WO2009103715A2 - Procédé et appareil pour refroidir et séparer un courant d'hydrocarbures - Google Patents

Procédé et appareil pour refroidir et séparer un courant d'hydrocarbures Download PDF

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Publication number
WO2009103715A2
WO2009103715A2 PCT/EP2009/051882 EP2009051882W WO2009103715A2 WO 2009103715 A2 WO2009103715 A2 WO 2009103715A2 EP 2009051882 W EP2009051882 W EP 2009051882W WO 2009103715 A2 WO2009103715 A2 WO 2009103715A2
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WO
WIPO (PCT)
Prior art keywords
stream
refrigerant
fraction
cooling
hydrocarbon
Prior art date
Application number
PCT/EP2009/051882
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English (en)
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WO2009103715A3 (fr
Inventor
Marco Dick Jager
Original Assignee
Shell Internationale Research Maatschappij B.V.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Shell Internationale Research Maatschappij B.V. filed Critical Shell Internationale Research Maatschappij B.V.
Priority to US12/867,106 priority Critical patent/US20100307193A1/en
Priority to CN2009801059211A priority patent/CN102203530A/zh
Priority to RU2010138604/06A priority patent/RU2488759C2/ru
Priority to AU2009216745A priority patent/AU2009216745B2/en
Publication of WO2009103715A2 publication Critical patent/WO2009103715A2/fr
Publication of WO2009103715A3 publication Critical patent/WO2009103715A3/fr

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
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    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
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    • F25J1/0214—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle
    • F25J1/0215—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle with one SCR cycle
    • F25J1/0216—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle with one SCR cycle using a C3 pre-cooling 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
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    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
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    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
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    • F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
    • F25J1/0239—Purification or treatment step being integrated between two refrigeration cycles of a refrigeration cascade, i.e. first cycle providing feed gas cooling and second cycle providing overhead gas cooling
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    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
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    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
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    • 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
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    • 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
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    • 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
    • F25J2270/02—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
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons

Definitions

  • the present invention relates to a method and apparatus for cooling and separating a hydrocarbon stream, particularly but not exclusively natural gas, and optionally subsequently liquefying the hydrocarbon stream.
  • the present invention relates to a liquefaction plant comprising such an apparatus.
  • LNG liquefied natural gas
  • Separation of heavier hydrocarbons from natural gas can be carried out by cooling the natural gas to partly condense it, and then using a fractionation column.
  • US 5,960,644 describes a method for removing carbon dioxide, ethane and heavier components from a high pressure natural gas stream, wherein the high pressure natural gas stream is partly condensed and passed through first and second separators, before various streams are passed into a fractionation column.
  • a fluid stream is removed from the fractionation column and is heated in a heat exchanger 46 to obtain a re-boiling stream, and the re-boiling stream is introduced into the fractionation column.
  • US 5,960,644 uses an external refrigerant to partly condense the high pressure natural gas stream, and a heating medium to provide heat to the lower part of the fractionation column.
  • the external refrigerant used to partly condense the high pressure natural gas stream is not described, and the heating medium is a compressed gaseous product stream requiring separate compression to pipeline pressure. It is an object of the present invention to reduce the power that is needed to provide a given cooling duty of a refrigerant around a refrigerant circuit.
  • the present invention provides a method of cooling and separating a hydrocarbon stream such as natural gas comprising at least the steps of:
  • the present invention also provides apparatus for cooling and separating a hydrocarbon stream such as natural gas comprising at least: a first cooling stage to cool a hydrocarbon stream and provide a partially liquefied hydrocarbon stream; a distillation column to receive and separate at least a fraction of the partially liquefied hydrocarbon stream provided through a first inlet; a refrigerant circuit comprising at least a compressed fully liquefied refrigerant stream; and a first heat exchanger to heat a lower feed stream against the compressed fully liquefied refrigerant stream to provide a cooled refrigerant stream and a heated lower feed stream to be passed into the distillation column through a second inlet lower than the first inlet; and a heat exchange system in the first cooling stage arranged in the refrigerant circuit downstream of the first heat exchanger to cool the hydrocarbon stream against at least a fraction of the cooled refrigerant stream, thereby partly or fully evaporating the at least the fraction of the cooled refrigerant stream.
  • a hydrocarbon stream such
  • the present invention also provides a liquefaction plant comprising apparatus as herein defined.
  • Figure 1 is a diagrammatic scheme for a first method of cooling and separating a hydrocarbon stream according to one embodiment of the present invention
  • Figure 2 is a diagrammatic scheme for a second method of cooling and separating a hydrocarbon stream as part of a liquefaction plant according to a second embodiment of the present invention
  • Figure 3 is a diagrammatic scheme for a third method of cooling and separating a hydrocarbon stream according to a third embodiment of the present invention
  • Figure 4 is a diagrammatic scheme for a fourth method of cooling and separating a hydrocarbon stream according to a fourth embodiment of the present invention.
  • Figure 5 is a diagrammatic scheme for a fifth method of cooling and separating a hydrocarbon stream according to a fifth embodiment of the present invention.
  • Embodiments of the present disclosure employ a refrigerant stream to heat a lower feed stream passing into a distillation column.
  • the thus resulting cooled refrigerant stream is then advantageously employed to cool a hydrocarbon stream, thereby to partially condense or help to partially condense the hydrocarbon stream, before passing at least part of it to the distillation column .
  • a method of cooling and separating a hydrocarbon stream such as natural gas comprising at least the steps of: (a) providing a hydrocarbon stream 10;
  • step (h) separating the partially liquefied hydrocarbon stream 20 in the distillation column 12 to provide at least a first overhead gaseous stream 70 and a first bottom liquid stream 80.
  • the cooling in step (b) is carried out by partially or fully evaporating the cooled refrigerant stream 60, such as a sub-cooled liquefied refrigerant stream.
  • the refrigerant stream 40 in steps (e) and (f) is a compressed fully liquefied refrigerant stream, such that the cooled refrigerant stream 60 produced in step (f) is a sub-cooled liquefied refrigerant stream.
  • an apparatus for cooling and separating a hydrocarbon stream such as natural gas
  • the apparatus comprises at least: a first cooling stage 14 to cool a hydrocarbon stream 10 and provide a partially liquefied hydrocarbon stream 20; a distillation column 12 to receive and separate at least a fraction of the partially liquefied hydrocarbon stream 20 provided through a first inlet 17; a refrigerant circuit 4 comprising at least a refrigerant stream 40; and a first heat exchanger 16 to heat a lower feed stream 30 against the refrigerant stream 40 to provide a heated lower feed stream 50 to be passed into the distillation column 12 through a second inlet 18 located gravitationally lower than the first inlet 17.
  • the apparatus further comprises a heat exchange system 34 in the first cooling stage 14 arranged downstream of the first heat exchanger 16 to receive at least a fraction of the cooled refrigerant stream 60 and cool the hydrocarbon stream 10 against the at least the fraction of the cooled refrigerant stream 60, thereby partly or fully evaporating the refrigerant stream 60.
  • the cooled refrigerant stream 60 is preferably a sub-cooled liquefied refrigerant stream.
  • the refrigerant stream 40 in the refrigerant circuit 4 is a compressed fully liquefied refrigerant stream.
  • One advantage of cooling the refrigerant stream through the heat exchange with the lower feed stream is that the refrigerant stream then has more cooling duty to cool the hydrocarbon stream, and optionally other streams .
  • Another advantage of the present invention is that by cooling the refrigerant stream through the heat exchange with the lower feed stream, less compression power is required for the refrigerant circuit to provide the same cooling duty around its circuit, for example to cool the hydrocarbon stream.
  • the present disclosure can provide a method that requires less power to provide the duty for cooling and separating the same amount of hydrocarbon.
  • Figure 1 shows a method of cooling and separating a hydrocarbon stream 10 according to one embodiment of the present invention.
  • the hydrocarbon stream 10 may be any suitable hydrocarbon stream such as, but not limited to, a hydrocarbon-containing gas stream able to be cooled.
  • a hydrocarbon-containing gas stream able to be cooled.
  • One example is a natural gas stream obtained from a natural gas or petroleum reservoir.
  • the natural gas stream may also be obtained from another source, also including a synthetic source such as a Fischer-Tropsch process .
  • such a hydrocarbon stream is comprised substantially of methane.
  • a hydrocarbon stream comprises at least 50 mol% methane, more preferably at least 80 mol% methane.
  • the method according to the present invention is applicable to various hydrocarbon streams, it is particularly suitable for natural gas streams to be liquefied. As the skilled person readily understands how to liquefy a hydrocarbon stream, this is not discussed herein in detail.
  • the hydrocarbon stream 10 may contain one or more non-hydrocarbons such as H2O, N2,
  • the hydrocarbon stream 10 may be pre-treated before use either as part of a hydrocarbon cooling process, or separately.
  • This pre-treatment may comprise reduction and/or removal of non-hydrocarbons such as CO2 and H2S or other steps such as early cooling and pre-pressurizing. As these steps are well known to the person skilled in the art, their mechanisms are not further discussed here.
  • hydrocarbon stream as used herein also includes a composition prior to any treatment, such treatment including cleaning, dehydration and/or scrubbing, as well as any composition having been partly, substantially or wholly treated for the reduction and/or removal of one or more compounds or substances, including but not limited to sulfur, sulfur compounds, carbon dioxide and water.
  • a hydrocarbon stream to be used in the present invention undergoes at least the minimum pre- treatment required to subsequently allow liquefaction of the hydrocarbon stream.
  • a requirement for liquefying natural gas is known in the art.
  • the hydrocarbon stream 10 may also contain varying amounts of hydrocarbons heavier than methane such as ethane, propane, butanes and pentanes, as well as some aromatic hydrocarbons.
  • the composition varies depending upon the type and location of the hydrocarbon stream such as natural gas .
  • Hydrocarbons heavier than methane generally need to be removed from natural gas for several reasons, such as having different freezing or liquefaction temperatures that may cause them to block parts of a methane liquefaction plant.
  • C2-C4 hydrocarbons can be used as a source of natural gas liquids (NGLs) and/or refrigerant . Removal of hydrocarbons heavier than methane is often termed 'NGL recovery' .
  • Figure 1 shows a hydrocarbon stream 10 containing natural gas, which is cooled in a first cooling stage 14 to provide a cooled and partially liquefied hydrocarbon stream 20.
  • the cooling in the first cooling stage 14 may cause partial condensation of the hydrocarbon stream 10.
  • the first cooling stage 14 may comprise a heat exchange system 34, e.g. in the form of one or more heat exchangers such as kettles, either in parallel, series or both, in a manner known in the art. Cooling in the first cooling stage 14 is provided by a first cooling stage refrigerant stream 15, which is warmed and partially or fully evaporated in the first cooling stage 14 to provide a warmed first cooling stage refrigerant stream 15a.
  • the cooling of the hydrocarbon stream 10 by the first cooling stage refrigerant stream 15 may be part of a liquefaction process, such as a pre-cooling stage, optionally involving a propane refrigerant circuit as described hereinafter with reference to Figure 2, or the cooling may be a separate process.
  • the first cooling stage refrigerant stream 15 may therefore be part of one or more refrigerant circuits hereinafter described, or may be provided separately. Cooling of the hydrocarbon stream 10 may involve reducing the temperature of the hydrocarbon stream 10 to below -0 0 C, for example, in the range -10 0 C to -70 0 C.
  • At least a fraction, optionally all, of the partially liquefied hydrocarbon stream 20 from the first cooling stage 14 is passed into a distillation column 12 through a first inlet 17.
  • the distillation column 12 may be of any suitable size and design known in the art.
  • One common distillation column is a scrubber or scrub column, generally operating at an above ambient pressure in a manner known in the art.
  • One purpose of the distillation column 12 is to provide a generally gaseous stream that is methane- enriched, and therefore more suitable for subsequent liquefaction.
  • Suitable operating parameters for a distillation column 12 are known in the art, and can be varied to vary the composition of at least one of the major product streams provided therefrom.
  • the bottom stream is intended to be enriched in the hydrocarbons heavier than methane in the hydrocarbon stream 10, especially butanes, pentanes and heavier hydrocarbons.
  • Figure 1 shows a lower feed stream 30 intended to provide heat at or near the bottom of distillation column 12 in the manner of a re-boiling stream known in the art.
  • heat for the re-boiling stream is provided by a separate boiler, which requires a dedicated fuel source, and whose energy is not recoverable.
  • the lower feed stream 30 passes through a first heat exchanger 16 to heat the lower feed stream 30 against a compressed fully liquefied refrigerant stream 40 discussed hereinafter in more detail.
  • the heat exchange in the first heat exchange 16 provides a heated lower feed stream 50, which passes into the distillation column 12 through a second inlet 18 lower than the first inlet 17, preferably at or near the bottom of the distillation column. This is to provide heat preferably at or near the bottom of the distillation column 12 to encourage the passage of methane in the partially liquefied hydrocarbon stream in the distillation column 20 to pass out of the distillation column 12 as part of the overhead gaseous stream 70.
  • the distillation column 12 preferably provides a first overhead gaseous stream 70 having a composition greater than 80 mol% methane, and having a temperature below 0 0 C, more preferably in the range -20 0 C to -40 0 C.
  • the distillation column 12 in Figure 1 also provides a first liquid bottom stream 80, generally being enriched in hydrocarbons heavier than methane.
  • the compressed fully liquefied refrigerant stream 40 is part of a first refrigerant circuit 4, several arrangements for which are shown and described in Figures 2, 3 and 4 hereinafter by way of examples only.
  • the first refrigerant circuit 4 comprises at least one refrigerant compressor and at least one refrigerant stream.
  • One or more of the refrigerant streams may be divided and/or combined one or more times in the refrigerant circuit, to provide cooling to one or more other streams, units, fluids, etc. in a manner known in the art, generally by passing through one or more heat exchangers.
  • the cooling by each refrigerant stream (being a full stream or a fraction or part thereof) is provided by the partial or full evaporation of the refrigerant stream at low pressure in a manner known in the art, the low pressure being provided by passage through one or more valves and/or other expanders.
  • Each refrigerant stream used in the present disclosure may be formed from a single component such as propane or nitrogen, or may be a mixed refrigerant formed from a mixture of two or more components selected from a group comprising: nitrogen, methane, ethane, ethylene, propane, propylene, butanes, pentanes, etc.
  • the first heat exchanger 16 may comprise one or more heat exchangers in parallel, series or both in a manner known in the art .
  • the compressed fully liquefied refrigerant stream 40 generally has a temperature above 0 0 C, such as in the range 10-70 0 C.
  • the temperature of the cooled refrigerant stream 60 which will be a sub-cooled liquefied refrigerant stream, is less than the refrigerant stream 40.
  • the heat input to the lower feed stream 30, supplied by the compressed fully liquefied refrigerant stream 40 can be controlled, and more particularly lowered, compared to the use of a partly or fully vaporised refrigerant stream, to provide a heated lower feed stream at a temperature suitable to optimise the separation in the distillation column 12.
  • Use of a partly or fully vaporised refrigerant stream may require too much cooling duty of the lower feed stream 30 such that the heated lower feed stream 50 would be too hot, reducing the separation efficiency in the distillation column.
  • a system is provided in which the cooling duty available from the lower feed stream 30 can be matched with the requirements of the compressed fully liquefied refrigerant stream 40.
  • the cooled, such as sub-cooled liquefied, refrigerant stream 60 is subsequently partially or fully evaporated to provide cooling as part of the first refrigerant circuit 4. At least a fraction of the cooling of the hydrocarbon stream 10 is carried out by partially or fully evaporating the cooled, such as sub-cooled liquefied, refrigerant stream 60.
  • the first refrigerant 4 circuit may be involved with treatment of the hydrocarbon stream 10 and/or with the first overhead gaseous stream 70, or be separate therefrom.
  • Figure 2 shows the hydrocarbon stream 10 passing through the first cooling stage 14 to provide a partially liquefied hydrocarbon stream 20, which fully passes into the distillation column 12 through the first inlet 17 to provide a first overhead gaseous stream 70 and a first bottom liquid stream 80 as described above.
  • Figure 2 also shows the compressed fully liquefied refrigerant stream 40 passing through a first heat exchanger 16 to provide a cooled, such as sub-cooled liquefied, refrigerant stream 60 as described above.
  • Figure 2 shows the first refrigerant circuit 4 comprising one or more first refrigerant compressors 42.
  • the refrigerant passing around the first refrigerant circuit 4 may be any suitable refrigerant being a single component such as propane, or a mixed refrigerant.
  • a refrigerant compressor includes any unit, device or apparatus able to increase the pressure of a refrigerant stream. This includes refrigerant compressors having a single compression process or step, or refrigerant compressors having multi-stage compressions or steps. Some stages or steps of a hydrocarbon cooling process may involve two or more refrigerant compressors in parallel, series or both.
  • the present invention is not limited by the type or arrangement or layout of the refrigerant compressor or refrigerant compressors, particularly in any refrigerant circuit .
  • the first refrigerant compressor 42 provides a first compressed refrigerant stream 44 which passes through one or more coolers such as a water and/or air cooler 46, to provide a cooler compressed stream 48 which passes into an accumulator 52 in a manner known in the art.
  • a first compressed refrigerant stream 44 which passes through one or more coolers such as a water and/or air cooler 46, to provide a cooler compressed stream 48 which passes into an accumulator 52 in a manner known in the art.
  • an accumulator stream 54 which is fully liquefied.
  • a fraction of the accumulator stream 54 is provided as a first cooling refrigerant stream 56, which is expanded and/or evaporated through a suitable valve 58 to provide an expanded refrigerant stream 62 (which can act as the first cooling stage refrigerant stream 15 in Figure 1) to pass into the first cooling stage 14 to at least partly cool the hydrocarbon stream 10, and to provide a warmed refrigerant stream 75 (like the warmed first cooling stage refrigerant stream 15a shown in Figure 1), which passes back to the first refrigerant compressor 42.
  • Figure 2 also shows the option of dividing the accumulator stream 54 by a stream splitter 64 to provide the compressed fully liquefied refrigerant stream 40.
  • the proportion of the divided streams 56, 40 from the accumulator stream 54 can be calculated in order to provide the desired subsequent heat exchanges.
  • the compressed fully liquefied refrigerant stream 40 provided by the stream splitter 64 is a relatively warm stream following the compression in the first refrigerant compressor 42. At least part of this heat can be used to heat the lower feed stream 30 prior to use of the cooled, such as a sub- cooled liquefied, lower feed stream refrigerant stream 60 as a normal refrigerant stream.
  • the cooled lower feed stream refrigerant stream 60 may be used as a normal refrigerant stream at any suitable location or locations, and through any suitable heat exchange system including any suitable heat exchangers and/or cooling stages, either as part of the present method cooling and separating a hydrocarbon stream, and/or elsewhere in the liquefaction plant 1, and/or in an independent process or plant.
  • the refrigerant circuit 4 may comprise a heat exchange system arranged downstream of the first heat exchanger 16, wherein at least a fraction of the cooled, such as a sub- cooled liquefied, refrigerant stream 60 may be used to provide cooling to another stream.
  • At least a fraction of the cooled, such as a sub- cooled liquefied, refrigerant stream 60 at least partially cools the hydrocarbon stream 10. This may be achieved by passage of the cooled, such as a sub-cooled liquefied, refrigerant stream 60 through a valve 19 to provide an expanded refrigerant stream 60a, and passage thereof into the first cooling stage 14. All of the heated/warmed refrigerant from the first cooling stage 14 can return to the first refrigerant compressor 42 through line 75. In this way, at least a fraction, optionally all, of the cooled, such as a sub-cooled liquefied, refrigerant stream 60 provides at least a part of the cooling of at least part of or all of the hydrocarbon stream 10 in the first cooling stage 14.
  • Figure 3 shows a number of other and/or alternative embodiments of the present invention using the first refrigerant circuit 4 shown in Figure 2.
  • the heated lower feed stream 50 passes into a lower feed gas/liquid separator 51, which may be external or internal to the distillation column 12, to provide a second overhead gaseous stream 50a for use in the distillation column 12, and a second bottom stream 50b for use as an NGL stream.
  • a lower feed gas/liquid separator 51 which may be external or internal to the distillation column 12, to provide a second overhead gaseous stream 50a for use in the distillation column 12, and a second bottom stream 50b for use as an NGL stream.
  • Figure 3 also shows the cooled, such as a sub-cooled liquefied, refrigerant stream 60 providing, as stream 60a after valve 19, at least a part of the cooling of the hydrocarbon stream 10 in the first cooling stage 14.
  • This could provide a separate warmed refrigerant stream 60b from the first cooling stage 14, which could be returned to the first refrigerant compressor 42 as part of the return stream 75 as described above (along with the expanded refrigerant stream 62 also passing into the first cooling stage 14), or could be separately returned to the first refrigerant compressor 42 at any other suitable location, one example of which is as a return stream 60c upstream of the first refrigerant compressor 42 (shown in dashed line in Figure 2 for clarity) .
  • Figure 3 also shows the option of dividing the accumulator stream 54 by the stream splitter 64 to provide a usually majority second refrigerant stream 66 which can be expanded by a valve 68 to provide cooling in a second heat exchanger 72 as described hereinbelow, and to provide a second return stream 74 to the refrigerant compressor 42.
  • the second heat exchanger 72 may be associated, aligned or integral with the first cooling stage 14 in a manner known in the art.
  • Figure 3 also shows non-limiting examples of alternative sources of the compressed fully liquefied refrigerant stream 40 from the first refrigerant circuit 4.
  • the compressed stream 44 from the refrigerant compressor 42 could be divided by a stream splitter to provide a first split stream 76 as the source prior to the cooler 46.
  • the source of the refrigerant stream could be divided by a stream splitter to provide a first split stream 76 as the source prior to the cooler 46.
  • 40 may be from a separate supply, such as a separate refrigerant circuit.
  • Figure 3 also shows a second refrigerant circuit 6 comprising one or more second refrigerant compressors 82 able to provide a second compressed refrigerant stream 84, which then passes through one or more second coolers 86 and then the second heat exchanger 72 to provide a cooler second compressed stream 92.
  • the cooler second compressed stream 92 is shown in Figure 3 passing through a third separator 94, generally to provide a lighter overhead stream 96 and a heavier bottom stream 98.
  • the lighter overhead stream 96 and the heavier bottom stream 98 pass though a third heat exchanger 102 to be cooled, are separately expanded outside the third heat exchanger 102, and then returned therein to provide cooling to the streams passing through the third heat exchanger 102.
  • This provides a second return refrigerant stream 104 to the second refrigerant compressor 82.
  • the third heat exchanger 102 may be fully or part of a second cooling stage of a hydrocarbon cooling process.
  • a second cooling stage is preferably separate from the first cooling stage. That is, the second cooling stage comprises one or more separate heat exchangers using a second refrigerant circulating in a second refrigerant circuit, although the refrigerant of the second refrigerant circuit may also pass through one or more heat exchangers of the first cooling stage.
  • Such a second cooling stage is sometimes also termed a 'main cooling' stage .
  • the second refrigerant circuit 6 may provide one or more part or split streams as the source of the compressed fully liquefied refrigerant stream 40.
  • the second compressed refrigerant stream 84 could be divided to provide a third split stream 106, and the second refrigerant stream after the cooler 86 could provide a fourth split stream 108.
  • the warmed refrigerant stream 60b from the first cooling stage 14 could be returned into the second refrigerant circuit 6 at any suitable location, such as as a third return stream 6Od after the second heat exchanger 72, or as a fourth return stream 6Oe into the third separator 94.
  • Figure 3 also shows at least a fraction, preferably all, of the first overhead gaseous stream 70 from the distillation column 12 being subsequently liquefied in the third heat exchanger 102 to provide a liquefied hydrocarbon stream 120 such as LNG.
  • Figure 4 shows a hydrocarbon stream 10 being cooled in heat exchanger system 34a of first cooling stage 14 similar to Figures 1 to 3, to provide a partially liquefied hydrocarbon stream 20.
  • the hydrocarbon stream 10 can be divided by a stream splitter 21 into at least a first part stream 10a and a second part stream 10b in a manner known in the art.
  • the ratio of the division of the hydrocarbon stream 10 into the first and second part streams 10a, 10b may be any ratio or proportion.
  • any part stream to be provided through the first inlet 17 into the distillation column 12 is the majority of the hydrocarbon stream 10, such as described in WO 2006/061400 Al, incorporated herein by way of reference .
  • the first part feed stream 10a passes through the heat exchange system 34a in first cooling stage 14 as described above to provide the partially liquefied hydrocarbon stream 20 which passes into the distillation column 12.
  • the second part stream 10b provides the lower feed stream 30 for passage into first heat exchanger 16 to provide a heated lower feed stream 50, which also passes into the distillation column 12.
  • the refrigerant stream 40 can be provided from the first refrigerant circuit 4 after the accumulator 52, optionally as a fraction of the second refrigerant stream 66 being provided to the second heat exchanger 72 (not shown in Figure 4), represented as fraction stream 78.
  • the hydrocarbon stream 10 is provided from an initial stream 8, which passes through a fourth heat exchanger 112, which may comprise one or more heat exchangers in series, parallel or both.
  • the fourth heat exchanger 112 may form part of the first cooling stage 14. Cooling for the fourth heat exchanger 112 can be provided either by use of the cooled, such as a sub- cooled liquefied, refrigerant stream 60 after passing through the valve 19 to provide an expanded refrigerant stream 60a, and/or by provision of at least a fraction of the expanded refrigerant stream 62 in the first refrigerant circuit 4 prior to its use as the first cooling stage refrigerant stream 15 in the first cooling stage 14.
  • Dashed line 63 show passage of an optional refrigerant stream into the fourth heat exchanger 112, and return line 63a could also be the path of return of the expanded refrigerant stream 60a and any optional refrigerant stream 63 back into the first refrigerant circuit 4 after use in the fourth heat exchanger 112.
  • An optional second fraction of the expanded refrigerant stream 6Og may be passed to heat exchanger system 34a of the first cooling stage 14.
  • Figure 4 shows second fraction expanded refrigerant stream 6Og being passed to first cooling stage refrigerant stream 15 which is then passed to heat exchange system 34a of the first cooling stage 14.
  • the fourth heat exchanger 112 is a part of the first cooling stage 14.
  • Figure 4 shows embodiments of the present invention wherein a fraction of the hydrocarbon stream 10 provides at least a fraction of the lower feed stream 30, preferably by division of the hydrocarbon stream 10 into at least first and second part streams 10a, 10b, and wherein the first part stream 10a is cooled to provide the partially liquefied hydrocarbon stream 20, and the second part stream 10b provides at least a fraction of the lower feed stream 30.
  • Figures 3 and 4 also show various alternatives for the provision of cooling to the first cooling stage 14, and various embodiments for the use of the cooled, such as a sub-cooled liquefied, refrigerant stream 60 to provide cooling, preferably as part of the refrigerant circuit 4 through one or more of the same or different heat exchangers.
  • the cooled such as a sub-cooled liquefied, refrigerant stream 60 to provide cooling, preferably as part of the refrigerant circuit 4 through one or more of the same or different heat exchangers.
  • FIG. 5 shows further alternative embodiments of the present invention.
  • the hydrocarbon stream 10 passes through the first cooling stage 14 as described above to provide a partially liquefied hydrocarbon stream 20 which passes into a feed stream gas/liquid separator 32 to provide a feed stream overhead gaseous stream 100a, and a feed stream liquid bottom stream 100b.
  • At least a fraction, preferably all, of the feed stream liquid bottom stream 100b is provided as the lower feed stream 30 which passes through the first heat exchanger 16 to provide the heated lower feed stream 50, and then passes into the distillation column 12 as described hereinabove. Meanwhile, at least a fraction, preferably all, of the feed stream overhead gaseous stream 100a passes through a fifth heat exchanger 116 to provide a cooled partially liquefied hydrocarbon stream 20a which also passes into the distillation column 12.
  • Cooling for the fifth heat exchanger 116 can be provided by a suitable cooling and/or refrigerant stream 114 from one or more of the sources of a refrigerant stream described herein, or from a separate source, in a manner known in the art, at least a fraction of which is derived from cooled, such as a sub-cooled liquefied, refrigerant stream 60, to provide a warmed further refrigerant stream 114a.
  • Cooling of the feed stream overhead gaseous stream 100a increases the temperature difference between the subsequent cooled partially liquefied hydrocarbon stream 20a and the heated lower feed stream 50 as they enter the distillation column 12, thus increasing the separation, or the efficiency of the separation, of the content of the distillation column 12 into its first overhead gaseous stream 70 and first bottom liquid stream 80, preferably increasing the amount of methane, which passes out of the distillation column 12 as part of the first overhead gaseous stream 70.
  • the first gaseous overhead stream 70 passes through a second cooling stage 22, comprising one or more heat exchangers in parallel, series or both in a manner known in the art.
  • the second cooling stage 22 comprises the third heat exchanger 102 and the cooler second compressed stream 92 shown in Figure 3.
  • a partially, preferably fully, liquefied hydrocarbon stream 120 passes to a final separator such as an end-flash vessel 24, to provide a final overhead stream such as end flash gas 24a, and a final bottom stream such as an enriched liquefied hydrocarbon stream 90.
  • a final separator such as an end-flash vessel 24
  • a final bottom stream such as an enriched liquefied hydrocarbon stream 90.
  • At least a fraction 90b of the final bottom stream 90 is split from the main product stream 90a (such as LNG) .
  • This fraction 90b is able to provide, via a pump 94, a secondary lower feed 30a which passes through a secondary heat exchanger 16a to provide a secondary heated lower feed stream 50a, which itself passes into the distillation column 12.
  • Heating for the secondary lower feed stream 30a can be provided by a secondary refrigerant stream 40a, being the same as, a fraction of, or separately derived from, the compressed fully liquefied refrigerant stream 40.
  • the secondary heat exchanger 16a provides a cooled secondary refrigerant stream 6Of, which may be combined with or associated with the cooled refrigerant stream 60, or otherwise separately used.
  • the distillation column 12 may receive more than one heated lower feed stream, either separately or combined into a single stream.
  • the present disclosure provides an advantageous method of using a least a fraction of a refrigerant stream to heat rather than cool another stream, prior to its subsequent use as a refrigerant stream in a refrigerant circuit as medium against which to cool another stream.
  • a refrigerant stream can be provided at, by or from a number of locations around a refrigerant circuit, and the heated refrigerant stream cam be returned to the refrigerant circuit at a number of suitable locations.
  • the present disclosure provides flexibility in the provision and return of the refrigerant stream to and from a refrigerant circuit.
  • the present disclosure also requires less compression power and less cooling in the first refrigerant circuit because of the cooling provided to the refrigerant stream by its use for heating the lower feed stream.
  • Table 2 below provides a comparison for the power duties required by or in the first cooling stage 14, the first heat exchanger 16, the first refrigerant compressor 42 and its subsequent cooler (s) 46, between; (i) an example of the present disclosure as shown in Figure 2; and
  • Table 2 confirms that the embodiment of the present disclosure shown in Figure 2 provides a near 20% reduction in the power required for the first refrigerant compressor 42, and a similar near 20% reduction in the cooling required in the first cooler (s) 46. These are significant power and cooling duty reductions in industrial scale of providing a liquefied hydrocarbon stream.
  • Table 2 confirms that the embodiment of the present disclosure shown in Figure 2 requires less compression power for the refrigerant circuit to provide the same cooling duty around its circuit, which reduces the overall power required to cool and separate the same amount of a hydrocarbon stream as the comparison example, which could equate to that shown in US 5,960,644.

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  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

La présente invention concerne un procédé et un appareil permettant de refroidir et de séparer un courant d'hydrocarbures tel que du gaz naturel. Ce procédé comporte au moins les opérations suivantes: (a) mise en place d'un courant d'hydrocarbures (10); (b) refroidissement du courant d'hydrocarbures (10) de façon à fournir un courant d'hydrocarbures partiellement liquéfiés (20); (c) introduction d'au moins une fraction du courant d'hydrocarbures partiellement liquéfiés (20) dans une colonne de distillation (12) en passant par une première entrée (17); (d) mise en place d'un courant d'alimentation inférieur (30); (e) mise en place d'un circuit de réfrigérant (4) comprenant au moins un courant de réfrigérant (40); (f) chauffage du courant d'alimentation inférieur (30) contre le courant de réfrigérant (40) de façon à obtenir un courant d'alimentation inférieur chauffé (50) et un courant de réfrigérant refroidi (60); (g) introduction du courant d'alimentation inférieur chauffé (50) dans la colonne de distillation (12) en passant par une deuxième entrée (18) située plus bas que la première entrée (17); et (h) séparation du courant d'hydrocarbures partiellement liquéfiés (20) dans la colonne de distillation (12) de façon à obtenir au moins un premier courant gazeux de tête de colonne (70) et un premier courant liquide de pieds de colonne (80).
PCT/EP2009/051882 2008-02-20 2009-02-18 Procédé et appareil pour refroidir et séparer un courant d'hydrocarbures WO2009103715A2 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
US12/867,106 US20100307193A1 (en) 2008-02-20 2009-02-18 Method and apparatus for cooling and separating a hydrocarbon stream
CN2009801059211A CN102203530A (zh) 2008-02-20 2009-02-18 用于冷却和分离烃流的方法和设备
RU2010138604/06A RU2488759C2 (ru) 2008-02-20 2009-02-18 Способ и устройство для охлаждения и разделения углеводородного потока
AU2009216745A AU2009216745B2 (en) 2008-02-20 2009-02-18 Method and apparatus for cooling and separating a hydrocarbon stream

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP08101798 2008-02-20
EP08101798.0 2008-02-20

Publications (2)

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WO2009103715A2 true WO2009103715A2 (fr) 2009-08-27
WO2009103715A3 WO2009103715A3 (fr) 2014-10-02

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US (1) US20100307193A1 (fr)
CN (1) CN102203530A (fr)
AU (1) AU2009216745B2 (fr)
RU (1) RU2488759C2 (fr)
WO (1) WO2009103715A2 (fr)

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US10808999B2 (en) 2014-09-30 2020-10-20 Dow Global Technologies Llc Process for increasing ethylene and propylene yield from a propylene plant

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US20100307193A1 (en) 2010-12-09
CN102203530A (zh) 2011-09-28
RU2010138604A (ru) 2012-03-27
WO2009103715A3 (fr) 2014-10-02
RU2488759C2 (ru) 2013-07-27
AU2009216745B2 (en) 2012-03-22
AU2009216745A1 (en) 2009-08-27

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