product stream is discharged through line 67 after which it can be further processed (not shown), for instance including re-gasification by heating it to convert it into a gaseous stream.
  • an optional compressor (not shown) can be provided in line 40 to be able to generate a comfort margin in the pressure to ensure that the product stream in line 55 leaving the first heat exchanger arrangement 5 at outlet 41 is not only fully re-condensed but also sub-cooled to a sufficient degree. This is of less importance when a substantial amount of the feed stream 2 is allowed to bypass via line 59, as in that case the product stream leaving the first heat exchanger arrangement 5 is subjected to direct heat exchange.
  • An advantage of having two heat exchanger arrangements 5,26 is that the intermediate streams 7 and/or 48 are now available for use in the process.
  • a portion (first portion 17) of the intermediate stream 7 is utilized as external reflux having a temperature that is lower than that of the portion (second portion 19) being fed to the distillation column 21 via the second feeding point 29 but not as low as the feed stream 1.
  • increased temperature control is achieved over the reflux stream 17 and the further heated feed stream 20, as compared to what is possible in the process as described in US patent 6,604,380 .
  • This increased flexibility enables efficient control of the process conditions in the distillation column 21, to achieve desired separation between overhead stream 40 and bottom stream 38 of a selected natural gas liquid component.
  • FIG 2 is based on the process as shown and explained above with reference to Figure 1 and shows a gas/liquid separator 9 (referred to in the claims as "second gas/liquid separator") that is arranged in the connection between the first outlet 6 of the first heat exchanger arrangement 5 and the distributor 14.
  • the gas/liquid separator is here provided in the form of a feed separation vessel 9.
  • the first outlet 6 of the first heat exchanger arrangement 5 is connected with the feed separation vessel 9.
  • the feed separation vessel 9 has a bottom outlet 11 and an overhead outlet 13.
  • the bottom outlet 11 is connected to the distributor 14 via line 15.
  • the overhead outlet 13 is fluidly connected to line 48 via line 57 upstream of the first heat exchanger arrangement 5.
  • the vapour will contain predominantly the leaner components such as methane.
  • the components with higher heating values, such as propane will still be essentially fully in the liquid phase together with ethane and methane.
  • the vapourised fraction does not have to be further distilled and can be mixed in with the distilled stream in line 48 to be recondensed in the first heat exchanger arrangement 5.
  • the molar fraction of vapour can be between 1 and 90%.
  • the liquid that is drawn from the bottom outlet 11 of the separator 9 is led to the distributor 14, where part of it is sent to the distillation 21 column via line 17 as an external reflux thereby bypassing the second heat exchanger arrangement 26.
  • An advantage of this process is that the external reflux is fully liquid so that it can be fully effective as scrubbing medium.
  • the temperature of the external reflux is lower than that of the portion being fed to the distillation column via the second feeding point 29, but not as low as that of the original feed stream 1.
  • the temperature can be controlled by choosing the amount of heat exchange in the first heat exchanger 5, optionally in co-dependence of controlling the amount of expansion in control valve 23.
  • An advantage of the optional control valves 23 and 27 is that the distillation column 21 is operated at a lower pressure than the feed separator 9, which improves the separation efficiency of natural gas liquid components in the column 21.
  • an optional overhead compressor 63 can be provided between the overhead vapour outlet 39 of the distillation column 21 and the second heat exchanger arrangement 26.
  • the optional pressure drop over valves 23 and 27 can be compensated whereby the pressure in line 48 can be brought to the pressure level as set by the feed stream in line 7.
  • the compressor 63 upstream of the second heat exchanger arrangement 26, because the overhead stream 40 is by virtue of the distillation column 21 always fully vaporous whereas downstream of the second heat exchanger arrangement 26 the product stream can be of a multi-phase nature.
  • FIG. 1 shows an embodiment according to the present invention which is based on the embodiment as shown and explained above with reference to Figure 1 , wherein an internal reflux system is provided in the connection line 48 between the distillation column's overhead vapour outlet 39 and the first heat exchanger arrangement 5.
  • the reflux system here shown comprises a gas/liquid separator (referred to in the claims as "first gas/liquid separator") here provided in the form of a reflux separation vessel 43.
  • the reflux separation vessel 43 is arranged downstream of the second heat exchanger arrangement 26 in line 48 and connected to the second heat exchanger arrangement 26 via line 42.
  • the separator 43 has a bottom outlet 45 and an overhead outlet 47.
  • the bottom outlet 45 is connected to the distillation column 21 via line 49 and a third feeding point 51 to provide a reflux stream.
  • An optional control valve 53 can be provided in line 49.
  • the third feeding point 51 is best arranged gravitationally higher than the second feeding point 29, as the temperature of the reflux stream 49 is generally lower than that of the further heated feed stream 20, and gravitationally lower than the first feeding point 25.
  • the overhead outlet 47 of the reflux separation vessel 43 is fluidly connected with the first heat exchanger arrangement 5 via line 48.
  • the mass selectivity of the reflux stream can be tailored by choice of that temperature, and optionally also the pressure drop in optional valve 53.
  • methane or ethane is unnecessarily circulated through the column thereby merely consuming energy but not increasing the production of deriched natural gas leaving the process via line 55.
  • Figure 4 shows a preferred embodiment according to the present invention, wherein the processes and apparatuses as illustrated in Figures 2 and 3 are combined. For a description of the details, reference is made to the above descriptions of Figures 1 , 2 , and 3 .
  • Table I shows recommended lower and upper limits of temperatures and pressures of the streams through various lines in the process, as well as a typical value of temperature and pressure in a particular example of operation.
  • Table I Line T-low (°C) T-up (°C) T (°C) P-low (bar) P-up (bar) P (bar) 1 -162 -120 -161 1.0 1.5 1.1 2 -162 -120 -161 5 50 33 7, 15, 17, 57 -140 -50 -81 5 50 33 20 -70 -20 -37 5 50 33 38 -10 150 90 2 45 29 40 -90 -10 -28 2 45 29 42, 48, 49 -60 -30 -49 5 50 33 55 -110 -162 -128 5 50 33 66 -40 0 -19 5 50 33 67 -110 -162 -140 20 140 70
  • the molar fraction of vapour in line 7 was 66%, and in line 42 it was 69%.
  • the molar fraction of vapour in line 20 was 75%. It has been predicted on the basis of mass-balance calculations that the apparatus and process of Figure 4 provide an efficient means for recovering natural gas liquid components from the liquefied natural gas feed stream in excess of 90%.
  • the heat exchanger arrangements can comprise one heat exchanger, or a plurality of heat exchangers in parallel and/or in series.

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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)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)

Claims (15)

  1. Procédé d'appauvrissement d'un courant de gaz naturel liquéfié (1) par l'extraction d'un liquide de gaz naturel (35) d'un courant de gaz naturel liquéfié, le procédé comprenant au moins les étapes suivantes :
    - le chauffage d'un courant d'alimentation (1) contenant le courant de gaz naturel liquéfié dans un premier ensemble échangeur de chaleur (5) pour former un courant d'alimentation intermédiaire (7) ;
    - la séparation du courant d'alimentation intermédiaire (7) en au moins une première partie (17) et une deuxième partie (19) ;
    - le passage de la première partie (17) dans une colonne de distillation (21) et son introduction (17) par un premier point d'alimentation (25) ;
    - le passage de la deuxième partie (19) dans un deuxième ensemble échangeur de chaleur (26), dans lequel elle est davantage chauffée, puis son introduction (20) dans la colonne de distillation (21) par un deuxième point d'alimentation (29) ;
    - le retrait d'un courant liquide (35) contenant le liquide de gaz naturel à partir d'une partie inférieure de la colonne de distillation (21) ;
    - le retrait d'un courant de vapeur de tête (40) à partir d'une partie supérieure de la colonne de distillation (21) ;
    - le passage du courant de vapeur de tête (40) dans le deuxième ensemble échangeur de chaleur (26) où il est refroidi contre la deuxième partie (19) du courant d'alimentation intermédiaire (7) pour former un courant appauvri intermédiaire (48) dont au moins une partie est passée par la suite dans le premier ensemble échangeur de chaleur (5) et davantage refroidi contre le courant d'alimentation (1) pour former un courant de produit de gaz naturel appauvri (55) ;
    caractérisé en ce que lors du refroidissement du courant de vapeur de tête (40) dans le deuxième ensemble échangeur de chaleur (26), il est partiellement condensé pour former un condensat intermédiaire dont au moins une partie (49) est passée dans la colonne de distillation (21) par un troisième point d'alimentation (51), et une vapeur intermédiaire qui est passée dans le premier ensemble échangeur de chaleur (5).
  2. Procédé selon la revendication 1, dans lequel ledit chauffage du courant d'alimentation dans le premier ensemble échangeur de chaleur (5) comprend la vaporisation partielle du courant d'alimentation, moyennant quoi le courant d'alimentation intermédiaire (7) comprend un mélange contenant une fraction liquide d'alimentation intermédiaire et une fraction vaporeuse d'alimentation intermédiaire ; et dans lequel au moins la fraction liquide d'alimentation intermédiaire (15) est séparée en au moins la première et la deuxième partie (17, 19).
  3. Procédé selon la revendication 2, dans lequel le mélange est passé dans un récipient de séparation d'alimentation (9) à partir duquel la fraction liquide d'alimentation intermédiaire (15) et la fraction vaporeuse d'alimentation intermédiaire (57) sont respectivement retirées avant de la séparer en les au moins première et deuxième parties (17, 19).
  4. Procédé selon l'une quelconque des revendications précédentes, dans lequel le deuxième point d'alimentation (29) est situé plus bas d'un point de vue de la pesanteur que le premier point d'alimentation (25).
  5. Procédé selon l'une quelconque des revendications précédentes, dans lequel le troisième point d'alimentation (51) est plus bas d'un point de vue de la pesanteur que le premier point d'alimentation (25).
  6. Procédé selon l'une quelconque des revendications précédentes, dans lequel le troisième point d'alimentation (51) est plus haut d'un point de vue de la pesanteur que le deuxième point d'alimentation (29).
  7. Procédé selon l'une quelconque des revendications précédentes, dans lequel le courant de vapeur de tête (40) est comprimé avant d'être passé dans le deuxième ensemble échangeur de chaleur (26).
  8. Procédé selon l'une quelconque des revendications précédentes, dans lequel le courant de produit de gaz naturel appauvri est ensuite regazéifié.
  9. Appareil permettant d'appauvrir un courant de gaz naturel liquéfié (1) par l'extraction d'un liquide de gaz naturel (35) d'un courant de gaz naturel liquéfié, l'appareil comprenant au moins :
    - un premier ensemble échangeur de chaleur (5) conçu pour recevoir un courant d'alimentation (1) contenant le courant de gaz naturel liquéfié et pourvu d'un orifice de sortie (6) servant à évacuer un courant d'alimentation intermédiaire (7) ;
    - un deuxième ensemble échangeur de chaleur (26) en communication fluidique avec l'orifice de sortie (6) du premier ensemble échangeur de chaleur (5) ;
    - une colonne de distillation (21) ayant au moins un premier, un deuxième et un troisième point d'alimentation (25, 29, 51), une partie inférieure pourvue d'une ouverture d'évacuation (31) pour retirer un courant liquide (35) contenant le liquide de gaz naturel, et une partie supérieure pourvue d'un orifice de sortie de vapeur de tête (39) en communication fluidique avec le premier ensemble échangeur de chaleur (5) via au moins le deuxième ensemble échangeur de chaleur (26) ; et
    - un distributeur (14) raccordé à l'orifice de sortie (6) du premier ensemble échangeur de chaleur (5), le distributeur (14) ayant un premier orifice de sortie (6) raccordé au premier point d'alimentation (25) de la colonne de distillation (21), et un deuxième orifice de sortie raccordé au deuxième point d'alimentation (29) de la colonne de distillation (21) via le deuxième ensemble échangeur de chaleur (26) ;
    caractérisé en ce que l'appareil comprend en outre :
    - un premier séparateur de gaz/liquide (43) en aval de l'orifice de sortie de vapeur de tête (39) et entre le deuxième ensemble échangeur de chaleur (26) et le premier ensemble échangeur de chaleur (5), le premier séparateur (43) ayant un orifice de sortie (45) raccordé au troisième point d'alimentation (51) de la colonne de distillation (21) et un orifice de sortie (47) en communication fluidique avec le premier ensemble échangeur de chaleur (5).
  10. Appareil selon la revendication 9, comprenant en outre un deuxième séparateur de gaz/liquide (9) ayant un orifice d'entrée raccordé à l'orifice de sortie (6) du premier échangeur de chaleur (5) et un orifice de sortie inférieur (11) raccordé au distributeur (14).
  11. Appareil selon la revendication 9 ou 10, comprenant en outre un compresseur (63) entre l'orifice de sortie (39) de la colonne de distillation (21) et le deuxième ensemble échangeur de chaleur (26).
  12. Procédé d'extraction d'un liquide de gaz naturel (35) par le procédé selon la revendication 1.
  13. Procédé selon la revendication 12, dans lequel ledit chauffage du courant d'alimentation dans le premier ensemble échangeur de chaleur (5) comprend la vaporisation partielle du courant d'alimentation, moyennant quoi le courant d'alimentation intermédiaire (7) comprend un mélange contenant une fraction liquide d'alimentation intermédiaire et une fraction vaporeuse d'alimentation intermédiaire ; et dans lequel au moins la fraction liquide d'alimentation intermédiaire (15) est séparée en au moins la première et la deuxième partie (17, 19), et dans lequel le mélange est passé dans un récipient de séparation d'alimentation (9) à partir duquel la fraction liquide d'alimentation intermédiaire (15) et la fraction vaporeuse d'alimentation intermédiaire (57) sont respectivement retirées avant de la séparer en les au moins première et deuxième parties (17, 19).
  14. Procédé selon l'une quelconque des revendications 12 à 13, dans lequel le deuxième point d'alimentation (29) est situé plus bas d'un point de vue de la pesanteur que le premier point d'alimentation (25), et/ou dans lequel le troisième point d'alimentation (51) est plus bas d'un point de vue de la pesanteur que le premier point d'alimentation (25), et/ou dans lequel le troisième point d'alimentation (51) est plus haut d'un point de vue de la pesanteur que le deuxième point d'alimentation (29).
  15. Procédé selon l'une quelconque des revendications 12 à 14, dans lequel le courant de vapeur de tête (40) est comprimé avant d'être passé dans le deuxième ensemble échangeur de chaleur (26).
EP06708800.5A 2005-03-22 2006-03-20 Procédé et dispositif pour séparer des liquides de gaz naturel à partir d'un courant de gaz naturel liquéfié Active EP1861671B1 (fr)

Priority Applications (1)

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Applications Claiming Priority (3)

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EP05102252 2005-03-22
PCT/EP2006/060867 WO2006100218A1 (fr) 2005-03-22 2006-03-20 Procede et dispositif permettant d'appauvrir un flux de gaz naturel liquefie
EP06708800.5A EP1861671B1 (fr) 2005-03-22 2006-03-20 Procédé et dispositif pour séparer des liquides de gaz naturel à partir d'un courant de gaz naturel liquéfié

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US20080264100A1 (en) * 2004-06-30 2008-10-30 John Mak Lng Regasification Configurations and Methods
US20080148771A1 (en) * 2006-12-21 2008-06-26 Chevron U.S.A. Inc. Process and apparatus for reducing the heating value of liquefied natural gas
BRPI0924594B1 (pt) * 2009-04-07 2020-12-29 Twister B.V. sistema de separação, sistema de processamento, método para separar um fluxo de fluido, e, métodos para processar um fluido
EP3604222A1 (fr) * 2018-07-30 2020-02-05 Evonik Operations GmbH Procédé de purification de cyanure d'hydrogène

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RU2386091C2 (ru) 2010-04-10
US20090056371A1 (en) 2009-03-05
ES2561808T3 (es) 2016-03-01
RU2007138916A (ru) 2009-04-27
WO2006100218A1 (fr) 2006-09-28
JP5411496B2 (ja) 2014-02-12
JP2008535961A (ja) 2008-09-04
EP1861671A1 (fr) 2007-12-05

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