EP1700071B1 - Procede permettant de conditionner le gaz naturel liquefie - Google Patents

Procede permettant de conditionner le gaz naturel liquefie Download PDF

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Publication number
EP1700071B1
EP1700071B1 EP04798684A EP04798684A EP1700071B1 EP 1700071 B1 EP1700071 B1 EP 1700071B1 EP 04798684 A EP04798684 A EP 04798684A EP 04798684 A EP04798684 A EP 04798684A EP 1700071 B1 EP1700071 B1 EP 1700071B1
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EP
European Patent Office
Prior art keywords
stream
natural gas
pressure
rich
gas
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Not-in-force
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EP04798684A
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German (de)
English (en)
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EP1700071A1 (fr
Inventor
David Andrew Harwood
Michael John Winstanley
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BP Exploration Operating Co Ltd
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BP Exploration Operating Co Ltd
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Priority to PL04798684T priority Critical patent/PL1700071T3/pl
Publication of EP1700071A1 publication Critical patent/EP1700071A1/fr
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Publication of EP1700071B1 publication Critical patent/EP1700071B1/fr
Priority to CY20121100688T priority patent/CY1112994T1/el
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • F25J3/0214—Liquefied natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • F17C9/04—Recovery of thermal energy
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
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    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2221/00—Handled fluid, in particular type of fluid
    • F17C2221/03—Mixtures
    • F17C2221/032—Hydrocarbons
    • F17C2221/033—Methane, e.g. natural gas, CNG, LNG, GNL, GNC, PLNG
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    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/01—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the phase
    • F17C2223/0146—Two-phase
    • F17C2223/0153—Liquefied gas, e.g. LPG, GPL
    • F17C2223/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
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    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/03—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the pressure level
    • F17C2223/033—Small pressure, e.g. for liquefied gas
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    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/04—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by other properties of handled fluid before transfer
    • F17C2223/042—Localisation of the removal point
    • F17C2223/046—Localisation of the removal point in the liquid
    • F17C2223/047—Localisation of the removal point in the liquid with a dip tube
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    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/01—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the phase
    • F17C2225/0107—Single phase
    • F17C2225/0123—Single phase gaseous, e.g. CNG, GNC
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/03—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the pressure level
    • F17C2225/035—High pressure, i.e. between 10 and 80 bars
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/01—Propulsion of the fluid
    • F17C2227/0128—Propulsion of the fluid with pumps or compressors
    • F17C2227/0135—Pumps
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
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    • F17C2227/0157—Compressors
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
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    • F17C2227/0171—Arrangement
    • F17C2227/0178—Arrangement in the vessel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
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    • F17C2227/0171—Arrangement
    • F17C2227/0185—Arrangement comprising several pumps or compressors
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0302—Heat exchange with the fluid by heating
    • F17C2227/0306—Heat exchange with the fluid by heating using the same fluid
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0367—Localisation of heat exchange
    • F17C2227/0388—Localisation of heat exchange separate
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/01—Purifying the fluid
    • F17C2265/015—Purifying the fluid by separating
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/02—Mixing fluids
    • F17C2265/022—Mixing fluids identical fluid
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/05—Regasification
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    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2270/00—Applications
    • F17C2270/01—Applications for fluid transport or storage
    • F17C2270/0134—Applications for fluid transport or storage placed above the ground
    • F17C2270/0136—Terminals
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
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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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
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    • 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
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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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • 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
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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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons

Definitions

  • This invention relates to a process for conditioning liquefied natural gas.
  • Liquefied natural gas needs to be vaporized before being fed into a pipeline for distribution.
  • the LNG is fed into a tank. This inevitably results in some gas vapour loss; typically this off-gas is compressed and then passed to a boil-off condenser where it is condensed, for example by passing a quantity of LNG from the tank into the boil-off condenser where the boil off gas, at increased pressure, is combined with the LNG stream to produce an all-liquid stream which may be passed back into the tank or combined with an outflow stream from the tank.
  • LNG is then passed from the tank to a pump which discharges the LNG, at a suitable pressure, to a pipeline, via one or more heat exchangers which vaporize the LNG.
  • the LNG does not meet required product or pipeline specifications because of the presence of excess quantities of hydrocarbons containing two or more carbon atoms, and various additional processing steps are required.
  • GB 1,185,053 discloses a high pressure process for obtaining a fluid rich in methane from LNG.
  • the high pressures used lead to high engineering and operating costs.
  • Fig. 1 shows a column which is fed by a pump which subjects the feed stream to the column to a pressure of 25 bars absolute, which means that the column must be engineered to operate at a pressure of close to 25 bars absolute.
  • the scheme is complex, initially splitting the feed stream into at least two parts, with at least one part being used as a reflux stream to a packed column.
  • US 2003/0158458A1 discloses a scheme for separating methane-rich and ethane-rich components from an LNG stream, which includes a separator and a column.
  • Fig. 1 shows the feed stream being passed direct to the column 28, which is operated using a reflux pumped from the separator 24.
  • the separator acts to recycle the gas stream from the column, and therefore .only part of the LNG feed is subject to that separation.
  • US 6,564,579 describes a process for the removal of natural gas liquids, typically hydrocarbons containing two or more carbon atoms, from LNG, in order to provide a product with a reduced heating value which meets pipeline or other commercial specifications.
  • This process which is of a type which may be referred to as conditioning, includes the following steps: vaporizing at least a major portion of a stream of the liquefied natural gas to produce an at least partially vaporized natural gas stream; fractionating the at least partially vaporized natural gas stream to produce a gas stream and a natural gas liquids stream; compressing the gas stream to increase the pressure of the gas stream by about 50 to about 150 psi to produce a compressed gas stream and cooling the compressed gas stream by heat exchange with the stream of liquefied natural gas to produce a liquid compressed gas stream; pumping the liquid compressed gas stream to produce a high-pressure liquid stream at a pressure from about 800 to about 1200 psig; vaporizing the high-pressure liquid stream to produce a conditioned natural gas suitable for delivery to a pipeline
  • the liquids recovered from separator 86 are passed via a line 88 to a pump 90 from which they are passed via a line 92 to distillation vessel 38.
  • Distillation vessel 38 functions as described previously to separate NGLs, which are recovered through a line 46, and to produce an overhead gas stream, which comprises primarily methane.
  • This gaseous stream is recovered through a line 48 and is passed to combination with the gas stream in line 54.
  • the combined streams are then liquefied in heat exchanger 34.” Because the pressure in line 48 must be the same as the pressure in line 53, column 38 must be operated with a gaseous outlet pressure of 100 to about 300 psig. This means that the liquid stream from 86 must be pumped (via pump 90) to column 38.
  • US 3837821 which discloses the features of the preamble of claim 1, discloses a method of production under high pressure of a gas rich in methane, to which is added a volatile gaseous fraction in which the natural gas is brought to an intermediate pressure and a volatile gaseous fraction is added to the natural gas at the said intermediate pressure, wherein the volatile gaseous fraction is added to the natural gas in the liquid state, after which the mixture obtained is brought to the pressure of the distribution system reheated and vaporized.
  • the present invention provides a process for the conditioning of liquefied natural gas, which comprises applying the following steps to a feed stream of liquefied natural gas:
  • the process according to the invention produces a conditioned natural gas which is suitable for delivery to a pipeline, or for other commercial use, together with natural gas liquids.
  • the natural gas liquids comprise hydrocarbons having 2 or more carbon atoms.
  • the initial natural gas liquids product obtained by the process of the invention can be further processed, for example by the removal of ethane in a deethaniser column.
  • step (i) of the process is fed to step (i) of the process.
  • a small quantity of the feed stream may be used to perform certain functions within the process, for example to cool a compressor. It is however an advantage of the process according to the invention that none of the feed stream is required to act as a reflux in columns used in the process, unlike the process of US 6,604,380 , in which part of the incoming cold LNG bypasses the vapourising heat exchanger and is used as reflux in the column 22 and possibly the separator 20.
  • step (ii) is carried out using a separator which contains a minimum of internal structure. No reflux streams are necessary, and therefore no packing materials or gas-liquid separation trays are required, although if desired the separator may contain one or more knit-mesh structures to assist in removing entrained liquids.
  • the output from step (ii) comprises two separate streams, a gas stream and a liquids stream.
  • the gas stream is compressed if necessary in optional step (iii) (whether this is necessary will depend upon the operating pressure of the fractionation step (ii)) and sent to a heat exchanger where, in step (iv), it is cooled against the LNG feed stream.
  • the liquids stream is separated into a natural gas liquids stream and a gas stream in the distillation vessel of step (v), which vessel contains gas-liquid separation packing or trays to provide vapour-liquid contact. Said vessel does not require the presence of a reflux stream; specifically, it does not require the presence of a cold LNG reflux stream obtained from the feed stream to the process.
  • the gas stream resulting from step (v) is sent to a heat exchanger where it is cooled against the LNG feed stream (step (vi)). It is an important feature of the process of the invention that the gas streams from steps (ii)/(iii) and (v) are at different pressures from each other and arc therefore cooled in separate streams.
  • the heat exchange on these two streams may be carried out using different heat exchangers, or it may be carried out using a multi-stream heat exchanger.
  • the heat exchanger(s) used is a plate-fin exchanger; these are very compact, and tighter temperature approaches are possible.
  • the gas stream originating from step (v) may be compressed to equalise its pressure with that of the higher-pressure stream originating from step (ii)/(iii), and the two streams may be combined prior to pumping to further increase the pressure, followed by vaporization to produce the desired conditioned natural gas.
  • the process of the present invention provides a number of advantages relative to the process described in Figure 5 of US 6,564,579 . Because there is no requirement to merge two separate gas streams prior to heat exchange, the distillation vessel used in step (iv) operates at a relatively low pressure, the exit stream rich in methane being at a pressure in the range of from 2 to 6 barg, preferably from 3 to 5 barg (in contrast to the column of Figure 5 of US 6,564,579 which operates at a relatively high pressure, the exit stream being at 100 to 300 psig, equivalent to 6.9 to 20.7 barg).
  • the liquid stream from step (ii) may therefore be let down into the distillation vessel: no pump is required to transfer the natural gas liquids stream from step (ii) to the distillation vessel, and the process is thereby simplified.
  • the compressor used to compress the gas stream exiting from the distillation vessel in step (ii) can be used at a lower pressure differential.
  • the distillation vessel may be reboiled using seawater rather than steam which is required for the reboiling of higher pressure vessels, although steam may be used if desired.
  • keeping the gas streams from steps (ii)/(iii) and (v) separate rather than combining them prior to heat exchange may improve the heat recovery efficiency, especially if a plate-fin heat exchanger(s) is used.
  • the process of the invention may be integrated with existing LNG handling facilities.
  • the process may also form part of an integrated energy recovery system as described in US 6,564,579 .
  • a tank 1 contains LNG forming the feed to the process.
  • Tank 1 is typically a cryogenic tank.
  • An in-tank pump 2 pumps the LNG from tank 1 via a pump 3 which increases the pressure typically to around 9 to 13 barg.
  • From the pump 3 the LNG is passed to a multi-channel heat exchanger 4, preferably of the plate-fin type.
  • a line 5 carries the LNG to a separation vessel 6 having two outlet lines and a minimum of internal structure.
  • Outlet line 7 carries a gas stream from the separation vessel 6 to a compressor 8 where the pressure is increased typically by from 2 to 5 bar, for example around 3 bar.
  • a line 9 feeds the resulting compressed gas stream back to one channel 30 of the multi-channel heat exchanger 4.
  • Outlet line 10 carries a liquid stream from the separation vessel to a distillation vessel 11 containing gas-liquid separation packing or trays to provide vapour-liquid contact, which separates the input stream into a liquid stream comprising natural gas liquids which are removed via line 12, and a gas stream which is removed via line 13 and fed back to the multi-channel heat exchanger 4 using a separate channel 31 from that used by line 9.
  • the pressure drop across distillation vessel 11 is such that pressure of the gas stream removed via line 13 is in the range of from 2 to 6 barg.
  • the distillation vessel 11 is provided with a reboiler 20 comprising a heat exchanger 21 and a line 22 forming a closed loop back to the distillation vessel 11.
  • the stream exiting channel 30 is carried by line 14 typically at a pressure of from 12 to 16 barg to mixing point 15.
  • the stream exiting channel 31 is carried to a pump 16 where its pressure is equalised to that of the stream exiting channel 30 before being carried to mixing point 15 where it is combined with the stream exiting channel 30.
  • the combined streams are then passed to pump 17 and subsequently vaporised in heat exchanger 18 before being discharged into a pipeline.
  • the whole process is carried out at normal cryogenic temperatures, for example, the feed stream of LNG is typically at a temperature of around -170 to -150°C, the temperature at each point in the process depending upon the pressure.

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Abstract

L'invention concerne un procédé amélioré permettant de conditionner le gaz naturel liquéfié. Ledit procédé consiste à séparer (6) au moins partiellement un flux de gaz naturel (5) vaporisé afin de produire un premier flux (7) riche en méthane et un second flux (10) riche en hydrocarbures comprenant deux atomes de carbone ou plus; et à faire passer ce second flux sans pompage dans un récipient de distillation (11) afin de produire un flux des liquides (12) de gaz naturel gaz et un flux (13) riche en méthane, la pression de fonctionnement du récipient de distillation étant telle que le flux riche en méthane sort dudit récipient de distillation à une pression se situant dans une plage comprise entre 2 et 6 bars.

Claims (13)

  1. Procédé pour le conditionnement de gaz naturel liquéfié, qui comprend l'application des étapes suivantes à un courant de charge de gaz naturel liquéfié :
    i. vaporisation d'au moins une partie majeure du courant de charge de gaz naturel liquéfié pour produire un courant de gaz naturel au moins partiellement vaporisé ;
    ii. séparation du courant de gaz naturel au moins partiellement vaporisé pour produire un premier courant qui est riche en méthane et un deuxième courant qui est riche en hydrocarbures ayant deux ou plus de deux atomes de carbone ;
    iii. si nécessaire compression du premier courant obtenu dans l'étape (ii) pour augmenter la pression et produire un courant de gaz comprimé ;
    iv. refroidir le premier courant obtenu dans l'étape (ii) ou le courant de gaz comprimé obtenu dans l'étape (iii) par échange de chaleur avec au moins une partie du courant de charge de gaz naturel liquéfié pour produire un courant de gaz comprimé liquide ;
    v. passage du deuxième courant obtenu dans l'étape (ii) sans pompage vers un récipient de distillation (11) pour produire un courant liquide de gaz naturel et un autre courant riche en méthane, la pression opérationnelle du récipient de distillation (11) étant telle que l'autre courant riche en méthane sorte du récipient de distillation (11) sous une pression située dans la plage allant de 2 à 6 bar au manomètre ;
    vi. refroidissement de l'autre courant riche en méthane obtenu dans l'étape (v) par échange de chaleur avec au moins une partie du courant de charge du gaz naturel liquéfié et ensuite pompage pour produire un courant de gaz comprimé liquide ;
    vii. éventuellement combinaison des courants de gaz comprimé liquide obtenus dans les étapes (iv) et (vi) ;
    viii. vaporisation des courants de gaz comprimé liquide obtenus dans les étapes (iv), (vi) et/ou (vii) pour
    ix. produire un gaz naturel conditionné ; et
    x. récupération des liquides du gaz naturel,
    caractérisé en ce qu'au moins la majeure partie du courant de charge de gaz naturel liquéfié est vaporisée dans l'étape (i) par échange de chaleur d'au moins une partie du courant de charge de gaz naturel liquéfié avec le premier courant obtenu dans l'étape (ii) ou le courant de gaz comprimé obtenu dans l'étape (iii) et avec l'autre courant riche en méthane obtenu dans l'étape (v).
  2. Procédé selon la revendication 1, dans lequel, dans l'étape (v), l'autre courant riche en méthane sort du récipient de distillation (11) sous une pression située dans la plage allant de 3 à 5 bar au manomètre.
  3. Procédé selon l'une ou l'autre de la revendication 1 et de la revendication 2, dans lequel la séparation de l'étape (ii) est effectuée au moyen d'un séparateur (6) sans courant de reflux et ne contenant pas de matériaux de garnissage ou de plateaux de séparation gaz-liquide.
  4. Procédé selon l'une quelconque des revendications 1 à 3, dans lequel la colonne de distillation (11) utilisée dans l'étape (v) contient des plateaux ou un garnissage de séparation gaz-liquide et fonctionne en l'absence d'un courant de reflux.
  5. Procédé selon l'une quelconque des revendications 1 à 4, dans lequel plus de 90 % du courant de charge pour le procédé sont traités dans l'étape (i), aucune partie dudit courant de charge n'étant utilisée pour servir de reflux dans une quelconque colonne utilisée dans le procédé.
  6. Procédé selon l'une quelconque des revendications 1 à 5, dans lequel l'autre courant riche en méthane obtenu dans l'étape (v) est refroidi par échange de chaleur avec au moins une partie du courant de charge de gaz naturel liquéfié et est ensuite pompé pour que sa pression soit égalisée avec celle du courant de gaz comprimé liquide produit dans l'étape (iv), et les deux courants sont combinés.
  7. Procédé selon la revendication 6, dans lequel ledit courant combiné est pompé pour que la pression soit augmentée et ensuite vaporisé.
  8. Procédé selon l'une quelconque des revendications 1 à 7, dans lequel le récipient de distillation (11) dans l'étape (ii) est doté d'un rebouilleur (20) qui utilise de l'eau de mer en tant que caloporteur.
  9. Procédé selon l'une quelconque des revendications 1 à 8, dans lequel la pression d'entrée du courant de gaz naturel au moins partiellement vaporisé dans l'étape (ii) est située dans la plage allant de 9 à 13 bar au manomètre.
  10. Procédé selon la revendication 9, dans lequel la pression du courant de gaz comprimé produit dans l'étape (iii) est augmentée de 2 à 5 bar.
  11. Procédé selon la revendication 9 ou 10, dans lequel le courant de gaz comprimé liquide obtenu dans l'étape (iv) est sous une pression de 12 à 16 bars au manomètre.
  12. Procédé selon l'une quelconque des revendications 1 à 11, dans lequel la température du courant de charge de gaz naturel liquéfié est située dans la plage allant de -170 à -150°C.
  13. Procédé selon l'une quelconque des revendications 1 à 12, dans lequel le ou les échangeurs de chaleur (4) utilisés dans les étapes (ii)/(iii) et (iv) sont des échangeurs à plaques-ailettes.
EP04798684A 2003-12-18 2004-11-25 Procede permettant de conditionner le gaz naturel liquefie Not-in-force EP1700071B1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
PL04798684T PL1700071T3 (pl) 2003-12-18 2004-11-25 Sposób kondycjonowania skroplonego gazu ziemnego
CY20121100688T CY1112994T1 (el) 2003-12-18 2012-08-02 Διαδικασια βελτιωσης υγροποιημενου φυσικου αεριου

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GBGB0329343.8A GB0329343D0 (en) 2003-12-18 2003-12-18 Process
PCT/GB2004/004988 WO2005059459A1 (fr) 2003-12-18 2004-11-25 Procede permettant de conditionner le gaz naturel liquefie

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EP1700071A1 EP1700071A1 (fr) 2006-09-13
EP1700071B1 true EP1700071B1 (fr) 2012-06-13

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CN (1) CN1922456A (fr)
CY (1) CY1112994T1 (fr)
ES (1) ES2386144T3 (fr)
GB (1) GB0329343D0 (fr)
PL (1) PL1700071T3 (fr)
PT (1) PT1700071E (fr)
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GB0503213D0 (en) * 2005-02-16 2005-03-23 Bp Exploration Operating Process for conditioning liquefied natural gas
US20090229276A1 (en) * 2006-03-23 2009-09-17 Marc Alexander Rieder Method and system for the regasification of lng
US20140366577A1 (en) 2013-06-18 2014-12-18 Pioneer Energy Inc. Systems and methods for separating alkane gases with applications to raw natural gas processing and flare gas capture
RU2663159C2 (ru) * 2014-01-07 2018-08-01 Линде Актингезелльшафт Способ разделения водородсодержащей углеводородной смеси, сепарационная секция и олефиновая установка
KR102651092B1 (ko) * 2017-01-24 2024-03-26 한화오션 주식회사 액화천연가스 연료 선박의 연료 공급 시스템 및 방법

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US3452548A (en) * 1968-03-26 1969-07-01 Exxon Research Engineering Co Regasification of a liquefied gaseous mixture
US3837821A (en) 1969-06-30 1974-09-24 Air Liquide Elevating natural gas with reduced calorific value to distribution pressure
US6941771B2 (en) 2002-04-03 2005-09-13 Howe-Baker Engineers, Ltd. Liquid natural gas processing
US6564579B1 (en) * 2002-05-13 2003-05-20 Black & Veatch Pritchard Inc. Method for vaporizing and recovery of natural gas liquids from liquefied natural gas

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GB0329343D0 (en) 2004-01-21
PL1700071T3 (pl) 2012-11-30
WO2005059459A1 (fr) 2005-06-30
CY1112994T1 (el) 2016-04-13
EP1700071A1 (fr) 2006-09-13
CN1922456A (zh) 2007-02-28
PT1700071E (pt) 2012-07-02
ES2386144T3 (es) 2012-08-10

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