US20080066493A1 - Treating Liquefied Natural Gas - Google Patents

Treating Liquefied Natural Gas Download PDF

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Publication number
US20080066493A1
US20080066493A1 US11/632,137 US63213705A US2008066493A1 US 20080066493 A1 US20080066493 A1 US 20080066493A1 US 63213705 A US63213705 A US 63213705A US 2008066493 A1 US2008066493 A1 US 2008066493A1
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stream
fuel gas
column
pressure
recycle stream
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Cornelis Buijs
Johan Barend Pek
Robert Nagelvoort
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Shell USA Inc
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Assigned to SHELL OIL COMPANY reassignment SHELL OIL COMPANY ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: PEK, JOHAN JAN BAREND, KLEIN NAGELVOORT, ROBERT, BUIJS, CORNELIS
Publication of US20080066493A1 publication Critical patent/US20080066493A1/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
    • 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
    • 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
    • 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
    • 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
    • F25J2200/40—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
    • F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
    • 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
    • F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator 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
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/30—Dynamic liquid or hydraulic expansion with extraction of work, e.g. single phase or two-phase turbine
    • 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
    • F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
    • 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
    • F25J2270/04—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
    • F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle
    • 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.
    • 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
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • the present invention relates to treating liquefied natural gas, and in particular treating liquefied natural gas that contains components having boiling-points lower than methane.
  • An example of such a component is nitrogen.
  • the expressions ‘low boiling point components’ and ‘components having low boiling points’ will be used to refer to components having boiling points lower than methane.
  • the treatment is directed to removing low boiling point components from the liquefied natural gas in order to obtain a liquefied natural gas having a reduced content of components having low boiling points.
  • the improved method can be applied in two ways: (1) to treat the same amount of liquefied natural gas as in a conventional method, or (2) to treat a larger amount of liquefied natural gas as in a conventional method.
  • the content of low boiling point components in the liquefied gas treated with the method of the present invention is lower than that in liquefied gas treated with a conventional method.
  • the content of low boiling point components is maintained and the amount of liquefied gas is increased.
  • U.S. Pat. No. 6,199,403 discloses a method to remove a high-volatility component such as nitrogen from a feed stream rich in methane. According to U.S. Pat. No. 6,199,403 the expanded liquefied natural gas stream enters a separation column at an intermediate level, i.e. not below a gas-liquid contacting section.
  • U.S. Pat. No. 5,421,165 relates to a process for denitrogenation of a feedstock of a liquefied mixture of hydrocarbons.
  • U.S. Pat. No. 5,421,165 suggests a relatively complicated process using a denitrogenation column comprising a plurality of theoretical fractionation stages.
  • WO 02/50483 discloses several methods of removing components having low boiling points from liquefied natural gas. According to WO 02/50483 a liquid product stream having a reduced content of components having low boiling points is obtained.
  • One or more of the above or other objects are achieved according to the present invention by providing a method of treating liquefied natural gas supplied at liquefaction pressure containing components having low boiling points to obtain a liquid product stream having a reduced content of components having low boiling points, which method comprises the steps of:
  • liquid product stream obtained according to the present invention contains a smaller content of components having low boiling points than one would expect.
  • An important advantage of the method according to the present invention is that it can be suitably used for large liquefaction plants.
  • FIG. 1 shows schematically a process flow scheme illustrating a part of an embodiment of the method of the present invention (not including a flash vessel as required according to the present invention);
  • FIG. 2 shows schematically an alternative of the process of FIG. 1 ;
  • FIG. 3 shows schematically a process flow scheme of a fully elaborated embodiment of the method of the present invention, including a flash vessel;
  • FIG. 4 shows schematically an alternative of the process of FIG. 3 ;
  • FIG. 5 shows schematically and not to scale an alternative to part V of the process flow scheme of FIG. 4 ;
  • FIG. 6 shows the process according to FIG. 4 having two contacting zones.
  • Liquefied natural gas containing components having low boiling points is supplied at liquefaction pressure through conduit 1 to an expansion device in the form of expansion engine 3 and Joule-Thompson valve 5 in the discharge conduit 6 of expansion engine 3 .
  • the expansion device the liquefied gas is allowed to expand to separation pressure, and an expanded two-phase fluid is obtained.
  • the liquefaction pressure is suitably in the range of from 3 to 8.5 MPa and the separation pressure is suitably in the range of from 0.1 to 0.5 MPa.
  • the expanded two-phase fluid is passed through conduit 9 to a column 10 .
  • the expanded two-phase fluid is introduced into the column 10 at separation pressure via a suitable inlet device, such as vane inlet device 12 .
  • the vane inlet device also known as schoepentoeter, allows efficient separation of gas and liquid.
  • the column 10 is provided with a gas-liquid contacting section 14 .
  • the contacting section 14 may comprise any suitable means for contacting a gas and a liquid, such as trays and packings.
  • the contacting section 14 consists of between two and eight horizontal contacting trays 15 .
  • the expanded two-phase fluid is introduced into the column 10 below the gas-liquid contacting section 14 .
  • the person skilled in the art will readily understand that the column may comprise two or more contacting sections 14 .
  • liquid from the two-phase fluid is collected, and a liquid stream having a reduced content of components having low boiling points is removed from the bottom 16 through conduit 17 and pumped by pump 18 to a storage tank 20 .
  • a liquid product stream is removed through conduit 21 and a gaseous stream through conduit 22 .
  • the gaseous stream is also known as boil-off gas.
  • Vapor from the two-phase fluid to flow through the contacting section 14 Vapor from the two-phase fluid to flow through the contacting section 14 .
  • a gaseous stream that is enriched in components having low boiling points is removed through conduit 25 .
  • the gaseous stream is heated in a heat exchanger 27 to obtain a heated gaseous stream that is passed through conduit 28 to a compressor 30 .
  • compressor 30 the heated gaseous stream is compressed to fuel gas pressure to obtain fuel gas.
  • the fuel gas is removed through conduit 31 and cooled in heat exchanger 32 to remove the heat of compression.
  • the fuel gas is passed away through conduit 33 .
  • the fuel gas pressure is in the range of from 1 to 3.5 MPa.
  • the recycle stream is at least partly condensed to obtain a reflux stream, which is passed to the column 10 through the conduit 34 b provided with Joule-Thompson valve 37 .
  • the reflux stream is introduced at separation pressure into the column 10 via inlet device, such as vane inlet device 39 above the contacting section 14 .
  • Table 1 summarizes the result of a hypothetical example, wherein the method of FIG. 1 is compared to a base case.
  • the recycle stream and the feed are introduced into the column at the same level, so that the liquid phases of the two streams are mixed before introduction thereof in the column and the column has no contacting section. It was found that the liquid stream withdrawn through conduit 17 for the base case contains more nitrogen than the same stream for the present invention.
  • TABLE 1 Summary of hypothetical example with the embodiment of FIG. 1 .
  • Embodiment of Base case Number of trays in 3 — contacting section Flow rate feed 190.86 kg/s 190.86 kg/s through conduit 9 Temperature of ⁇ 145° C. ⁇ 145° C.
  • Table 1 shows that a lower nitrogen content in the product stream is obtained with the method of the present invention.
  • the recycle stream separated from the fuel gas is additionally compressed in an auxiliary compressor to an elevated pressure before it is at least partly condensed in heat exchanger 27 .
  • the high-pressure recycle stream can be used in several ways, which will be discussed with reference to FIG. 2 . The parts that were already discussed with reference to FIG. 1 have got the same reference numerals.
  • the auxiliary compressor included in conduit 34 a is referred to with reference numeral 35 .
  • the auxiliary compressor 35 can be provided with a cooler (not shown) to remove the heat of compression for the compressed recycle stream.
  • the compressed recycle stream is at least partly condensed by cooling it in heat exchanger 27 . Part of the cold that is needed is provided by the gaseous stream that is enriched in components having low boiling points that is passed through conduit 25 . The remainder is provided by the recycle stream.
  • Cold from the recycle stream can be obtained by expanding a part of the recycle stream to an intermediate pressure in Joule-Thompson valve 38 , using the expanded fluid to cool the recycle stream in conduit 34 a and supplying the expanded fluid through conduit 38 a to the compressor 30 .
  • the intermediate pressure to which the part of the recycle stream is expanded is in the range of from the suction pressure to the discharge pressure of the compressor 30 (ends of the range included).
  • the stage at which the expanded recycle stream enters the compressor 30 is so selected that the pressure of the expanded recycle stream matches the pressure of the fluid in the compressor 30 in that stage.
  • the remainder of the recycle stream is expanded by the Joule-Thompson valve 37 and introduced as reflux in the column 10 as discussed with reference to FIG. 1 .
  • An advantage of the embodiment discussed with reference to FIG. 2 is that the recycle stream is expanded from a larger pressure and thus cooled to a lower temperature. This allows a warmer feed stream, for example a feed stream at ⁇ 142° C., compared to a feed stream temperature of ⁇ 145° C. (in the above example). Thus the temperature of the liquefied gas from the main cryogenic heat exchanger can be higher and therefore, for the same amount of energy, more gas can be liquefied.
  • the elevated pressure of the fluid discharged from the auxiliary compressor 35 is so selected that the costs of the power required to drive the auxiliary compressor 35 are less than the value of the increased amount of gas that is liquefied.
  • the expansion is done in the expansion valves 37 and 38 .
  • the expansion of the recycle stream can be done in two stages, at first in an expansion device, such as expander 36 and subsequently in the Joule-Thompson valves 37 and 38 .
  • the expanded fluid can be supplied to an inlet (not shown) of the compressor 35 .
  • this step comprises collecting in the bottom of the column liquid from the two-phase fluid and withdrawing from the bottom of the column a liquid stream having a reduced content of components having low boiling points; introducing the liquid stream into a flash vessel at a low pressure; removing a second gaseous stream from the top of the flash vessel; and removing from the bottom of the flash vessel a liquid stream to obtain the liquid product stream.
  • the column 10 ′ comprises an upper part 10 u and a lower part 10 l, wherein the upper part performs the function of the column 10 in FIG. 1 and the lower part 10 l is a flash vessel operating at a pressure that is below the pressure in the upper part 10 u.
  • the pressure in the upper part 10 u is in the range of from 0.2 to 0.5 MPa and the pressure in the flash vessel 10 l in the range of from 0.1 to 0.2 MPa.
  • the flash vessel 10 l may be a component that is physically separated from the column 10 l (i.e. at a certain distance).
  • liquid from the two-phase fluid supplied through conduit 9 is collected in the bottom 16 ′ of the upper part 10 u of the column 10 ′. From that bottom 16 ′ is withdrawn a liquid stream having a reduced content of components having low boiling points through conduit 17 ′. This stream is then introduced into the flash vessel 10 l at a low pressure. The pressure reduction is achieved by means of Joule-Thompson valve 40 in conduit 17 ′. Consequently a two-phase mixture is formed and that is introduced via inlet device 41 into the flash vessel 10 l.
  • the second gaseous stream is passed through conduit 42 to heat exchanger 27 , in which the second gaseous stream is heated by heat exchange with the recycle stream supplied through conduit 34 a.
  • the heated stream is compressed in compressor 45 , the heat of compression is removed in heat exchanger 48 and passed through conduit 49 to add the compressed second gaseous stream to the recycle stream in conduit 34 a.
  • compressors 45 and 30 can be combined into one compressor (not shown).
  • conduit 42 is connected to the suction end of that compressor
  • conduit 28 to an intermediate inlet
  • conduit 32 is connected to the discharge end of that compressor.
  • An advantage of this method is that it can be used for large liquefaction plants.
  • the embodiment discussed with reference to FIG. 3 can as well be provided with an auxiliary compressor to compress the recycle stream separated from the fuel gas to an elevated pressure before it is at least partly condensed in heat exchanger 27 .
  • the high-pressure recycle stream can be used in several ways, which will be discussed with reference to FIG. 4 . The parts that were already discussed with reference to FIG. 3 have got the same reference numerals.
  • the auxiliary compressor included in conduit 34 a is referred to with reference numeral 35 .
  • the auxiliary compressor 35 can be provided with a cooler (not shown) to remove the heat of compression for the compressed recycle stream.
  • the compressed recycle stream is partially condensed by cooling it in heat exchanger 27 . Part of the cold that is needed is provided by the gaseous stream that is enriched in components having low boiling points that is passed through conduit 25 . The remainder is provided by the recycle stream.
  • Cold from the recycle stream can be obtained by expanding a part of the recycle stream to an intermediate pressure in Joule-Thompson valve 38 , using the expanded fluid to cool the recycle stream in conduit 34 a and supplying the expanded fluid through conduit 38 a to the compressor 30 .
  • the intermediate pressure to which the part of the recycle stream is expanded is in the range of from the suction pressure to the discharge pressure of the compressor 30 (ends of the range included).
  • the point at which the expanded recycle stream enters the compressor 30 is so selected that the pressure of the expanded recycle stream matches the pressure of the fluid in the compressor 30 at the inlet point.
  • the remainder of the recycle stream is expanded by the Joule-Thompson valve 37 and introduced as reflux in the column 10 as discussed with reference to FIG. 1 .
  • An advantage of this embodiment is that the recycle stream is expanded from a larger pressure and thus cooled to a lower temperature. This allows a warmer feed stream, for example a feed stream at ⁇ 142° C., compared to a feed stream temperature of ⁇ 145° C. (in the above example). Thus the temperature of the liquefied gas from the main cryogenic heat exchanger can be higher and therefore, for the same amount of energy, more gas can be liquefied.
  • the elevated pressure of the fluid discharged from the auxiliary compressor 35 is so selected that the costs of the power required to drive the auxiliary compressor 35 are less than the value of the increased amount of gas that is liquefied.
  • the expansion is done in the expansion valves 37 and 38 .
  • the expansion of the recycle stream can be done in two stages, at first in an expansion device, such as expander 36 and subsequently in the Joule-Thompson valves 37 and 38 .
  • FIG. 4 also shows that the boil-off gas from the storage tank 20 is provided via the conduit 22 to the suction end of the compressor 45 .
  • compressors 45 and 30 can be combined into one compressor (not shown).
  • conduit 42 into which conduit 22 opens
  • conduit 28 to an intermediate inlet
  • conduit 32 is connected to the discharge end of that compressor.
  • the expanded fluid can be supplied to an inlet (not shown) of the compressor 35 .
  • FIG. 5 An alternative of the embodiment shown in FIG. 4 is shown in FIG. 5 , wherein a part of the recycle stream that is passed through conduit 34 a is separated therefrom and passed through conduit 50 through the heat exchanger 27 . Then the cooled recycle stream is expanded to the intermediate pressure in expander 51 and used to cool the recycle stream in conduit 34 a. The expanded stream is then introduced into the compressor 30 at an intermediate stage.
  • the recycle stream passed through conduit 34 a is between 10 and 90% by mass of the fuel gas that is passed through conduit 31 .
  • FIG. 6 shows the process according to FIG. 4 wherein the column 10 u comprises two contacting sections 14 .
  • the column 10 u comprises two contacting sections 14 .
  • the skilled person will readily understand that more than two contacting sections 14 may be present.
  • a stream is removed via draw off device 63 and fed via line 60 to a heat exchanger 61 , wherein the stream is heat exchanged against the stream in line 1 . Subsequently the stream in line 60 is returned to the column 10 u and fed via vane inlet device 62 .
  • the contacting section 14 contains trays, however, any other contacting means such as packing can be employed as well.
  • the length of the packed section is then preferably equivalent to between two and eight contacting trays for the section above vane inlet device 12 and between five and fifteen trays for the section below draw-off device 63 .
  • the method of the present invention provides a simple way of reducing the amount of components having low boiling points in a liquefied natural gas stream.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
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  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)
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Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011009832A2 (en) 2009-07-21 2011-01-27 Shell Internationale Research Maatschappij B.V. Method for treating a multi-phase hydrocarbon stream and an apparatus therefor
EP2597406A1 (en) * 2011-11-25 2013-05-29 Shell Internationale Research Maatschappij B.V. Method and apparatus for removing nitrogen from a cryogenic hydrocarbon composition
WO2013087569A3 (en) * 2011-12-12 2014-05-01 Shell Internationale Research Maatschappij B.V. Method and apparatus for removing nitrogen from a cryogenic hydrocarbon composition
WO2013087571A3 (en) * 2011-12-12 2014-05-01 Shell Internationale Research Maatschappij B.V. Method and apparatus for removing nitrogen from a cryogenic hydrocarbon composition
WO2013087570A3 (en) * 2011-12-12 2014-05-01 Shell Internationale Research Maatschappij B.V. Method and apparatus for removing nitrogen from a cryogenic hydrocarbon composition
US20150135767A1 (en) * 2013-11-15 2015-05-21 Black & Veatch Holding Company Systems and methods for hydrocarbon refrigeration with a mixed refrigerant cycle
EP3043133A1 (en) * 2015-01-12 2016-07-13 Shell Internationale Research Maatschappij B.V. Method of removing nitrogen from a nitrogen containing stream
WO2017009341A1 (fr) * 2015-07-13 2017-01-19 Technip France Procédé de détente et de stockage d'un courant de gaz naturel liquéfié issu d'une installation de liquéfaction de gaz naturel, et installation associée
US10704830B2 (en) * 2018-01-24 2020-07-07 Gas Technology Development Pte Ltd Process and system for reliquefying boil-off gas (BOG)
US20210063084A1 (en) * 2019-08-28 2021-03-04 Toyo Engineering Corporation Process and apparatus for treating lean lng

Families Citing this family (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
PE20060219A1 (es) * 2004-07-12 2006-05-03 Shell Int Research Tratamiento de gas natural licuado
US8522574B2 (en) * 2008-12-31 2013-09-03 Kellogg Brown & Root Llc Method for nitrogen rejection and or helium recovery in an LNG liquefaction plant
EP2702311B1 (en) * 2011-04-19 2021-06-09 Babcock IP Management (Number One) Limited Method of cooling boil off gas and an apparatus therefor
JP5679201B2 (ja) * 2011-08-08 2015-03-04 エア・ウォーター株式会社 ボイルオフガス中の窒素除去方法およびそれに用いる窒素除去装置
RU2474778C1 (ru) * 2011-09-19 2013-02-10 Сергей Николаевич Кузнецов Теплообменный аппарат для ожижения смешанных паров
DK2638942T3 (da) * 2012-03-15 2017-01-02 Cryostar Sas Tågeseparationsanordning
DE102012008961A1 (de) * 2012-05-03 2013-11-07 Linde Aktiengesellschaft Verfahren zum Rückverflüssigen einer Methan-reichen Fraktion
EP2796818A1 (en) 2013-04-22 2014-10-29 Shell Internationale Research Maatschappij B.V. Method and apparatus for producing a liquefied hydrocarbon stream
BR112015026176B1 (pt) 2013-04-22 2022-05-10 Shell Internationale Research Maatschappij B.V Método e aparelho para produzir uma corrente de hidrocarboneto liquefeito
EP2857782A1 (en) 2013-10-04 2015-04-08 Shell International Research Maatschappij B.V. Coil wound heat exchanger and method of cooling a process stream
EP2957621A1 (en) 2014-06-17 2015-12-23 Shell International Research Maatschappij B.V. De-superheater system and compression system employing such de-superheater system, and method of producing a pressurized and at least partially condensed mixture of hydrocarbons
EP2957620A1 (en) 2014-06-17 2015-12-23 Shell International Research Maatschappij B.V. Method and system for producing a pressurized and at least partially condensed mixture of hydrocarbons
EP2977430A1 (en) 2014-07-24 2016-01-27 Shell Internationale Research Maatschappij B.V. A hydrocarbon condensate stabilizer and a method for producing a stabilized hydrocarbon condenstate stream
EP2977431A1 (en) 2014-07-24 2016-01-27 Shell Internationale Research Maatschappij B.V. A hydrocarbon condensate stabilizer and a method for producing a stabilized hydrocarbon condenstate stream
CN105240064B (zh) * 2015-11-25 2017-06-16 杰瑞石油天然气工程有限公司 一种lng能量回收工艺
RU2626612C2 (ru) * 2015-12-16 2017-07-31 Общество с ограниченной ответственностью "Научно-исследовательский институт природных газов и газовых технологий - Газпром ВНИИГАЗ" Автономная установка очистки сжиженного природного газа (варианты)
US10330363B2 (en) 2016-02-08 2019-06-25 Trane International Inc. Lubricant separator for a heating, ventilation, and air conditioning system

Citations (31)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2500118A (en) * 1945-08-18 1950-03-07 Howell C Cooper Natural gas liquefaction
US2504429A (en) * 1946-04-18 1950-04-18 Phillips Petroleum Co Recovery of hydrocarbons from natural gas
US3203191A (en) * 1960-09-02 1965-08-31 Conch Int Methane Ltd Energy derived from expansion of liquefied gas
US3247649A (en) * 1963-04-29 1966-04-26 Union Oil Co Absorption process for separating components of gaseous mixtures
US3555837A (en) * 1968-02-01 1971-01-19 Phillips Petroleum Co Temperature control of fluid separation systems
US3616652A (en) * 1966-09-27 1971-11-02 Conch Int Methane Ltd Process and apparatus for liquefying natural gas containing nitrogen by using cooled expanded and flashed gas therefrom as a coolant therefor
US4112700A (en) * 1974-08-09 1978-09-12 Linde Aktiengesellschaft Liquefaction of natural gas
US4541852A (en) * 1984-02-13 1985-09-17 Air Products And Chemicals, Inc. Deep flash LNG cycle
US5036671A (en) * 1990-02-06 1991-08-06 Liquid Air Engineering Company Method of liquefying natural gas
US5051120A (en) * 1990-06-12 1991-09-24 Union Carbide Industrial Gases Technology Corporation Feed processing for nitrogen rejection unit
US5325673A (en) * 1993-02-23 1994-07-05 The M. W. Kellogg Company Natural gas liquefaction pretreatment process
US5421165A (en) * 1991-10-23 1995-06-06 Elf Aquitaine Production Process for denitrogenation of a feedstock of a liquefied mixture of hydrocarbons consisting chiefly of methane and containing at least 2 mol % of nitrogen
US5568737A (en) * 1994-11-10 1996-10-29 Elcor Corporation Hydrocarbon gas processing
US5881569A (en) * 1997-05-07 1999-03-16 Elcor Corporation Hydrocarbon gas processing
US5893274A (en) * 1995-06-23 1999-04-13 Shell Research Limited Method of liquefying and treating a natural gas
US5953935A (en) * 1997-11-04 1999-09-21 Mcdermott Engineers & Constructors (Canada) Ltd. Ethane recovery process
US6014869A (en) * 1996-02-29 2000-01-18 Shell Research Limited Reducing the amount of components having low boiling points in liquefied natural gas
US6070429A (en) * 1999-03-30 2000-06-06 Phillips Petroleum Company Nitrogen rejection system for liquified natural gas
US6182468B1 (en) * 1999-02-19 2001-02-06 Ultimate Process Technology Thermodynamic separation of heavier components from natural gas
US6199403B1 (en) * 1998-02-09 2001-03-13 Exxonmobil Upstream Research Company Process for separating a multi-component pressurizied feed stream using distillation
US6401486B1 (en) * 2000-05-18 2002-06-11 Rong-Jwyn Lee Enhanced NGL recovery utilizing refrigeration and reflux from LNG plants
US6449984B1 (en) * 2001-07-04 2002-09-17 Technip Process for liquefaction of and nitrogen extraction from natural gas, apparatus for implementation of the process, and gases obtained by the process
US20020157538A1 (en) * 2001-03-01 2002-10-31 Foglietta Jorge H. Cryogenic process utilizing high pressure absorber column
US20020166336A1 (en) * 2000-08-15 2002-11-14 Wilkinson John D. Hydrocarbon gas processing
US20030136146A1 (en) * 2002-01-18 2003-07-24 Ernesto Fischer-Calderon Integrated processing of natural gas into liquid products
US20040165113A1 (en) * 2002-11-07 2004-08-26 Samsung Electronics Co., Ltd. Apparatus and method for adjusting screen
US20040231359A1 (en) * 2003-05-22 2004-11-25 Brostow Adam Adrian Nitrogen rejection from condensed natural gas
US6898949B2 (en) * 2000-12-18 2005-05-31 Technip France Method for refrigerating liquefied gas and installation therefor
US20050279132A1 (en) * 2004-06-16 2005-12-22 Eaton Anthony P LNG system with enhanced turboexpander configuration
US20070245771A1 (en) * 2005-04-22 2007-10-25 Spilsbury Christopher G Dual stage nitrogen rejection from liquefied natural gas
US20080066492A1 (en) * 2004-07-12 2008-03-20 Cornelis Buijs Treating Liquefied Natural Gas

Family Cites Families (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL197609A (ko) * 1961-06-01
US3625017A (en) * 1968-06-07 1971-12-07 Mc Donnell Douglas Corp Separation of components of hydrogen and hydrocarbon mixtures by plural distillation with heat exchange
JPS5121642B2 (ko) * 1972-12-27 1976-07-03
GB1464558A (en) * 1973-04-13 1977-02-16 Cryoplants Ltd Gas liquefaction process and apparatus
FR2292203A1 (fr) * 1974-11-21 1976-06-18 Technip Cie Procede et installation pour la liquefaction d'un gaz a bas point d'ebullition
US4225329A (en) * 1979-02-12 1980-09-30 Phillips Petroleum Company Natural gas liquefaction with nitrogen rejection stabilization
US4455158A (en) * 1983-03-21 1984-06-19 Air Products And Chemicals, Inc. Nitrogen rejection process incorporating a serpentine heat exchanger
JPH06299174A (ja) * 1992-07-24 1994-10-25 Chiyoda Corp 天然ガス液化プロセスに於けるプロパン系冷媒を用いた冷却装置
DE4235006A1 (de) * 1992-10-16 1994-04-21 Linde Ag Verfahren zum Auftrennen eines im wesentlichen aus Wasserstoff, Methan und C¶3¶/C¶4¶-Kohlenwasserstoffen bestehenden Einsatzstromes
US5438836A (en) * 1994-08-05 1995-08-08 Praxair Technology, Inc. Downflow plate and fin heat exchanger for cryogenic rectification
FR2778232B1 (fr) * 1998-04-29 2000-06-02 Inst Francais Du Petrole Procede et dispositif de liquefaction d'un gaz naturel sans separation de phases sur les melanges refrigerants
FR2841330B1 (fr) * 2002-06-21 2005-01-28 Inst Francais Du Petrole Liquefaction de gaz naturel avec recyclage de gaz naturel
US7581411B2 (en) * 2006-05-08 2009-09-01 Amcs Corporation Equipment and process for liquefaction of LNG boiloff gas

Patent Citations (31)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2500118A (en) * 1945-08-18 1950-03-07 Howell C Cooper Natural gas liquefaction
US2504429A (en) * 1946-04-18 1950-04-18 Phillips Petroleum Co Recovery of hydrocarbons from natural gas
US3203191A (en) * 1960-09-02 1965-08-31 Conch Int Methane Ltd Energy derived from expansion of liquefied gas
US3247649A (en) * 1963-04-29 1966-04-26 Union Oil Co Absorption process for separating components of gaseous mixtures
US3616652A (en) * 1966-09-27 1971-11-02 Conch Int Methane Ltd Process and apparatus for liquefying natural gas containing nitrogen by using cooled expanded and flashed gas therefrom as a coolant therefor
US3555837A (en) * 1968-02-01 1971-01-19 Phillips Petroleum Co Temperature control of fluid separation systems
US4112700A (en) * 1974-08-09 1978-09-12 Linde Aktiengesellschaft Liquefaction of natural gas
US4541852A (en) * 1984-02-13 1985-09-17 Air Products And Chemicals, Inc. Deep flash LNG cycle
US5036671A (en) * 1990-02-06 1991-08-06 Liquid Air Engineering Company Method of liquefying natural gas
US5051120A (en) * 1990-06-12 1991-09-24 Union Carbide Industrial Gases Technology Corporation Feed processing for nitrogen rejection unit
US5421165A (en) * 1991-10-23 1995-06-06 Elf Aquitaine Production Process for denitrogenation of a feedstock of a liquefied mixture of hydrocarbons consisting chiefly of methane and containing at least 2 mol % of nitrogen
US5325673A (en) * 1993-02-23 1994-07-05 The M. W. Kellogg Company Natural gas liquefaction pretreatment process
US5568737A (en) * 1994-11-10 1996-10-29 Elcor Corporation Hydrocarbon gas processing
US5893274A (en) * 1995-06-23 1999-04-13 Shell Research Limited Method of liquefying and treating a natural gas
US6014869A (en) * 1996-02-29 2000-01-18 Shell Research Limited Reducing the amount of components having low boiling points in liquefied natural gas
US5881569A (en) * 1997-05-07 1999-03-16 Elcor Corporation Hydrocarbon gas processing
US5953935A (en) * 1997-11-04 1999-09-21 Mcdermott Engineers & Constructors (Canada) Ltd. Ethane recovery process
US6199403B1 (en) * 1998-02-09 2001-03-13 Exxonmobil Upstream Research Company Process for separating a multi-component pressurizied feed stream using distillation
US6182468B1 (en) * 1999-02-19 2001-02-06 Ultimate Process Technology Thermodynamic separation of heavier components from natural gas
US6070429A (en) * 1999-03-30 2000-06-06 Phillips Petroleum Company Nitrogen rejection system for liquified natural gas
US6401486B1 (en) * 2000-05-18 2002-06-11 Rong-Jwyn Lee Enhanced NGL recovery utilizing refrigeration and reflux from LNG plants
US20020166336A1 (en) * 2000-08-15 2002-11-14 Wilkinson John D. Hydrocarbon gas processing
US6898949B2 (en) * 2000-12-18 2005-05-31 Technip France Method for refrigerating liquefied gas and installation therefor
US20020157538A1 (en) * 2001-03-01 2002-10-31 Foglietta Jorge H. Cryogenic process utilizing high pressure absorber column
US6449984B1 (en) * 2001-07-04 2002-09-17 Technip Process for liquefaction of and nitrogen extraction from natural gas, apparatus for implementation of the process, and gases obtained by the process
US20030136146A1 (en) * 2002-01-18 2003-07-24 Ernesto Fischer-Calderon Integrated processing of natural gas into liquid products
US20040165113A1 (en) * 2002-11-07 2004-08-26 Samsung Electronics Co., Ltd. Apparatus and method for adjusting screen
US20040231359A1 (en) * 2003-05-22 2004-11-25 Brostow Adam Adrian Nitrogen rejection from condensed natural gas
US20050279132A1 (en) * 2004-06-16 2005-12-22 Eaton Anthony P LNG system with enhanced turboexpander configuration
US20080066492A1 (en) * 2004-07-12 2008-03-20 Cornelis Buijs Treating Liquefied Natural Gas
US20070245771A1 (en) * 2005-04-22 2007-10-25 Spilsbury Christopher G Dual stage nitrogen rejection from liquefied natural gas

Cited By (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20120167617A1 (en) * 2009-07-21 2012-07-05 Alexandra Teodora Anghel Method for treating a multi-phase hydrocarbon stream and an apparatus therefor
WO2011009832A2 (en) 2009-07-21 2011-01-27 Shell Internationale Research Maatschappij B.V. Method for treating a multi-phase hydrocarbon stream and an apparatus therefor
WO2013076185A3 (en) * 2011-11-25 2014-05-01 Shell Internationale Research Maatschappij B.V. Method and apparatus for removing nitrogen from a cryogenic hydrocarbon composition
EP2597406A1 (en) * 2011-11-25 2013-05-29 Shell Internationale Research Maatschappij B.V. Method and apparatus for removing nitrogen from a cryogenic hydrocarbon composition
AU2013200643B2 (en) * 2011-11-25 2014-03-20 Shell Internationale Research Maatschappij B.V. Method and apparatus for removing nitrogen from a cryogenic hydrocarbon composition
CN104024774A (zh) * 2011-11-25 2014-09-03 国际壳牌研究有限公司 由低温烃组合物脱除氮的方法和设备
WO2013087571A3 (en) * 2011-12-12 2014-05-01 Shell Internationale Research Maatschappij B.V. Method and apparatus for removing nitrogen from a cryogenic hydrocarbon composition
CN103988035A (zh) * 2011-12-12 2014-08-13 国际壳牌研究有限公司 用于从低温烃类组合物中去除氮气的方法和装置
CN103998882A (zh) * 2011-12-12 2014-08-20 国际壳牌研究有限公司 用于从低温烃类组合物中去除氮气的方法和装置
WO2013087569A3 (en) * 2011-12-12 2014-05-01 Shell Internationale Research Maatschappij B.V. Method and apparatus for removing nitrogen from a cryogenic hydrocarbon composition
AU2012350742B2 (en) * 2011-12-12 2015-08-20 Shell Internationale Research Maatschappij B.V. Method and apparatus for removing nitrogen from a cryogenic hydrocarbon composition
AU2012350743B2 (en) * 2011-12-12 2015-08-27 Shell Internationale Research Maatschappij B.V. Method and apparatus for removing nitrogen from a cryogenic hydrocarbon composition
WO2013087570A3 (en) * 2011-12-12 2014-05-01 Shell Internationale Research Maatschappij B.V. Method and apparatus for removing nitrogen from a cryogenic hydrocarbon composition
US10563913B2 (en) * 2013-11-15 2020-02-18 Black & Veatch Holding Company Systems and methods for hydrocarbon refrigeration with a mixed refrigerant cycle
US20150135767A1 (en) * 2013-11-15 2015-05-21 Black & Veatch Holding Company Systems and methods for hydrocarbon refrigeration with a mixed refrigerant cycle
EP3043133A1 (en) * 2015-01-12 2016-07-13 Shell Internationale Research Maatschappij B.V. Method of removing nitrogen from a nitrogen containing stream
WO2017009341A1 (fr) * 2015-07-13 2017-01-19 Technip France Procédé de détente et de stockage d'un courant de gaz naturel liquéfié issu d'une installation de liquéfaction de gaz naturel, et installation associée
US20180202610A1 (en) * 2015-07-13 2018-07-19 Technip France Process for expansion and storage of a flow of liquefied natural gas from a natural gas liquefaction plant, and associated plant
FR3038964A1 (fr) * 2015-07-13 2017-01-20 Technip France Procede de detente et de stockage d'un courant de gaz naturel liquefie issu d'une installation de liquefaction de gaz naturel, et installation associee
US10995910B2 (en) * 2015-07-13 2021-05-04 Technip France Process for expansion and storage of a flow of liquefied natural gas from a natural gas liquefaction plant, and associated plant
US10704830B2 (en) * 2018-01-24 2020-07-07 Gas Technology Development Pte Ltd Process and system for reliquefying boil-off gas (BOG)
US20210063084A1 (en) * 2019-08-28 2021-03-04 Toyo Engineering Corporation Process and apparatus for treating lean lng
US11692771B2 (en) * 2019-08-28 2023-07-04 Toyo Engineering Corporation Process and apparatus for treating lean LNG

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US20080066492A1 (en) 2008-03-20
JP2008506027A (ja) 2008-02-28
RU2007105106A (ru) 2008-08-20
MY140540A (en) 2009-12-31
BRPI0512692A (pt) 2008-04-01
EP1766312A1 (en) 2007-03-28
EP1766311A1 (en) 2007-03-28
JP5378681B2 (ja) 2013-12-25
PE20060219A1 (es) 2006-05-03
MY141887A (en) 2010-07-16
AU2005261727B2 (en) 2008-07-10
AU2005261729B2 (en) 2008-07-17
JP2008506026A (ja) 2008-02-28
KR101178072B1 (ko) 2012-08-30
RU2007105107A (ru) 2008-08-20
PE20060221A1 (es) 2006-05-03
KR20070032003A (ko) 2007-03-20
AU2005261729A1 (en) 2006-01-19
KR101238172B1 (ko) 2013-02-28
AU2005261727A1 (en) 2006-01-19
JP5043655B2 (ja) 2012-10-10
RU2392552C1 (ru) 2010-06-20
WO2006005746A1 (en) 2006-01-19
WO2006005748A1 (en) 2006-01-19
KR20070034612A (ko) 2007-03-28
RU2362954C2 (ru) 2009-07-27

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