EP1861671B1 - Process and apparatus for extracting natural gas liquids from a stream of liquefied natural gas - Google Patents
Process and apparatus for extracting natural gas liquids from a stream of liquefied natural gas Download PDFInfo
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- EP1861671B1 EP1861671B1 EP06708800.5A EP06708800A EP1861671B1 EP 1861671 B1 EP1861671 B1 EP 1861671B1 EP 06708800 A EP06708800 A EP 06708800A EP 1861671 B1 EP1861671 B1 EP 1861671B1
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- stream
- heat exchanger
- exchanger arrangement
- natural gas
- feeding point
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims description 97
- 239000007788 liquid Substances 0.000 title claims description 56
- 238000000034 method Methods 0.000 title claims description 53
- 239000003949 liquefied natural gas Substances 0.000 title claims description 39
- 239000003345 natural gas Substances 0.000 title claims description 38
- 238000004821 distillation Methods 0.000 claims description 52
- 238000010438 heat treatment Methods 0.000 claims description 15
- 239000007789 gas Substances 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 8
- 238000004891 communication Methods 0.000 claims description 6
- 239000012530 fluid Substances 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 5
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 24
- 238000010992 reflux Methods 0.000 description 23
- 238000000926 separation method Methods 0.000 description 13
- 239000001294 propane Substances 0.000 description 12
- 238000011084 recovery Methods 0.000 description 10
- 239000000047 product Substances 0.000 description 9
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 6
- 239000012071 phase Substances 0.000 description 4
- 238000011144 upstream manufacturing Methods 0.000 description 4
- 238000002309 gasification Methods 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 238000005201 scrubbing Methods 0.000 description 3
- 239000001273 butane Substances 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- 238000011064 split stream procedure Methods 0.000 description 2
- 239000003381 stabilizer Substances 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
Images
Classifications
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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
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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
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- 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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- 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
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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
- 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
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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
- 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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- 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
- F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
- F25J2200/92—Details relating to the feed point
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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
- 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
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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
- 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
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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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
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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
- 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
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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
- 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
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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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/88—Quasi-closed internal refrigeration or heat pump cycle, if not otherwise provided
Definitions
- the present invention relates to a method and apparatus for deriching a stream of liquefied natural gas (LNG) by extracting a natural gas liquid from the stream of liquefied natural gas.
- LNG liquefied natural gas
- the resulting stream of deriched liquefied natural gas can be in liquid and/or vapour phase for instance utilizing subsequent regasification.
- deriching is used in the present specification and claims as an opposite term for enriching, and is understood to include a meaning of removing hydrocarbon compounds higher than methane, i.e. "stripping" or "making leaner".
- natural gas liquid is understood to include hydrocarbon compounds higher than methane, including ethane, ethylene, propane, propylene, butane and isomeric variations thereof, and butylenes and isomeric variations thereof.
- liquefied natural gas typically contains higher hydrocarbon compounds including ethane, propane, and various isomeric forms of butane. These additional compounds have higher heating values than methane. Different specifications of liquefied natural gas, in particular with regard to heating value, are demanded in various markets.
- US patent 6,604,380 discloses such a method for the recovery of natural gas liquids.
- a liquefied natural gas feed stream is split.
- one portion of the split stream is heated in a heat exchanger whereby it is partially vapourised and then fed to a feed separator.
- a natural gas liquid rich bottom stream is removed from the feed separator and routed to a second separation method including a stabilizer.
- the other portion of the split stream bypasses the heat exchanger and is fed at a very low temperature of around -157 °C (-250 °F) as an external reflux into the second separation method.
- the methane-rich overhead vapour streams are drawn from the feed separator and the stabilizer, and combined and directed through the heat exchanger where it is cooled against the one portion of the split feed stream.
- WO 2004/109180 discloses a method of processing LNG in a plant in which a heat source vaporizes pressurized LNG which is subsequently expanded to produce work in an open power cycle.
- One or more of the above and other objects may be achieved according to the present invention by providing a method of deriching a stream of liquefied natural gas by extracting a natural gas liquid from the stream of liquefied natural gas, the method at least comprising the steps of:
- An advantage of the present invention is that it provides more flexibility in choosing the temperature profile in the distillation column, which facilitates efficient control of the method conditions in the distillation column.
- the overhead vapour stream from the distillation column is partially condensed during the cooling in the second heat exchanger arrangement and the intermediate deriched stream comprises an intermediate condensate which can be passed to the distillation column via the third feeding point, and an intermediate vapour which can be passed to the first heat exchanger arrangement.
- a further advantage is that the intermediate condensate is enriched in heavier components including natural gas liquids. Instead of submitting this condensate to the first heat exchanger arrangement it is re-submitted to the distillation column as an internal reflux. Hence the recovery of the natural gas liquid is significantly improved.
- an intermediate temperature can be chosen in the intermediate deriched stream that allows to tailor the composition of the condensate.
- Another advantage of the invention is that the heating and cooling upstream respectively downstream of the distillation column is performed in at least two stages.
- the resulting intermediate streams between the at least two stages are thus available for use in the method in addition to the fully heated respectively cooled streams.
- One way of utilizing the intermediate feed stream is as an external reflux having a temperature that is lower than that of the portion being fed to the distillation column via the second feeding point but not as low as that of the original feed stream.
- an external reflux stream having a temperature as low as of liquefied natural gas (approximately of around -157 °C, or less than -140 °C) is not generally required for an efficient separation of natural gas liquid components from liquefied natural gas.
- An advantage of the invention is that the temperature of the external reflux can be chosen higher than the temperature of the feed stream, for instance higher than -140 °C.
- equipment such as the distillation column or a reboiler (if provided), can be smaller sized, and less power needs to be dissipated in a reboiler.
- the high-quality cold in the feed stream thus becomes available fully for recondensating the deriched natural gas.
- the intermediate feed stream can either be fully liquid or partly vapourized.
- the heating of the feed stream in the first heat exchanger arrangement comprises partly vapourizing the feed stream whereby the intermediate feed stream comprises a mixture of liquid intermediate feed fraction and vaporous intermediate feed fraction
- the intermediate feed stream comprises a mixture of liquid intermediate feed fraction and vaporous intermediate feed fraction
- the vaporous intermediate feed fraction because of it relatively low temperature compared to the temperature after the second heating, is already relatively lean from natural gas liquids and does not have to be further distilled. It can be mixed in with a final product stream.
- the present invention provides a deriched natural gas stream obtained by the method according to the present invention as well as an apparatus suitable for performing the method according to the present invention.
- Preferred embodiments for the apparatus are derivable from preferred embodiments of the method and/or from the detailed description of embodiments set out below.
- Figure 1 schematically shows an apparatus for deriching a stream of liquefied natural gas by extracting a natural gas liquid from the stream of liquefied natural gas.
- a feed line 1 is connectable to a source of the liquefied natural gas.
- An optional pump 3 is provided in the feed line 1, of which the high-pressure outlet is in fluid communication with a first heat exchanger arrangement 5 via line 2.
- An intermediate feed line 7 fluidly connects a first outlet 6 of the first heat exchanger arrangement 5 with a distributor 14.
- the distributor 14 has two outlets connected to lines 17 and 19. If desired, the distributor 14 may have more than two outlets.
- Line 17 connects to a distillation column 21 via an optional first control valve 23 and a first feeding point 25 provided in an upper part of the distillation column 21.
- the other line, line 19, also connects to the distillation column 21 but via a second heat exchanger arrangement 26, line 20, which can be optionally provided with a second control valve 27, and a second feeding point 29.
- the first outlet 6 of the first heat exchanger arrangement 5 is in fluid communication with the second heat exchanger arrangement 26.
- Line 17 bypasses the second heat exchanger arrangement 26.
- the second feeding point 29 of the distillation column 21 is preferably located gravitationally lower than the first feeding point 25.
- the distillation column 21 has a lower portion provided with a discharge opening 31 for withdrawing a liquid stream 35 from the distillation column 21.
- An optional reboiler 33 may be provided in line 35 connecting to the discharge opening 31.
- a reboil return line 37 feeds back from the reboiler 33 into the lower portion of the distillation column 21.
- the optional reboiler 33 may be integrated with the distillation column 21 instead of the shown external arrangement.
- a line 38 connects to line 35 or to the optional reboiler 33 for discharging the natural gas liquid.
- the distillation column 21 also has an upper portion provided with an overhead vapour outlet 39.
- the overhead vapour outlet 39 is in fluid communication with the first heat exchanger arrangement 5 via the second heat exchanger arrangement 26.
- Line 40 extends between the overhead vapour outlet 39 and the second heat exchanger arrangement 26, and is connected to line 48 that extends between the second heat exchanger arrangement 26 and the first heat exchanger arrangement 5, and is connected to line 55 downstream of the first heat exchanger arrangement 5 via a second outlet 41 of the first heat exchanger arrangement 5.
- An optional pump 65 can be included in line 55, which discharges into line 67, for increasing the pressure to produce a deriched liquefied natural gas stream at a pressure according to a local specification.
- Line 67 can be connected to any type of re-gasification system, including systems known from an article "Integrated gas processing with various LNG sources” by Joseph Cho et al, as published in LNG Journal January/February 2005 pp 23-27 .
- the above-described apparatus is capable of deriching a stream of liquefied natural gas by extracting a natural gas liquid from the stream of liquefied natural gas.
- An optional bypass line 59 can be provided to fluidly connect line 1 or the high-pressure outlet of pump 3 upstream of the first heat exchanger arrangement 5 with line 55 downstream of the first heat exchanger arrangement 5.
- the optional bypass line 59 can be provided with a control valve 61. With the bypass line 59 the deriching arrangement can be bypassed and the extraction of the natural gas liquid avoided.
- the apparatus of Figure 1 works as follows.
- a feed stream containing the stream of liquefied natural gas is supplied via feed line 1 and heated in the first heat exchanger arrangement 5 against an intermediate deriched stream in line 48 to form an intermediate feed stream 7.
- the intermediate feed stream 7 is split in the distributor 14 into at least a first portion 17 and a second portion 19.
- the first portion 7 is passed to the distillation column 21 and fed into it via the first feeding point 25.
- Pressure and temperature can be controlled utilizing control valve 23.
- the second portion 19 of the intermediate feed stream 7 is passed to the second heat exchanger arrangement 26 wherein it is further heated, against an overhead stream in line 40.
- the resulting further heated stream is then supplied to the distillation column 21 via line 20 and the second feeding point 29. Pressure can be controlled employing control valve 27.
- the second portion 19 of the intermediate feed stream 7 is at least partially vapourised. It is generally recommended to vapourize to a molar fraction of at least 60%.
- the first portion 17 acts as an external reflux stream in the distillation process. It helps scrubbing the natural gas liquid from vapour generated from the second portion 19 as well as in optional reboiler 33. The scrubbing is facilitated by the preference that the first feeding point 25 is located gravitationally higher than the second feeding point 29.
- a liquid stream containing the natural gas liquid is then withdrawn from a lower portion of the distillation column 21 via the discharge opening 31 into line 35.
- the liquid stream is heated and partly fed back via line 37 to the lower portion of the distillation column 21 to allow some vapour to form containing relatively lighter molecules.
- the remainder is discharged as natural gas liquid into line 38.
- an overhead vapour stream 40 is withdrawn from an upper portion of the distillation column 21.
- the overhead vapour stream 40 is a deriched stream containing mainly methane and sometimes also other components such as for instance ethane and a remainder of propane.
- the overhead vapour stream 40 is passed to the second heat exchanger arrangement 26 where it is cooled against the intermediate feed stream to form an intermediate deriched stream 48 of which at least a portion is thereafter passed to the first heat exchanger arrangement 5 and further cooled against the feed stream 1 to form a product stream 55 of deriched natural gas.
- the product stream 55 can be fully re-condensed.
- the product stream 55 is combined with a bypass stream drawn from the feed stream 2 via line 59.
- the pressure of the product stream in line 55 can then be raised to a desired pressure level by means of the optional pump 65, which is generally more energy efficient as the stream in line 55 generally tends to be fully condensed.
- the product stream is discharged through line 67 after which it can be further processed (not shown), for instance including re-gasification by heating it to convert it into a gaseous stream.
- an optional compressor (not shown) can be provided in line 40 to be able to generate a comfort margin in the pressure to ensure that the product stream in line 55 leaving the first heat exchanger arrangement 5 at outlet 41 is not only fully re-condensed but also sub-cooled to a sufficient degree. This is of less importance when a substantial amount of the feed stream 2 is allowed to bypass via line 59, as in that case the product stream leaving the first heat exchanger arrangement 5 is subjected to direct heat exchange.
- An advantage of having two heat exchanger arrangements 5,26 is that the intermediate streams 7 and/or 48 are now available for use in the process.
- a portion (first portion 17) of the intermediate stream 7 is utilized as external reflux having a temperature that is lower than that of the portion (second portion 19) being fed to the distillation column 21 via the second feeding point 29 but not as low as the feed stream 1.
- increased temperature control is achieved over the reflux stream 17 and the further heated feed stream 20, as compared to what is possible in the process as described in US patent 6,604,380 .
- This increased flexibility enables efficient control of the process conditions in the distillation column 21, to achieve desired separation between overhead stream 40 and bottom stream 38 of a selected natural gas liquid component.
- FIG 2 is based on the process as shown and explained above with reference to Figure 1 and shows a gas/liquid separator 9 (referred to in the claims as "second gas/liquid separator") that is arranged in the connection between the first outlet 6 of the first heat exchanger arrangement 5 and the distributor 14.
- the gas/liquid separator is here provided in the form of a feed separation vessel 9.
- the first outlet 6 of the first heat exchanger arrangement 5 is connected with the feed separation vessel 9.
- the feed separation vessel 9 has a bottom outlet 11 and an overhead outlet 13.
- the bottom outlet 11 is connected to the distributor 14 via line 15.
- the overhead outlet 13 is fluidly connected to line 48 via line 57 upstream of the first heat exchanger arrangement 5.
- the vapour will contain predominantly the leaner components such as methane.
- the components with higher heating values, such as propane will still be essentially fully in the liquid phase together with ethane and methane.
- the vapourised fraction does not have to be further distilled and can be mixed in with the distilled stream in line 48 to be recondensed in the first heat exchanger arrangement 5.
- the molar fraction of vapour can be between 1 and 90%.
- the liquid that is drawn from the bottom outlet 11 of the separator 9 is led to the distributor 14, where part of it is sent to the distillation 21 column via line 17 as an external reflux thereby bypassing the second heat exchanger arrangement 26.
- An advantage of this process is that the external reflux is fully liquid so that it can be fully effective as scrubbing medium.
- the temperature of the external reflux is lower than that of the portion being fed to the distillation column via the second feeding point 29, but not as low as that of the original feed stream 1.
- the temperature can be controlled by choosing the amount of heat exchange in the first heat exchanger 5, optionally in co-dependence of controlling the amount of expansion in control valve 23.
- An advantage of the optional control valves 23 and 27 is that the distillation column 21 is operated at a lower pressure than the feed separator 9, which improves the separation efficiency of natural gas liquid components in the column 21.
- an optional overhead compressor 63 can be provided between the overhead vapour outlet 39 of the distillation column 21 and the second heat exchanger arrangement 26.
- the optional pressure drop over valves 23 and 27 can be compensated whereby the pressure in line 48 can be brought to the pressure level as set by the feed stream in line 7.
- the compressor 63 upstream of the second heat exchanger arrangement 26, because the overhead stream 40 is by virtue of the distillation column 21 always fully vaporous whereas downstream of the second heat exchanger arrangement 26 the product stream can be of a multi-phase nature.
- FIG. 1 shows an embodiment according to the present invention which is based on the embodiment as shown and explained above with reference to Figure 1 , wherein an internal reflux system is provided in the connection line 48 between the distillation column's overhead vapour outlet 39 and the first heat exchanger arrangement 5.
- the reflux system here shown comprises a gas/liquid separator (referred to in the claims as "first gas/liquid separator") here provided in the form of a reflux separation vessel 43.
- the reflux separation vessel 43 is arranged downstream of the second heat exchanger arrangement 26 in line 48 and connected to the second heat exchanger arrangement 26 via line 42.
- the separator 43 has a bottom outlet 45 and an overhead outlet 47.
- the bottom outlet 45 is connected to the distillation column 21 via line 49 and a third feeding point 51 to provide a reflux stream.
- An optional control valve 53 can be provided in line 49.
- the third feeding point 51 is best arranged gravitationally higher than the second feeding point 29, as the temperature of the reflux stream 49 is generally lower than that of the further heated feed stream 20, and gravitationally lower than the first feeding point 25.
- the overhead outlet 47 of the reflux separation vessel 43 is fluidly connected with the first heat exchanger arrangement 5 via line 48.
- the mass selectivity of the reflux stream can be tailored by choice of that temperature, and optionally also the pressure drop in optional valve 53.
- methane or ethane is unnecessarily circulated through the column thereby merely consuming energy but not increasing the production of deriched natural gas leaving the process via line 55.
- Figure 4 shows a preferred embodiment according to the present invention, wherein the processes and apparatuses as illustrated in Figures 2 and 3 are combined. For a description of the details, reference is made to the above descriptions of Figures 1 , 2 , and 3 .
- Table I shows recommended lower and upper limits of temperatures and pressures of the streams through various lines in the process, as well as a typical value of temperature and pressure in a particular example of operation.
- Table I Line T-low (°C) T-up (°C) T (°C) P-low (bar) P-up (bar) P (bar) 1 -162 -120 -161 1.0 1.5 1.1 2 -162 -120 -161 5 50 33 7, 15, 17, 57 -140 -50 -81 5 50 33 20 -70 -20 -37 5 50 33 38 -10 150 90 2 45 29 40 -90 -10 -28 2 45 29 42, 48, 49 -60 -30 -49 5 50 33 55 -110 -162 -128 5 50 33 66 -40 0 -19 5 50 33 67 -110 -162 -140 20 140 70
- the molar fraction of vapour in line 7 was 66%, and in line 42 it was 69%.
- the molar fraction of vapour in line 20 was 75%. It has been predicted on the basis of mass-balance calculations that the apparatus and process of Figure 4 provide an efficient means for recovering natural gas liquid components from the liquefied natural gas feed stream in excess of 90%.
- the heat exchanger arrangements can comprise one heat exchanger, or a plurality of heat exchangers in parallel and/or in series.
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Description
- The present invention relates to a method and apparatus for deriching a stream of liquefied natural gas (LNG) by extracting a natural gas liquid from the stream of liquefied natural gas. The resulting stream of deriched liquefied natural gas can be in liquid and/or vapour phase for instance utilizing subsequent regasification.
- The term deriching is used in the present specification and claims as an opposite term for enriching, and is understood to include a meaning of removing hydrocarbon compounds higher than methane, i.e. "stripping" or "making leaner". The term natural gas liquid is understood to include hydrocarbon compounds higher than methane, including ethane, ethylene, propane, propylene, butane and isomeric variations thereof, and butylenes and isomeric variations thereof.
- In addition to methane, liquefied natural gas typically contains higher hydrocarbon compounds including ethane, propane, and various isomeric forms of butane. These additional compounds have higher heating values than methane. Different specifications of liquefied natural gas, in particular with regard to heating value, are demanded in various markets.
- In order to conform to pipeline specifications having a lower heating value, there can thus be a need for deriching a liquefied natural gas stream at a regasification facility before sending the regasified stream into the grid. One way of deriching is formed by recovery of natural gas liquids from the liquefied natural gas stream.
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US patent 6,604,380 discloses such a method for the recovery of natural gas liquids. In the disclosed method, a liquefied natural gas feed stream is split. With particular reference toFigure 2 of the mentioned US patent, one portion of the split stream is heated in a heat exchanger whereby it is partially vapourised and then fed to a feed separator. A natural gas liquid rich bottom stream is removed from the feed separator and routed to a second separation method including a stabilizer. The other portion of the split stream bypasses the heat exchanger and is fed at a very low temperature of around -157 °C (-250 °F) as an external reflux into the second separation method. The methane-rich overhead vapour streams are drawn from the feed separator and the stabilizer, and combined and directed through the heat exchanger where it is cooled against the one portion of the split feed stream. -
WO 2004/109180 discloses a method of processing LNG in a plant in which a heat source vaporizes pressurized LNG which is subsequently expanded to produce work in an open power cycle. - It has been found that the above-described methods are unnecessarily inefficient.
- It is an object of the present invention to minimize the above problem.
- It is a further object of the present invention to provide an alternative method for deriching a stream of liquefied natural gas.
- One or more of the above and other objects may be achieved according to the present invention by providing a method of deriching a stream of liquefied natural gas by extracting a natural gas liquid from the stream of liquefied natural gas, the method at least comprising the steps of:
- heating a feed stream containing the stream of liquefied natural gas in a first heat exchanger arrangement to form an intermediate feed stream;
- splitting the intermediate feed stream into at least a first portion and a second portion;
- passing the first portion to a distillation column and feeding it via a first feeding point;
- passing the second portion to a second heat exchanger arrangement wherein it is further heated, and then supplying it to the distillation column via a second feeding point;
- withdrawing a liquid stream containing the natural gas liquid from a lower portion of the distillation column;
- withdrawing an overhead vapour stream from an upper portion of the distillation column;
- passing the overhead vapour stream to the second heat exchanger arrangement where it is cooled against the second portion of the intermediate feed stream to form an intermediate deriched stream of which at least a portion is thereafter passed to the first heat exchanger arrangement and further cooled against the feed stream to form a product stream of deriched natural gas;
wherein during cooling of the overhead vapour stream in the second heat exchanger arrangement it is partially condensed to form an intermediate condensate, of which at least a portion is passed to the distillation column via a third feeding point, and an intermediate vapour which is passed to the first heat exchanger arrangement. - An advantage of the present invention is that it provides more flexibility in choosing the temperature profile in the distillation column, which facilitates efficient control of the method conditions in the distillation column.
- Further it has been found that the use of the intermediate deriched stream to generate a reflux stream improves the natural gas liquid recovery significantly. The overhead vapour stream from the distillation column is partially condensed during the cooling in the second heat exchanger arrangement and the intermediate deriched stream comprises an intermediate condensate which can be passed to the distillation column via the third feeding point, and an intermediate vapour which can be passed to the first heat exchanger arrangement.
- A further advantage is that the intermediate condensate is enriched in heavier components including natural gas liquids. Instead of submitting this condensate to the first heat exchanger arrangement it is re-submitted to the distillation column as an internal reflux. Hence the recovery of the natural gas liquid is significantly improved.
- By choosing the relative cooling in the first and second heat exchanger arrangements, an intermediate temperature can be chosen in the intermediate deriched stream that allows to tailor the composition of the condensate.
- Another advantage of the invention is that the heating and cooling upstream respectively downstream of the distillation column is performed in at least two stages. The resulting intermediate streams between the at least two stages are thus available for use in the method in addition to the fully heated respectively cooled streams.
- One way of utilizing the intermediate feed stream is as an external reflux having a temperature that is lower than that of the portion being fed to the distillation column via the second feeding point but not as low as that of the original feed stream.
- It has been found that an external reflux stream having a temperature as low as of liquefied natural gas (approximately of around -157 °C, or less than -140 °C) is not generally required for an efficient separation of natural gas liquid components from liquefied natural gas. An advantage of the invention is that the temperature of the external reflux can be chosen higher than the temperature of the feed stream, for instance higher than -140 °C. As a consequence, equipment such as the distillation column or a reboiler (if provided), can be smaller sized, and less power needs to be dissipated in a reboiler. The high-quality cold in the feed stream thus becomes available fully for recondensating the deriched natural gas.
- Depending on the amount of heating applied in the first heat exchanger arrangement and the pressure of the feed stream, the intermediate feed stream can either be fully liquid or partly vapourized.
- Where the heating of the feed stream in the first heat exchanger arrangement comprises partly vapourizing the feed stream whereby the intermediate feed stream comprises a mixture of liquid intermediate feed fraction and vaporous intermediate feed fraction, it is advantageous to split at least the liquid intermediate feed fraction into at least the first and second portions. The vaporous intermediate feed fraction, because of it relatively low temperature compared to the temperature after the second heating, is already relatively lean from natural gas liquids and does not have to be further distilled. It can be mixed in with a final product stream.
- In a further aspect the present invention provides a deriched natural gas stream obtained by the method according to the present invention as well as an apparatus suitable for performing the method according to the present invention.
- Preferred embodiments for the apparatus are derivable from preferred embodiments of the method and/or from the detailed description of embodiments set out below.
- The above-described features and other features of the present invention will be further illustrated by way of example and with reference to the accompanying nonlimiting drawing.
- In the accompanying drawing:
-
Figures 1 and2 schematically show process flow schemes and apparatus not containing all features of the present invention but incorporated for illustration purposes; -
Figure 3 schematically shows a process flow scheme and apparatus according to the present invention; and -
Figure 4 schematically shows a preferred embodiment of the present invention wherein the process scheme ofFigure 2 is combined with the process scheme ofFigure 3 . - For the purposes of this description, like reference numerals correspond to like parts. Reference numerals corresponding to lines are also used to refer to the respective streams carried in these lines.
-
Figure 1 schematically shows an apparatus for deriching a stream of liquefied natural gas by extracting a natural gas liquid from the stream of liquefied natural gas. A feed line 1 is connectable to a source of the liquefied natural gas. Anoptional pump 3 is provided in the feed line 1, of which the high-pressure outlet is in fluid communication with a firstheat exchanger arrangement 5 vialine 2. - An intermediate feed line 7 fluidly connects a
first outlet 6 of the firstheat exchanger arrangement 5 with adistributor 14. Thedistributor 14 has two outlets connected tolines distributor 14 may have more than two outlets.Line 17 connects to adistillation column 21 via an optionalfirst control valve 23 and afirst feeding point 25 provided in an upper part of thedistillation column 21. The other line,line 19, also connects to thedistillation column 21 but via a secondheat exchanger arrangement 26,line 20, which can be optionally provided with asecond control valve 27, and asecond feeding point 29. This way, thefirst outlet 6 of the firstheat exchanger arrangement 5 is in fluid communication with the secondheat exchanger arrangement 26.Line 17 bypasses the secondheat exchanger arrangement 26. Thesecond feeding point 29 of thedistillation column 21 is preferably located gravitationally lower than thefirst feeding point 25. - The
distillation column 21 has a lower portion provided with adischarge opening 31 for withdrawing aliquid stream 35 from thedistillation column 21. Anoptional reboiler 33 may be provided inline 35 connecting to thedischarge opening 31. Areboil return line 37 feeds back from thereboiler 33 into the lower portion of thedistillation column 21. Theoptional reboiler 33 may be integrated with thedistillation column 21 instead of the shown external arrangement. Aline 38 connects to line 35 or to theoptional reboiler 33 for discharging the natural gas liquid. - The
distillation column 21 also has an upper portion provided with anoverhead vapour outlet 39. Theoverhead vapour outlet 39 is in fluid communication with the firstheat exchanger arrangement 5 via the secondheat exchanger arrangement 26.Line 40 extends between theoverhead vapour outlet 39 and the secondheat exchanger arrangement 26, and is connected to line 48 that extends between the secondheat exchanger arrangement 26 and the firstheat exchanger arrangement 5, and is connected to line 55 downstream of the firstheat exchanger arrangement 5 via asecond outlet 41 of the firstheat exchanger arrangement 5. - An
optional pump 65 can be included inline 55, which discharges intoline 67, for increasing the pressure to produce a deriched liquefied natural gas stream at a pressure according to a local specification.Line 67 can be connected to any type of re-gasification system, including systems known from an article "Innovative gas processing with various LNG sources" by Joseph Cho et al, as published in LNG Journal January/February 2005 pp 23-27. - The above-described apparatus is capable of deriching a stream of liquefied natural gas by extracting a natural gas liquid from the stream of liquefied natural gas. An
optional bypass line 59 can be provided to fluidly connect line 1 or the high-pressure outlet ofpump 3 upstream of the firstheat exchanger arrangement 5 withline 55 downstream of the firstheat exchanger arrangement 5. Theoptional bypass line 59 can be provided with acontrol valve 61. With thebypass line 59 the deriching arrangement can be bypassed and the extraction of the natural gas liquid avoided. - In operation, the apparatus of
Figure 1 works as follows. A feed stream containing the stream of liquefied natural gas is supplied via feed line 1 and heated in the firstheat exchanger arrangement 5 against an intermediate deriched stream inline 48 to form an intermediate feed stream 7. Before supplying the feed stream 1 to theheat exchanger arrangement 5 it can be pressurized or its pressure increased using theoptional pump 3. This is particularly useful when the liquefied natural gas is supplied at atmospheric pressure or near atmospheric pressure. - The intermediate feed stream 7 is split in the
distributor 14 into at least afirst portion 17 and asecond portion 19. The first portion 7 is passed to thedistillation column 21 and fed into it via thefirst feeding point 25. Pressure and temperature can be controlled utilizingcontrol valve 23. - The
second portion 19 of the intermediate feed stream 7 is passed to the secondheat exchanger arrangement 26 wherein it is further heated, against an overhead stream inline 40. The resulting further heated stream is then supplied to thedistillation column 21 vialine 20 and thesecond feeding point 29. Pressure can be controlled employingcontrol valve 27. - During the further heating in the second
heat exchanger arrangement 26 thesecond portion 19 of the intermediate feed stream 7 is at least partially vapourised. It is generally recommended to vapourize to a molar fraction of at least 60%. - As the temperature of the
first portion 17 can be lower than that of thesecond portion 19, thefirst portion 17 acts as an external reflux stream in the distillation process. It helps scrubbing the natural gas liquid from vapour generated from thesecond portion 19 as well as inoptional reboiler 33. The scrubbing is facilitated by the preference that thefirst feeding point 25 is located gravitationally higher than thesecond feeding point 29. - A liquid stream containing the natural gas liquid is then withdrawn from a lower portion of the
distillation column 21 via thedischarge opening 31 intoline 35. Optionally, the liquid stream is heated and partly fed back vialine 37 to the lower portion of thedistillation column 21 to allow some vapour to form containing relatively lighter molecules. The remainder is discharged as natural gas liquid intoline 38. - On the other side of the
distillation column 21, anoverhead vapour stream 40 is withdrawn from an upper portion of thedistillation column 21. Theoverhead vapour stream 40 is a deriched stream containing mainly methane and sometimes also other components such as for instance ethane and a remainder of propane. - The
overhead vapour stream 40 is passed to the secondheat exchanger arrangement 26 where it is cooled against the intermediate feed stream to form an intermediatederiched stream 48 of which at least a portion is thereafter passed to the firstheat exchanger arrangement 5 and further cooled against the feed stream 1 to form aproduct stream 55 of deriched natural gas. Theproduct stream 55 can be fully re-condensed. - Optionally, the
product stream 55 is combined with a bypass stream drawn from thefeed stream 2 vialine 59. The pressure of the product stream inline 55 can then be raised to a desired pressure level by means of theoptional pump 65, which is generally more energy efficient as the stream inline 55 generally tends to be fully condensed. The product stream is discharged throughline 67 after which it can be further processed (not shown), for instance including re-gasification by heating it to convert it into a gaseous stream. Several possible re-gasification methods are described in the article from the LNG Journal January/February 2005 already introduced. - Although not strictly required, an optional compressor (not shown) can be provided in
line 40 to be able to generate a comfort margin in the pressure to ensure that the product stream inline 55 leaving the firstheat exchanger arrangement 5 atoutlet 41 is not only fully re-condensed but also sub-cooled to a sufficient degree. This is of less importance when a substantial amount of thefeed stream 2 is allowed to bypass vialine 59, as in that case the product stream leaving the firstheat exchanger arrangement 5 is subjected to direct heat exchange. - An advantage of having two
heat exchanger arrangements Figure 1 , a portion (first portion 17) of the intermediate stream 7 is utilized as external reflux having a temperature that is lower than that of the portion (second portion 19) being fed to thedistillation column 21 via thesecond feeding point 29 but not as low as the feed stream 1. By proper balance of the heating capacity in the firstheat exchanger arrangement 5 versus the secondheat exchanger arrangement 26, increased temperature control is achieved over thereflux stream 17 and the furtherheated feed stream 20, as compared to what is possible in the process as described inUS patent 6,604,380 . This increased flexibility enables efficient control of the process conditions in thedistillation column 21, to achieve desired separation betweenoverhead stream 40 andbottom stream 38 of a selected natural gas liquid component. -
Figure 2 is based on the process as shown and explained above with reference toFigure 1 and shows a gas/liquid separator 9 (referred to in the claims as "second gas/liquid separator") that is arranged in the connection between thefirst outlet 6 of the firstheat exchanger arrangement 5 and thedistributor 14. The gas/liquid separator is here provided in the form of afeed separation vessel 9. Thefirst outlet 6 of the firstheat exchanger arrangement 5 is connected with thefeed separation vessel 9. Thefeed separation vessel 9 has abottom outlet 11 and anoverhead outlet 13. Thebottom outlet 11 is connected to thedistributor 14 vialine 15. Theoverhead outlet 13 is fluidly connected toline 48 vialine 57 upstream of the firstheat exchanger arrangement 5. - The process of
Figure 2 works as follows. As the feed stream is heated in the firstheat exchanger arrangement 5, it can be partially vapourised. The vapour is drawn from theoverhead outlet 13 and combined with the intermediate deriched stream inline 48. The combined streams are then further cooled and recondensed together in the firstheat exchanger arrangement 5 against thefeed stream 2. - As the temperature is still relatively low, the vapour will contain predominantly the leaner components such as methane. The components with higher heating values, such as propane will still be essentially fully in the liquid phase together with ethane and methane. The vapourised fraction does not have to be further distilled and can be mixed in with the distilled stream in
line 48 to be recondensed in the firstheat exchanger arrangement 5. - Typically, the molar fraction of vapour can be between 1 and 90%. The higher the molar fraction of vapour, the lower the mass load is on the extraction apparatus downstream. In this respect, for a typical liquefied natural gas composition it is preferred that at least 50 mol.% is in vapour phase. On the other hand, the higher the molar fraction of vapour the lower the recovery of natural gas liquids since the mass separation in the vessel is not as high as in the
distillation column 21. In this respect, it is preferred that the molar fraction of vapour is not more than 80%. - The liquid that is drawn from the
bottom outlet 11 of theseparator 9 is led to thedistributor 14, where part of it is sent to thedistillation 21 column vialine 17 as an external reflux thereby bypassing the secondheat exchanger arrangement 26. - An advantage of this process is that the external reflux is fully liquid so that it can be fully effective as scrubbing medium. The temperature of the external reflux is lower than that of the portion being fed to the distillation column via the
second feeding point 29, but not as low as that of the original feed stream 1. The temperature can be controlled by choosing the amount of heat exchange in thefirst heat exchanger 5, optionally in co-dependence of controlling the amount of expansion incontrol valve 23. - An advantage of the
optional control valves distillation column 21 is operated at a lower pressure than thefeed separator 9, which improves the separation efficiency of natural gas liquid components in thecolumn 21. - Still referring to
Figure 2 , an optionaloverhead compressor 63 can be provided between theoverhead vapour outlet 39 of thedistillation column 21 and the secondheat exchanger arrangement 26. Herewith the optional pressure drop overvalves line 48 can be brought to the pressure level as set by the feed stream in line 7. - It is preferred to arrange the
compressor 63 upstream of the secondheat exchanger arrangement 26, because theoverhead stream 40 is by virtue of thedistillation column 21 always fully vaporous whereas downstream of the secondheat exchanger arrangement 26 the product stream can be of a multi-phase nature. - Alternatively, an expansion device can be provided in
line 57, such as a Joule-Thompson valve (not shown) to lower the pressure inline 57 to that inline 48. Now having the process schemes ofFigures 1 and2 explained,Figure 3 shows an embodiment according to the present invention which is based on the embodiment as shown and explained above with reference toFigure 1 , wherein an internal reflux system is provided in theconnection line 48 between the distillation column'soverhead vapour outlet 39 and the firstheat exchanger arrangement 5. The reflux system here shown comprises a gas/liquid separator (referred to in the claims as "first gas/liquid separator") here provided in the form of areflux separation vessel 43. Thereflux separation vessel 43 is arranged downstream of the secondheat exchanger arrangement 26 inline 48 and connected to the secondheat exchanger arrangement 26 vialine 42. Theseparator 43 has abottom outlet 45 and anoverhead outlet 47. Thebottom outlet 45 is connected to thedistillation column 21 vialine 49 and athird feeding point 51 to provide a reflux stream. Anoptional control valve 53 can be provided inline 49. Thethird feeding point 51 is best arranged gravitationally higher than thesecond feeding point 29, as the temperature of thereflux stream 49 is generally lower than that of the furtherheated feed stream 20, and gravitationally lower than thefirst feeding point 25. - The
overhead outlet 47 of thereflux separation vessel 43 is fluidly connected with the firstheat exchanger arrangement 5 vialine 48. - In operation, where a methane, ethane and propane containing feed stream of liquefied natural gas is fed into the process, a majority of the propane is recovered in
distillation column 21. The selective recovery of propane can be increased by allowing the residual propane components that may be present in theoverhead vapour stream 40 to condense in the secondheat exchanger arrangement 26. Theintermediate condensate 49 is drawn from thereflux separation vessel 43 and fed back into thedistillation column 21 as a cold reflux stream. The propane has another chance of leaving the process viaoutlet 31. - Since the second
heat exchanger arrangement 26 brings the intermediate deriched stream only to an intermediate temperature, the mass selectivity of the reflux stream can be tailored by choice of that temperature, and optionally also the pressure drop inoptional valve 53. Herewith it can be avoided that methane or ethane is unnecessarily circulated through the column thereby merely consuming energy but not increasing the production of deriched natural gas leaving the process vialine 55. - While comparing the process scheme of
Figure 1 (not containing all the features of the present invention) and the process scheme ofFigure 3 (according to the present invention), calculations predicting the recovery of propane have shown that the process scheme ofFigure 1 under given process conditions resulted in a propane recovery of 69%, whilst under the same given process conditions the process scheme ofFigure 3 resulted in a propane recovery of 90%. - Typically, the molar fraction of vapour can be between 50 and 95%. The higher the molar fraction of vapour, the better the lesser the quantity of leaner components circulated in the reflux loop. In this respect, it is preferred that at least 60 mol.% is in vapour phase. On the other hand, the higher the molar fraction of vapour the lower the recovery of natural gas liquids since less of the natural gas liquid components are recondensed and fed back into the
distillation column 21. In this respect, for most typical liquefied natural gas compositions it is preferred that the molar fraction of vapour is not more than 90%. -
Figure 4 shows a preferred embodiment according to the present invention, wherein the processes and apparatuses as illustrated inFigures 2 and3 are combined. For a description of the details, reference is made to the above descriptions ofFigures 1 ,2 , and3 . - The following Table I shows recommended lower and upper limits of temperatures and pressures of the streams through various lines in the process, as well as a typical value of temperature and pressure in a particular example of operation.
Table I Line T-low (°C) T-up (°C) T (°C) P-low (bar) P-up (bar) P (bar) 1 -162 -120 -161 1.0 1.5 1.1 2 -162 -120 -161 5 50 33 7, 15, 17, 57 -140 -50 -81 5 50 33 20 -70 -20 -37 5 50 33 38 -10 150 90 2 45 29 40 -90 -10 -28 2 45 29 42, 48, 49 -60 -30 -49 5 50 33 55 -110 -162 -128 5 50 33 66 -40 0 -19 5 50 33 67 -110 -162 -140 20 140 70 - In the example to which Table I relates, the molar fraction of vapour in line 7 was 66%, and in
line 42 it was 69%. The molar fraction of vapour inline 20 was 75%. It has been predicted on the basis of mass-balance calculations that the apparatus and process ofFigure 4 provide an efficient means for recovering natural gas liquid components from the liquefied natural gas feed stream in excess of 90%. - In the context of the present specification, the heat exchanger arrangements can comprise one heat exchanger, or a plurality of heat exchangers in parallel and/or in series.
Claims (15)
- Method of deriching a stream of liquefied natural gas (1) by extracting a natural gas liquid (35) from the stream of liquefied natural gas, the method at least comprising the steps of:- heating a feed stream (1) containing the stream of liquefied natural gas in a first heat exchanger arrangement (5) to form an intermediate feed stream (7);- splitting the intermediate feed stream (7) into at least a first portion (17) and a second portion (19);- passing the first portion (17) to a distillation column (21) and feeding it (17) via a first feeding point (25);- passing the second portion (19) to a second heat exchanger arrangement (26) wherein it is further heated, and then supplying it (20) to the distillation column (21) via a second feeding point (29);- withdrawing a liquid stream (35) containing the natural gas liquid from a lower portion of the distillation column (21);- withdrawing an overhead vapour stream (40) from an upper portion of the distillation column (21);- passing the overhead vapour stream (40) to the second heat exchanger arrangement (26) where it is cooled against the second portion (19) of the intermediate feed stream (7) to form an intermediate deriched stream (48) of which at least a portion is thereafter passed to the first heat exchanger arrangement (5) and further cooled against the feed stream (1) to form a product stream of deriched natural gas (55); characterized in that during cooling of the overhead vapour stream (40) in the second heat exchanger arrangement (26) it is partially condensed to form an intermediate condensate, of which at least a portion (49) is passed to the distillation column (21) via a third feeding point (51), and an intermediate vapour which is passed to the first heat exchanger arrangement (5).
- Method of claim 1, wherein said heating of the feed stream in the first heat exchanger arrangement (5) comprises partly vapourizing the feed stream whereby the intermediate feed stream (7) comprises a mixture of liquid intermediate feed fraction and vaporous intermediate feed fraction; and wherein at least the liquid intermediate feed fraction (15) is split into at least the first and second portions (17,19).
- Method of claim 2, wherein the mixture is passed to a feed separating vessel (9) from which the liquid intermediate feed fraction (15) and the vaporous intermediate feed fraction (57) are respectively drawn before splitting it into the at least first and second portions (17,19).
- Method of one or more of the preceding claims, wherein the second feeding point (29) is located gravitationally lower than the first feeding point (25).
- Method of one or more of the preceding claims, wherein the third feeding point (51) is gravitationally lower than the first feeding point (25).
- Method of one or more of the preceding claims, wherein the third feeding point (51) is gravitationally higher than the second feeding point (29).
- Method of one or more of the preceding claims, wherein the overhead vapour stream (40) is compressed before passing it to the second heat exchanger arrangement (26).
- Method of one or more of the preceding claims, wherein the product stream of de-riched natural gas is subsequently re-gasified.
- Apparatus for deriching a stream of liquefied natural gas (1) by extracting a natural gas liquid (35) from the stream of liquefied natural gas, the apparatus at least comprising:- a first heat exchanger arrangement (5) arranged to receive a feed stream (1) containing the stream of liquefied natural gas and provided with an outlet (6) to discharge an intermediate feed stream (7);- a second heat exchanger arrangement (26) in fluid communication with the outlet (6) of the first heat exchanger arrangement (5);- a distillation column (21) having at least first, second and third feeding points (25,29,51), a lower portion provided with a discharge opening (31) for withdrawing a liquid stream (35) containing the natural gas liquid, and an upper portion provided with an overhead vapour outlet (39) in fluid communication with the first heat exchanger arrangement (5) via at least the second heat exchanger arrangement (26); and- a distributor (14) connected to the outlet (6) of the first heat exchanger arrangement (5), the distributor (14) having a first outlet (6) being connected to the first feeding point (25) of the distillation column (21), and a second outlet being connected to the second feeding point (29) of the distillation column (21) via the second heat exchanger arrangement (26); characterized in that the apparatus further comprises:- a first gas/liquid separator (43) downstream of the overhead vapour outlet (39) and between the second heat exchanger arrangement (26) and first heat exchanger arrangement (5), the first separator (43) having an outlet (45) connected to the third feeding point (51) of the distillation column (21) and an outlet (47) in fluid communication with the first heat exchanger arrangement (5).
- Apparatus according to claim 9, further comprising a second gas/liquid separator (9) having an inlet connected to the outlet (6) of the first heat exchanger (5) and a bottom outlet (11) connected to the distributor (14).
- Apparatus according to claim 9 or 10, further comprising a compressor (63) between the outlet (39) of the distillation column (21) and the second heat exchanger arrangement (26).
- Method of extracting a natural gas liquid (35) by the method of claim 1.
- Method of claim 12, wherein said heating of the feed stream in the first heat exchanger arrangement (5) comprises partly vapourizing the feed stream whereby the intermediate feed stream (7) comprises a mixture of liquid intermediate feed fraction and vaporous intermediate feed fraction; and wherein at least the liquid intermediate feed fraction (15) is split into at least the first and second portions (17, 19) and
wherein the mixture is passed to a feed separating vessel (9) from which the liquid intermediate feed fraction (15) and the vaporous intermediate feed fraction (57) are respectively drawn before splitting it into the at least first and second portions (17,19). - Method of one or more of claims 12-13, wherein the second feeding point (29) is located gravitationally lower than the first feeding point (25) and/or wherein the third feeding point (51) is gravitationally lower than the first feeding point (25) and/or wherein the third feeding point (51) is gravitationally higher than the second feeding point (29).
- Method of one or more of the claims 12-14, wherein the overhead vapour stream (40) is compressed before passing it to the second heat exchanger arrangement (26).
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP06708800.5A EP1861671B1 (en) | 2005-03-22 | 2006-03-20 | Process and apparatus for extracting natural gas liquids from a stream of liquefied natural gas |
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP05102252 | 2005-03-22 | ||
EP06708800.5A EP1861671B1 (en) | 2005-03-22 | 2006-03-20 | Process and apparatus for extracting natural gas liquids from a stream of liquefied natural gas |
PCT/EP2006/060867 WO2006100218A1 (en) | 2005-03-22 | 2006-03-20 | Method and apparatus for deriching a stream of liquefied natural gas |
Publications (2)
Publication Number | Publication Date |
---|---|
EP1861671A1 EP1861671A1 (en) | 2007-12-05 |
EP1861671B1 true EP1861671B1 (en) | 2015-12-23 |
Family
ID=34939026
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP06708800.5A Active EP1861671B1 (en) | 2005-03-22 | 2006-03-20 | Process and apparatus for extracting natural gas liquids from a stream of liquefied natural gas |
Country Status (6)
Country | Link |
---|---|
US (1) | US20090056371A1 (en) |
EP (1) | EP1861671B1 (en) |
JP (1) | JP5411496B2 (en) |
ES (1) | ES2561808T3 (en) |
RU (1) | RU2386091C2 (en) |
WO (1) | WO2006100218A1 (en) |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EA010743B1 (en) * | 2004-06-30 | 2008-10-30 | Флуор Текнолоджиз Корпорейшн | Plant (embodiments) and method of lng regasification |
US20080148771A1 (en) * | 2006-12-21 | 2008-06-26 | Chevron U.S.A. Inc. | Process and apparatus for reducing the heating value of liquefied natural gas |
EP2416865B1 (en) * | 2009-04-07 | 2013-10-02 | Twister B.V. | Separation system comprising a swirl valve |
EP3604222A1 (en) * | 2018-07-30 | 2020-02-05 | Evonik Operations GmbH | Process for the purification of hydrogen cyanide |
Family Cites Families (15)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
BE579774A (en) * | 1958-06-23 | |||
FR1501013A (en) * | 1966-09-13 | 1967-11-10 | Air Liquide | Process for the production of a gas rich in methane under high pressure from liquid natural gas under low pressure |
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 |
US5114451A (en) * | 1990-03-12 | 1992-05-19 | Elcor Corporation | Liquefied natural gas processing |
US6510706B2 (en) * | 2000-05-31 | 2003-01-28 | Exxonmobil Upstream Research Company | Process for NGL recovery from pressurized liquid natural gas |
US7069743B2 (en) * | 2002-02-20 | 2006-07-04 | Eric Prim | System and method for recovery of C2+ hydrocarbons contained in liquefied natural gas |
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 |
US6964181B1 (en) * | 2002-08-28 | 2005-11-15 | Abb Lummus Global Inc. | Optimized heating value in natural gas liquids recovery scheme |
WO2004109206A1 (en) * | 2003-06-05 | 2004-12-16 | Fluor Corporation | Liquefied natural gas regasification configuration and method |
US6907752B2 (en) * | 2003-07-07 | 2005-06-21 | Howe-Baker Engineers, Ltd. | Cryogenic liquid natural gas recovery process |
US7155931B2 (en) * | 2003-09-30 | 2007-01-02 | Ortloff Engineers, Ltd. | Liquefied natural gas processing |
BRPI0512744A (en) * | 2004-07-01 | 2008-04-08 | Ortloff Engineers Ltd | liquefied natural gas processing |
US20060130520A1 (en) * | 2004-12-17 | 2006-06-22 | Abb Lummus Global Inc. | Method for recovery of natural gas liquids for liquefied natural gas |
-
2006
- 2006-03-20 JP JP2008502388A patent/JP5411496B2/en not_active Expired - Fee Related
- 2006-03-20 ES ES06708800.5T patent/ES2561808T3/en active Active
- 2006-03-20 RU RU2007138916/06A patent/RU2386091C2/en not_active IP Right Cessation
- 2006-03-20 EP EP06708800.5A patent/EP1861671B1/en active Active
- 2006-03-20 WO PCT/EP2006/060867 patent/WO2006100218A1/en active Application Filing
- 2006-03-20 US US11/886,801 patent/US20090056371A1/en not_active Abandoned
Also Published As
Publication number | Publication date |
---|---|
JP2008535961A (en) | 2008-09-04 |
RU2007138916A (en) | 2009-04-27 |
JP5411496B2 (en) | 2014-02-12 |
RU2386091C2 (en) | 2010-04-10 |
ES2561808T3 (en) | 2016-03-01 |
WO2006100218A1 (en) | 2006-09-28 |
US20090056371A1 (en) | 2009-03-05 |
EP1861671A1 (en) | 2007-12-05 |
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