EP2597408A1 - Procédé et appareil de préparation d'un courant de gaz contenant du méthane pauvre - Google Patents

Procédé et appareil de préparation d'un courant de gaz contenant du méthane pauvre Download PDF

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Publication number
EP2597408A1
EP2597408A1 EP11190287.0A EP11190287A EP2597408A1 EP 2597408 A1 EP2597408 A1 EP 2597408A1 EP 11190287 A EP11190287 A EP 11190287A EP 2597408 A1 EP2597408 A1 EP 2597408A1
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Prior art keywords
stream
fractionation
column
recycle
liquid bottom
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
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EP11190287.0A
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German (de)
English (en)
Inventor
Jan Van Amelsvoort
Temitope Olaniyi Ogedengbe
Kornelis Jan Vink
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Shell Internationale Research Maatschappij BV
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Shell Internationale Research Maatschappij BV
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Priority to EP11190287.0A priority Critical patent/EP2597408A1/fr
Publication of EP2597408A1 publication Critical patent/EP2597408A1/fr
Withdrawn legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/78—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
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • 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
    • F25J2215/62—Ethane or ethylene
    • 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
    • F25J2215/64—Propane or propylene
    • 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
    • F25J2230/32—Compression of the product stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/60—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
    • F25J2235/02—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams using a pump in general or hydrostatic pressure increase
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/20—Integration in an installation for liquefying or solidifying a fluid stream

Definitions

  • the present invention relates to a method and apparatus for preparing a lean methane-containing gas stream. At least part of the lean methane-containing gas may subsequently be subjected to full condensation and subcooling, to provide a liquefied methane-containing stream.
  • Natural gas, and other methane-containing gases may in addition to methane ("C 1 ") contain amounts of hydrocarbons heavier than methane ("C 2 +”; sometimes referred to as “higher hydrocarbons”), including ethane (“C 2 "), propane (“C 3 “), butanes (“C 4 "), and hydrocarbons heavier than butanes (“C 5 +”), such as pentanes ("C 5 ”) and higher.
  • C 2 + hydrocarbons heavier than methane
  • propane C 3
  • butanes C 4
  • hydrocarbons heavier than butanes such as pentanes (“C 5 ") and higher.
  • Various hydrocarbons heavier than methane may be extracted from the methane-containing gas to various degrees.
  • the resulting gas is referred to as lean methane-containing gas stream, which means that the content of hydrocarbons heavier than methane in the gas stream is lower than in the methane-containing gas prior to said extracting.
  • the heavier hydrocarbons are usually extracted in condensed form as natural gas liquids and fractionated to yield valuable hydrocarbon products.
  • US patent application publication 2006/0260355 describes a process and apparatus for integrated natural gas liquids (NGL) recovery and liquefied natural gas production.
  • NGL natural gas liquids
  • An admixture of methane with ethane and higher hydrocarbons is separated in a scrub column into a methane-rich overhead stream and a liquid methane-depleted bottoms liquid.
  • the methane-rich overhead stream is partially condensed to provide reflux to the scrub column. Additional reflux is derived from an ethane-enriched stream from fractionation of the bottoms liquid.
  • Absorber liquid containing C 4 and/or C 5 from the fractionation may also be introduced into the scrub column.
  • Such absorber liquid sometimes referred to as "lean oil” functions as a washing liquid that helps to improve NGL recovery.
  • the vapour fraction remaining after partial condensation can be liquefied to provide an LNG product.
  • the present invention provides a method of preparing a lean methane-containing gas stream, comprising:
  • the present invention provides an apparatus for preparing a lean methane-containing gas stream, comprising:
  • recycle portion has the same composition as the first residue liquid bottom stream being withdrawn from the first fractionation column, further fractionation of first residue liquid bottom stream can be dispensed with in the context of the present invention, or applied only to a remaining portion of first residue liquid bottom stream, which is not recycled.
  • the recycle path bypasses any subsequent fractionation columns within the fractionation system downstream of the first fractionation column, so that the recycle portion does not pass through more than one fractionation column downstream of the extraction column.
  • FIG. 1 shows a schematic line up containing an embodiment of the invention.
  • Part of the line up is an apparatus 10 for preparing a lean methane-containing gas stream 510. It employs an extraction column 20 with a first feeding inlet 22 located in a first feeding position.
  • the first feeding inlet may be any suitable inlet including optional feed internals 24.
  • the extraction column 20 also has an overhead vapour outlet 26, for discharging a vaporous overhead stream 30.
  • the lean methane-containing gas stream 510 can be produced from the vaporous overhead stream 30.
  • the producing of the lean methane-containing gas stream 510 from the vaporous overhead stream 30 involves recompression via at least overhead compressor 44, optionally followed by one or more booster compressors (not shown).
  • An optional overhead cold recovery heat exchanger (not shown, but reference is made to e.g. US patent application publication No. 2009/0064713 which contains an example) may optionally be provided, wherein the lean methane-containing gas stream 510 is in indirect heat exchanging contact with the vaporous overhead stream 30 before it is recompressed in the overhead compressor 44.
  • the extraction column 20 also has a liquid bottom stream outlet 28 located at a first withdrawal level.
  • the first withdrawal level is gravitationally lower than the first feeding position.
  • the extraction column 20 may further comprise other internals, such as for example one or more contacting devices 23 in the form of a plurality of contacting trays and/or packing (structured packing or non-structured packing).
  • the first feeding inlet 22 is in fluid communication with a feed supply 5 of a hydrocarbon feed stream 15. In the embodiment as shown, this feeding inlet 22 is arranged below at least one of the one or more contacting devices 23.
  • an optional inlet phase separator 16 is provided between the feed supply 5 and the first feeding inlet 22.
  • a liquid phase feed line 17 extends between a liquid outlet of the optional inlet phase separator 16 and the first feeding inlet 22.
  • a Joule Thomson valve 19 is provided in the liquid phase feed line 17.
  • a vapour phase feed line 18 extends between a vapour outlet of the optional inlet phase separator 16 and an auxiliary feeding inlet 21 into the extraction column 20.
  • the auxiliary feeding inlet 21 may be any suitable inlet including optional feed internals 25.
  • Means for partially condensing the vapour phase is provided in line 18.
  • Such means for partially condensing the vapour phase may comprise at least one from the group consisting of a heat exchanger to extract heat from the vapour phase in line 18 and an expansion device to lower the pressure and a combination thereof.
  • the expansion device may be in the form of a Joule Thomson valve and/or a dynamic expander such as, for example, an expansion turbine, and/or a combination thereof.
  • the means for partially condensing the vapour phase is represented by an expander in the form of a turbo expander 14.
  • the turbo expander 14 is shaft-coupled to an overhead compressor 44 via shaft 13-13'.
  • a flow control system comprising a flow rate controller is arranged to control an actual feed rate of the hydrocarbon feed stream 15 flowing into the extraction column 20.
  • the flow control system may take any suitable form. It may, for instance, be provided in the form of a flow restriction valve in the feed line 15 between the feed supply 5 and the extraction column 20. In the example of Figure 1 , however, it is embodied as part of a depressurizing system 535 downstream of an (optional) liquefaction system 500. More about such optional liquefaction system 500 and optional depressurizing system 535 will be described below.
  • the liquid bottom stream outlet 28 feeds into a liquid bottom stream discharge line 40, provided with a pressure reduction device, here represented in the form of a bottom stream control valve 55.
  • the liquid bottom stream discharge line 40 is fluidly connected to a fractionation system 300, whereby the bottom stream control valve 55 separates the fractionation system 300 from the extraction column 20.
  • the bottom stream control valve is suitable on liquid level control LC of the extraction column 20.
  • the fractionation system employs at least three consecutively arranged fractionation columns.
  • the fractionation system 300 receives at least a part of the liquid bottom stream 40 from the extraction column 20 that is to be subjected to fractionation into one or more fractionated streams 310, 320, each of single component with a relatively high purity compared to the liquid bottom stream 40.
  • Such fractionated streams can be used as refrigerant make-up, or sold separately or sold as natural gas liquids (NLG) and/or liquefied petroleum gas (LPG) products.
  • NLG natural gas liquids
  • LPG liquefied petroleum gas
  • the fractionated streams 310, 320 often consist of hydrocarbon components that are vaporous under atmospheric pressure and temperature.
  • the fractionation system also produces a so-called stabilized liquid stream 390, which can remain in liquid phase under atmospheric pressure and ambient temperature conditions.
  • this is entirely optional.
  • the fractionation system 300 does not have to be fully operative, when carrying out the present invention.
  • a first fractionation column 350 of the at least three consecutively arranged fractionation columns is in direct fluid communication contact, via the bottom stream control valve 55, with the liquid bottom stream outlet 28 of the extraction column 20.
  • the first fractionation column 350 is in fluid communication with a first overhead discharge line 352, and with a first residue liquid discharge line 50.
  • An optional reboiler 357 may be connected to the first residue liquid discharge line 50, or optionally directly to the first fractionation column 350 without using the first residue liquid discharge line 50.
  • a first fractionated stream discharge line 305 is in fluid communication with the first overhead discharge line 352, so that at least a part of the first fractionation overhead stream that is withdrawn from the first fractionation column 350 can be discharged in the form of a first fractionated stream 305.
  • a stream splitter 52 is provided in the first residue liquid discharge line 50, via which a remaining portion discharge line 70 is connected to the first residue liquid discharge line 50.
  • a recycling line 60 is fluidly connected to the stream splitter 52. More will be disclosed about the recycling line 60 below.
  • an optional second fractionation reflux system 361 is provided to serve the second fractionation column 360 with a second reflux stream 365 in liquid phase.
  • the second fraction reflux system 361 employs a second fractionation overhead condenser 363 arranged to partly condense the second fractionation overhead vapour stream 362 that is discharged from the second fractionation column 360.
  • the second fractionation overhead condenser 363 is fluidly connected to the second fractionation overhead gas/liquid separator 364.
  • the second fractionated stream discharge line 310 is in fluid communication with the second fractionation overhead gas/liquid separator 364 via a vapour outlet.
  • a second fractionation reflux line 365 is also in fluid communication with the second fractionation overhead gas/liquid separator 364, via a liquid outlet.
  • the second fractionation column 360 is in fluid connection with the second fractionation overhead gas/liquid separator 364 via second first fractionation reflux line 365.
  • An optional second fractionation reflux pump 366 is arranged in the second fractionation reflux line 365 to assist the flow of the second reflux stream 365.
  • a third fractionation column 370 is connected he second residue liquid discharge line 369. More fractionation columns may be provided if desired. However, in the embodiment as shown, the third fractionation column 370 is in fluid communication with a third fractionated stream discharge line 320 and with a stabilized liquid discharge line 390. Optionally, a third fractionation reflux system (not shown) is associated with the third fractionation column 370, similarly to the second fractionation reflux system 361 being associated with the second fractionation column 360.
  • the first fractionation column 350 is a demethanizer.
  • a relatively small amount of methane and lighter - and/or more volatile - components are present in the first residue liquid discharge line 50 that can end up in the recycling line 60, while a broad spectrum of C 2 + hydrocarbons are available to be drawn off into the recycling line 60.
  • the first fractionated stream 305 is not expected to be comprised of essentially pure methane, as together with the methane also more volatile components are expected to end up preferentially in the first fractionation overhead vapour stream 352.
  • At least one the at least three consecutive fractionation columns of the fractionation system, other than the first fractionation column, may be a debutanizer.
  • at least one of the fractionation columns upstream of the stabilized liquid discharge line is a debutanizer.
  • the last fractionation column of the three consecutive fractionation columns, in the present example the third fractionation column 370, is a debutanizer.
  • An optional first fractionation reflux system 351 may be provided at the top of the first fractionation column 350.
  • the optional first fractionation reflux circuit 351 which employs a reflux condenser in the form of a first fractionation overhead condenser 353 arranged to partly condense the first fractionation overhead vapour stream 352 that is discharged from the first fractionation column 350.
  • the first fractionation overhead condenser 353 is fluidly connected to a first fractionation overhead gas/liquid separator 354.
  • a first fractionated stream discharge line 305 is in fluid communication with the first fractionation overhead gas/liquid separator 354, as well as a first fractionation reflux line 355.
  • the first fractionation column 350 is in fluid connection with the first fractionation overhead gas/liquid separator 354 via the first fractionation reflux line 355.
  • An optional first fractionation reflux pump 356 is arranged in the first fractionation reflux line 355, to assist the flow of the first reflux stream 355.
  • a recycle pump 62 and a recycle chiller 32 are arranged in the recycling line 60 between the first fractionation column 350 and the extraction column 20.
  • the recycling line 60 follows a recycle path to a location into the extraction column 20 that is preferably gravitationally higher than the first feeding position.
  • the recycle path extends from the first fractionation column 350, through the first residue liquid discharge line 50, the stream splitter 52, a recycle pump 62, and a recycle chiller 33, to a second feeding inlet 32 into the extraction column 20.
  • the second feeding inlet 32 is in a second feeding position that is gravitationally higher than the first feeding position.
  • the second feeding inlet 32 may comprise any suitable form of internals for handling liquids, such as for example a liquid nozzle distributor 34.
  • the second feeding inlet 32 and/or its associate internals may optionally be integrated with and/or combined with the auxiliary inlet 21 and/or its associated internals.
  • a remaining portion flow control valve 75 is provided in the remaining portion discharge line 70, suitable on liquid level control of the first fractionation column 350.
  • a flow rate signal may be obtained from any suitable location upstream or downstream of the extraction column 20, including locations selected from the non-exhaustive list consisting of: the overhead vapour stream 30; the lean methane-containing gas stream 510; the first residue liquid bottom stream 50; the feed supply 5; the hydrocarbon feed stream 15; and anywhere else between the feed supply 5 of the hydrocarbon feed stream 15 and the extraction column 20.
  • the liquefaction system 500 is entirely optional. If it is provided, as is the case in Figure 1 , it is arranged in fluid communication with the overhead vapour outlet 26 of the extraction column 20. In such a liquefaction system 500, the lean methane-containing gas stream 510 can be subjected to full condensation and subcooling, to provide a liquefied methane-containing stream 530. Many possible liquefaction processes are available to the person skilled in the art, including processes that employ heat exchanging of the lean methane-containing gas stream 510, or parts thereof, against evaporating refrigerants that are circulated in two or more refrigeration circuits.
  • Various parts of the apparatus described herein including for instance the feed supply 5 and/or the recycle chiller 33 may be integrated with, and/or form part of, the liquefaction system 500, for instance by sharing or making use of refrigeration duty from the liquefaction system 500 (not shown in the drawing).
  • An optional depressurization system 535 may be provided downstream of the liquefaction system 500, to depressurize the liquefied methane-containing stream 530, preferably to a pressure of between 1 and 2 bara.
  • the depressurization system 535 may comprise one or more expander turbines and/or one or more Joule Thomson valves and/or a combination thereof, as well as a flash vapour separator arranged to receive the depressurized liquefied methane-containing stream 530 and remove flashed-off vapours from the depressurized liquefied methane-containing stream 530 (not shown).
  • the depressurization system 535 may be integrated with the liquefaction system 500 and/or form a part of the liquefaction system 500.
  • part of the flashed-off vapours is re-compressed and reinjected into the process stream in the liquefaction system 500 (not shown).
  • a hydrocarbon feed stream 15 is fed from the feed supply 5 into the extraction column 20 at the first feeding position and at an actual feed rate.
  • the hydrocarbon feed stream 15 contains methane, and one or more C 2 + hydrocarbons.
  • the hydrocarbon feed stream 15 contains ethane as one of the C 2 + hydrocarbons, in any non-zero amount.
  • the feeding of the hydrocarbon feed stream 15 into the extraction column 20 comprises separating a liquid phase of the hydrocarbon feed stream 15 from a vapour phase.
  • the liquid phase is discharged from the optional inlet phase separator 16 into the liquid phase feed line 17, and in the embodiment of Figure 1 only essentially this liquid phase 17 is passed into the extraction column 20 via said first feeding inlet 22.
  • the Joule Thomson valve 19 serves to match the pressure of the liquid phase 17 to the operating pressure in the extraction column 20 (corresponding to the extraction pressure).
  • the vapour phase is discharged into the vapour phase feed line 18, then partially condensed by refrigeration and/or expansion, and passed to and into the extraction column 20 via the auxiliary inlet 21.
  • the partial condensation of the vapour phase in line 18 is achieved by expanding in the turbo expander 14. Work generated in the turbo expander 14 is optionally used to drive the overhead compressor 44 via the shaft 13-13'.
  • the hydrocarbon feed stream from the feed supply 5 may be formed out of any hydrocarbon containing gas stream.
  • a common example of such hydrocarbon containing gas stream is a natural gas stream, obtained from natural gas or petroleum reservoirs.
  • the hydrocarbon feed stream may also be obtained from another supply source, including for instance a synthetic source, such as a Fischer-Tropsch process.
  • the hydrocarbon feed stream 15 When the hydrocarbon feed stream 15 is obtained from a natural gas stream, it is usually comprised primarily of methane.
  • the hydrocarbon feed stream 15 may comprise at least 50 mol% methane, and often at least 80 mol% methane as is often the case with natural gas.
  • hydrocarbon feed stream may contain varying amounts of hydrocarbons heavier than methane, such as in particular ethane, propane and the butanes, and possibly lesser amounts of pentanes and aromatic hydrocarbons.
  • hydrocarbons heavier than methane such as in particular ethane, propane and the butanes, and possibly lesser amounts of pentanes and aromatic hydrocarbons.
  • the composition varies depending upon the type and location of the gas.
  • Natural gas may also contain non-hydrocarbons such as H 2 O, N 2 , CO 2 , Hg, H 2 S and other sulphur compounds, and the like, which may be removed to various degrees as well. Particularly, CO 2 and hydrocarbons heavier than butanes should be removed in order to avoid freezing out of these components during subsequent liquefaction.
  • non-hydrocarbons such as H 2 O, N 2 , CO 2 , Hg, H 2 S and other sulphur compounds, and the like, which may be removed to various degrees as well.
  • CO 2 and hydrocarbons heavier than butanes should be removed in order to avoid freezing out of these components during subsequent liquefaction.
  • the hydrocarbon feed stream 15 may have been pre-treated as part of being supplied from the feed supply 5.
  • Pre-treatment may comprise reduction and/or removal of undesired components such as CO 2 and H 2 S or other steps such as early cooling, pre-pressurizing or the like. As these steps are well known to the person skilled in the art, their mechanisms are not further discussed here.
  • the extraction column 20 that is employed for this purpose may be operated at an extraction pressure in a range of from 20 bara to 65 bara, preferably in a range of from 40 bara to 65 bara, more preferably in a range of from 40 bara to 60 bara.
  • the removing of the hydrocarbons heavier than methane from the hydrocarbon feed stream 15 involves withdrawing a vaporous overhead stream 30 from the extraction column 20.
  • the vaporous overhead stream contains at least the majority of the methane from the hydrocarbon feed stream 15.
  • the lean methane-containing gas stream 510 is produced from the vaporous overhead stream 30. In the embodiment of Figure 1 , this involves recompression of the vaporous overhead stream 30 in the overhead compressor 14, which is driven by turbo-expander 14.
  • a liquid bottom stream 40 is withdrawn from the extraction column 20 from the first withdrawal level.
  • the liquid bottom stream 40 contains at least a recovery fraction of the C 2 + hydrocarbons from the hydrocarbon feed stream 15.
  • the pressure of at least a first portion of the liquid bottom stream 40 is reduced.
  • the pressure is reduced preferably by at least 5 bar (at least 10 bar in case the extraction column 20 is provided in the form of a scrub column).
  • the pressure reduction may typically be between from 10 bar to 30 bar.
  • the first portion is subsequently passed, at reduced pressure, into the first fractionation column 350 of the at least three consecutive fractionation columns of the fractionation system 300.
  • the first portion being passed into the first fractionation column 350 has the same composition as the liquid bottom stream 40 being withdrawn the extraction column 20.
  • a first residue liquid bottom stream 50 is simultaneously withdrawn from the first fractionation column 350.
  • the first residue liquid bottom stream contains at least a recycle portion 60.
  • This recycle portion 60 is recycled, at increased pressure, into the extraction column 20.
  • the first residue liquid bottom stream 50 is split into the recycle portion 60 and a remaining portion 70.
  • the recycle portion 60 has the same composition as the first residue liquid bottom stream 50 being withdrawn from the first fractionation column 350.
  • the content of C 5 + hydrocarbons in the first residue liquid bottom stream 50 and the recycle portion 60 may be between 40 and 75 mol%, whereby the remainder up to 99.0 mol%, preferably up to 99.5 mol%, of the first residue liquid bottom stream 50, respectively the recycle portion 60, may consist of C 2 -C 4 hydrocarbons (i.e. one or more hydrocarbons selected from the group consisting of C 2 , C 3 , and C 4 hydrocarbons).
  • the recycle portion 60 contains a recycle fraction of less than unity (1.00) from the first residue liquid bottom stream 50 being withdrawn from the first fractionation column 350, and it is fed back into the extraction column 20 in liquid phase, preferably fully liquid phase free from any vapour.
  • the fraction of the first residue liquid bottom stream 50 comprised in the recycle portion is more than zero.
  • the recycle portion 60 is fed back into the extraction column 20 via the second feeding inlet 32. To that end, the pressure of at least the recycle portion 60 is increased, with the recycle pump 62.
  • the recycle portion 60 is optionally refrigerated (sub-cooled) in the recycle chiller 33, by heat exchanging the recycle portion 60 against a chilling stream.
  • the recycle portion 60 enters the extraction column 60 gravitationally higher than the first feeding position.
  • the remaining portion 70 may optionally be subjected to further fractionation in the fractionation system 300, thereby obtaining at least one fractionation product stream (310,320) being enriched in a selected hydrocarbon component from the remaining stream 70.
  • the remaining portion 70 may for instance be passed to the second fractionation column 360 in the fractionation system 300 at reduced pressure.
  • the fraction of the first residue liquid bottom stream 50 that is split off from the first residue liquid bottom stream 50 into the recycle portion 60 may be controlled using the split ratio controller C.
  • This split ratio controller C is preferably programmed to reduce the fraction of the liquid bottom stream 50 that is split off into the recycle portion 60 over a course of time.
  • Another absorber liquid such as a fractionated stream 320 from the fractionation system 300 (if provided) when such fractionated stream 320 becomes available.
  • a second reason could be that liquid build-up in the extraction column 20 limits the allowable flow rate of the recycle portion 60 over the course of time. Particularly if, in the course of time, the actual feed rate is allowed to increase, the fraction of the first residue liquid bottom stream 50 that is split off in the recycle portion 60 may have to be lowered to avoid overloading the recycle pump 62 and/or the extraction column 20.
  • the embodiment of Figure 2 is provided with an overhead condenser 31 which is fluidly connected to the overhead vapour outlet 26, arranged to receive and partially condense the vaporous overhead stream from the extraction column 20.
  • the overhead condenser 31 may comprise a plurality of consecutive heat exchangers operating at progressively decreasing temperature levels, for instance each operating with a different refrigerant composition and/or at different pressure level.
  • the overhead condenser 31 may be a stand-alone heat exchange unit having as its sole specific function removing of heat from the overhead vapour stream 30.
  • the overhead condenser 31 may be integrated with any other heat exchanger arrangement in the process.
  • the liquefaction system 500 may be integrated with, for instance, the liquefaction system 500 if provided and/or exercise a combined function. For instance, it may share a heat exchanger with another stream to be cooled, such as a stream derived from the lean methane-containing gas stream 510 and/or it may share in refrigeration duty from a refrigerant circuit that also refrigerates another stream.
  • a heat exchanger with another stream to be cooled, such as a stream derived from the lean methane-containing gas stream 510 and/or it may share in refrigeration duty from a refrigerant circuit that also refrigerates another stream.
  • An overhead phase separator 39 is fluidly connected to the overhead condenser 31 to receive the partially condensed effluent stream from the overhead condenser 31. It is arranged to receive and phase separate a partially condensed overhead stream from the overhead condenser 31, into the lean methane-containing gas stream 510 and a liquid reflux stream 36.
  • the lean methane-containing gas line 510 communicates with the overhead phase separator 39 via a vapour outlet.
  • the overhead phase separator 39 is furthermore connected to the second feeding inlet 32 into the extraction column 20, via a reflux line 36, for feeding the liquid reflux stream into the extraction column 20.
  • a reflux pump 38 is optionally provided in the reflux line 36. Alternatively, flow of the liquid reflux stream 36 can be driven by gravity if the overhead phase separator 39 is arranged sufficiently high above the second feeding position.
  • the vaporous overhead stream 30 is partially condensed in the overhead condenser 31, by removing heat from the vaporous overhead stream 30 by indirect heat exchanging.
  • An effluent stream containing the partially condensed overhead stream 30 is discharged from the overhead condenser 31, and passed to the overhead phase separator 39 where the partially condensed overhead stream is allowed to separate into two phases.
  • the lean methane-containing gas stream is drawn from the overhead phase separator 39 in vapour phase, while a liquid reflux stream 36 is drawn from the overhead phase separator 39 in liquid phase.
  • the liquid reflux stream 36 is fed into the extraction column 20 at the second feeding position, optionally assisted by the reflux pump 38 and/or gravity.
  • a mixing junction 37 is optionally provided in the overhead vapour line 30, for admixing the recycle portion 60 with the vaporous overhead stream upstream of the overhead condenser 31.
  • the mixing junction 37 is arranged in fluid communication with the recycling line 60 and upstream of the overhead condenser 31 between the overhead vapour outlet 26 and the overhead condenser 31.
  • the mixing junction 37 is in fluid communication with the overhead condenser 31.
  • a recycle chiller 33 is provided in the recycling line 60 similar to the embodiment of Figure 1 .
  • the recycle chiller 33 can be arranged in the recycling line 60 between the stream splitter 52 and the mixing junction 37.
  • the embodiment of Figure 3 is similar to the embodiment of Figure 2 , except for the location of the mixing junction 37 which in the case of Figure 3 is located in the reflux line 36.
  • the mixing junction 37 is arranged between the reflux pump 38 (if provided) and the second feeding inlet 32, which has as advantage that the recycle flow from the recycling line 60 does not load the reflux pump 38.
  • the reflux stream 36 and the recycle stream 60 are fed into the extraction column 20 via mutually separate inlets, which can be at the same gravitational level or at mutually different gravitational levels in the extraction column 20.
  • Model calculations have been performed using the line up of Figure 2 as example, to illustrate the effect of the recycle stream 60 on the recovery of C 2 .
  • Table 1 shows the composition of the hydrocarbon feed stream 15, which is fed into the extraction column 20 at a pressure of 58 bara and a temperature of 20°C. Under these conditions, the hydrocarbon feed stream 15 is practically fully vaporous.
  • the full capacity feed rate in this example is 180 kg/s.
  • the extraction column 20 has been operated at 50 % of its full capacity, thereby simulating circumstances during a start up procedure, and allowing spare capacity in the extraction column 20 for handling a substantial recycle stream 60.
  • cooling the overhead condenser 31 at a base duty of 8.55 MW results in 7.14 kg/s of reflux stream in reflux line 36 at a temperature of about -46°C.
  • the recovery of ethane, without recycle, is 1.78 % while the amount of C 5 + in the lean methane-containing gas stream 510 is 0.040 mol%.
  • recovery of a selected component e.g. C 2 or C 3
  • recovery of a selected component is defined as the flow rate of that selected component in the liquid bottom stream 40 minus the flow rate of that component in the recycle stream 60, expressed as a percentage of the flow rate of the same component in the hydrocarbon feed stream 15 as it is delivered from the feed source 5.
  • Table 3 presents a reference case (not according to the present invention) wherein instead of a recycle portion from the first residue liquid bottom stream 50, an alternative recycle portion is drawn off from the liquid bottom stream 40 at a range of recycle fractions.
  • the temperature of the liquid bottom stream 40 was about -13 °C.
  • Table 3 Comparative example based on an alternative recycle from the liquid bottom stream 40 instead of the recycle from the first residue liquid bottom stream 50.
  • Recycle fract. Flow in reflux line 36 Duty in overhead condenser C 2 recov. C 3 recov. (%) (kg/s) 31 (MW) (%) (%) 0 7.14 8.55 1.78 5.93 25 7.69 8.30 1.79 5.96 50 9.42 8.02 1.85 6.17 67 14.2 8.71 2.35 8.14 75 18.8 9.10 2.64 9.45
  • recovery of a component is defined as the flow rate of that component in the not-recycled remainder of the liquid bottom stream 40 (this is what would be passed to the fractionation system) as a percentage of the flow rate of the same component in the hydrocarbon feed stream 15 as it is delivered from the feed source 5.
  • the C 5 + content in the lean methane-containing gas stream 510 is 0.040 mol% in all cases of Table 3.
  • Table 4 shows, for the same conditions as for Table 2, effective ethane and propane recovery values defined as the flow rate of ethane (respectively propane) in the remaining portion 70 of the first residue liquid bottom stream 50, expressed as a percentage of the flow rate of that same component in the hydrocarbon feed stream 15 as it is delivered from the feed source 5.
  • Effective ethane and propane recovery in the first residue liquid bottom stream 50 Same conditions as in Table 2. Recycle Fraction (%) Effective C 2 recovery (%) Effective C 3 recovery (%) 0 1.32 5.56 25 1.32 5.59 50 1.36 5.77 67 1.70 7.53 75 1.89 8.66
  • the effective recovery rates are lower than the recovery rates in the liquid bottom stream 40 shown in Table 2, because some of the ethane and propane ends up in the vapour phase in the first fractionated stream discharge line 305.
  • the degree that this happens depends on the operation conditions in the first fractionation column 350, and the type of column employed for this first fractionation column 350.
  • the first fractionation column 350 was optimized to minimize the amount of methane in the first residue liquid bottom stream 50. This can be mitigated by operating the first fractionation column 350 at a lower temperature, which increases the effective recovery values.
  • the loss of propane through the first fractionated stream discharge line 305 is less pronounced the loss of ethane.
  • the invention has been illustrated with reference to non-reboiled extraction columns.
  • at least part of the hydrocarbon feed stream 15 is fed into the extraction column 20 below the lowest of the contacting devices 23 arranged in the extraction column 20.
  • the invention can be applied to extraction column arrangements, including reboiled extraction columns.
  • different fractionation column arrangements can be applied than the one example embodiment of Figure 1 .

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JP2016136083A (ja) * 2015-01-23 2016-07-28 エア プロダクツ アンド ケミカルズ インコーポレイテッドＡｉｒ Ｐｒｏｄｕｃｔｓ Ａｎｄ Ｃｈｅｍｉｃａｌｓ Ｉｎｃｏｒｐｏｒａｔｅｄ 天然ガスの液化と統合した天然ガスからの重質炭化水素及びｎｇｌの改良分離
WO2017067908A1 (fr) 2015-10-21 2017-04-27 Shell Internationale Research Maatschappij B.V. Procédé et système de préparation d'un flux de gaz pauvre en méthane

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US4070165A (en) * 1975-12-15 1978-01-24 Uop Inc. Pretreatment of raw natural gas prior to liquefaction
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JP2016136083A (ja) * 2015-01-23 2016-07-28 エア プロダクツ アンド ケミカルズ インコーポレイテッドＡｉｒ Ｐｒｏｄｕｃｔｓ Ａｎｄ Ｃｈｅｍｉｃａｌｓ Ｉｎｃｏｒｐｏｒａｔｅｄ 天然ガスの液化と統合した天然ガスからの重質炭化水素及びｎｇｌの改良分離
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