EP1700071B1 - Verfahren zur konditionierung von flüssigerdgas - Google Patents

Verfahren zur konditionierung von flüssigerdgas 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
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.)
Not-in-force
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EP04798684A
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English (en)
French (fr)
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EP1700071A1 (de
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/de
Application granted granted Critical
Publication of EP1700071B1 publication Critical patent/EP1700071B1/de
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
    • 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
    • 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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    • 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
    • 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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    • 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
    • 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
    • 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
    • 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
    • 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
    • F17C2225/01—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
    • 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
    • F17C2227/01—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
    • F17C2227/01—Propulsion of the fluid
    • F17C2227/0128—Propulsion of the fluid with pumps or compressors
    • 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
    • F17C2227/01—Propulsion of the fluid
    • F17C2227/0128—Propulsion of the fluid with pumps or compressors
    • F17C2227/0171—Arrangement
    • F17C2227/0178—Arrangement in the vessel
    • 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
    • F17C2227/01—Propulsion of the fluid
    • F17C2227/0128—Propulsion of the fluid with pumps or compressors
    • F17C2227/0171—Arrangement
    • F17C2227/0185—Arrangement comprising several pumps or 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
    • 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
    • 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
    • F17C2265/01—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
    • 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
    • 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
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • 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
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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
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons

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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  • Chemical Kinetics & Catalysis (AREA)
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Claims (13)

  1. Verfahren zur Konditionierung von verflüssigtem Erdgas, welches das Anwenden der folgenden Schritte auf einen Speisestrom von verflüssigtem Erdgas umfasst:
    i. Verdampfen zumindest eines Hauptteils des Speisestroms von verflüssigtem Erdgas unter Erzeugung eines zumindest teilweise verdampften Erdgasstroms;
    ii. Trennen des zumindest teilweise verdampften Erdgasstroms unter Erzeugung eines ersten Stroms, der reich an Methan ist, und eines zweiten Stroms, der reich an Kohlenwasserstoffen mit zwei oder mehr Kohlenstoffatomen ist;
    iii. wenn erforderlich, Komprimieren des ersten Stroms aus Schritt (ii), um den Druck zu erhöhen und einen komprimierten Gasstrom zu erzeugen;
    iv. Kühlen des ersten Stroms aus Schritt (ii) oder des komprimierten Gasstroms aus Schritt (iii) durch Wärmeaustausch mit zumindest einem Teil des Speisestroms von verflüssigtem Erdgas unter Erzeugung eines flüssigen komprimierten Gasstroms;
    v. Leiten des zweiten Stroms aus Schritt (ii) ohne Pumpen zu einem Destillationsgefäß (11) unter Erzeugung eines Erdgasflüssigstroms und eines weiteren Stroms, der reich an Methan ist, wobei der Betriebsdruck des Destillationsgefäßes (11) derart ist, dass der weitere Strom, der reich an Methan ist, das Destillationsgefäß (11) bei einem Druck in dem Bereich von 2 bis 6 barg verlässt;
    vi. Kühlen des weiteren Stroms, der reich an Methan ist, aus Schritt (v) durch Wärmeaustausch mit zumindest einem Teil des Speisestroms von verflüssigtem Erdgas und anschließend Pumpen unter Erzeugung eines flüssigen komprimierten Gasstroms;
    vii. gegebenenfalls Vereinigen der flüssigen komprimierten Gasströme aus den Schritten (iv) und (vi);
    viii. Verdampfen der flüssigen komprimierten Gasströme aus den Schritten (iv), (vi) und/oder (vii) unter
    ix. Erzeugung eines konditionierten Erdgases und
    x. Gewinnen der Erdgasflüssigkeiten,
    dadurch gekennzeichnet, dass zumindest der Hauptteil des Speisestroms von verflüssigtem Erdgas in Schritt (i) durch Wärmeaustausch zumindest eines Teils des Speisestroms von verflüssigtem Erdgas mit dem ersten Strom aus Schritt (ii) oder dem komprimierten Gasstrom aus Schritt (iii) und mit dem weiteren Strom, der reich an Methan ist, aus Schritt (v) verdampft wird.
  2. Verfahren nach Anspruch 1, wobei in Schritt (v) der weitere Strom, der reich an Methan ist, das Destillationsgefäß (11) bei einem Druck in dem Bereich von 3 bis 5 barg verlässt.
  3. Verfahren nach entweder Anspruch 1 oder Anspruch 2, wobei die Trennung von Schritt (ii) durchgeführt wird, indem ein Separator (6) ohne Rücklaufströme verwendet wird und keine Packmaterialien oder Gas-Flüssigkeits-Trennböden enthalten sind.
  4. Verfahren nach einem der Ansprüche 1 bis 3, wobei die in Schritt (v) verwendete Destillationssäule (11) Gas-Flüssigkeits-Packung oder -Böden enthält und ohne die Gegenwart eines Rücklaufstroms betrieben wird.
  5. Verfahren nach einem der Ansprüche 1 bis 4, wobei mehr als 90 % des Speisestroms des Verfahrens in Schritt (i) verarbeitet werden, wobei nichts von dem Speisestrom als ein Rücklauf in einer in dem Verfahren verwendeten Säule verwendet wird.
  6. Verfahren nach einem der Ansprüche 1 bis 5, wobei der weitere Strom, der reich an Methan ist, aus Schritt (v) durch Wärmeaustausch mit zumindest einem Teil des Speisestroms von verflüssigtem Erdgas abgekühlt und anschließend gepumpt wird, um seinen Druck mit dem des in Schritt (iv) erzeugten flüssigen komprimierten Gasstroms abzugleichen, und die beiden Ströme vereinigt werden.
  7. Verfahren nach Anspruch 6, wobei der vereinigte Strom gepumpt wird, um den Druck zu erhöhen, und anschließend verdampft wird.
  8. Verfahren nach einem der Ansprüche 1 bis 7, wobei das Destillationsgefäß (11) in Schritt (ii) mit einem Rückverdampfer (20) versehen ist, der Meerwasser als Kühlmittel verwendet.
  9. Verfahren nach einem der Ansprüche 1 bis 8, wobei der Eingangsdruck des zumindest teilweise verdampften Erdgasstroms in Schritt (ii) im Bereich von 9 bis 13 barg liegt.
  10. Verfahren nach Anspruch 9, wobei der Druck des in Schritt (iii) erzeugten komprimierten Gasstroms von 2 auf 5 bar erhöht wird.
  11. Verfahren nach den Ansprüchen 9 oder 10, wobei der flüssige komprimierte Gasstrom aus Schritt (iv) einen Druck von 12 bis 16 barg hat.
  12. Verfahren nach einem der Ansprüche 1 bis 11, wobei die Temperatur des Speisestroms von verflüssigtem Erdgas im Bereich von -170 bis 150 °C liegt.
  13. Verfahren nach einem der Ansprüche 1 bis 12, wobei der/die in den Schritten (ii)/(iii) und (v) verwendete(n) Wärmetauscher (4) (ein) Wirbelzellentauscher ist/sind.
EP04798684A 2003-12-18 2004-11-25 Verfahren zur konditionierung von flüssigerdgas Not-in-force EP1700071B1 (de)

Priority Applications (2)

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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

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GBGB0329343.8A GB0329343D0 (en) 2003-12-18 2003-12-18 Process
PCT/GB2004/004988 WO2005059459A1 (en) 2003-12-18 2004-11-25 Process for the conditioning of liquefied natural gas

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EP1700071B1 true EP1700071B1 (de) 2012-06-13

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GB0503213D0 (en) * 2005-02-16 2005-03-23 Bp Exploration Operating Process for conditioning liquefied natural gas
DE602007005782D1 (de) * 2006-03-23 2010-05-20 Shell Int Research Verfahren und system für wiederverdampfung von flüssigerdgas
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
JP2017503994A (ja) * 2014-01-07 2017-02-02 リンデ アクチエンゲゼルシャフトＬｉｎｄｅ Ａｋｔｉｅｎｇｅｓｅｌｌｓｃｈａｆｔ 水素を含有する炭化水素混合物を分離する方法と分離装置とオレフィンプラント
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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ES2386144T3 (es) 2012-08-10
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CN1922456A (zh) 2007-02-28
WO2005059459A1 (en) 2005-06-30
CY1112994T1 (el) 2016-04-13
PT1700071E (pt) 2012-07-02
EP1700071A1 (de) 2006-09-13

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