WO2019122656A1 - Method for liquefying a natural gas stream containing nitrogen - Google Patents
Method for liquefying a natural gas stream containing nitrogen Download PDFInfo
- Publication number
- WO2019122656A1 WO2019122656A1 PCT/FR2018/053334 FR2018053334W WO2019122656A1 WO 2019122656 A1 WO2019122656 A1 WO 2019122656A1 FR 2018053334 W FR2018053334 W FR 2018053334W WO 2019122656 A1 WO2019122656 A1 WO 2019122656A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- stream
- natural gas
- cooled
- gas
- nitrogen
- Prior art date
Links
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 104
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 64
- 238000000034 method Methods 0.000 title claims abstract description 45
- 239000003345 natural gas Substances 0.000 title claims abstract description 44
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 32
- 239000007789 gas Substances 0.000 claims abstract description 29
- 239000007788 liquid Substances 0.000 claims abstract description 27
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 26
- 238000001816 cooling Methods 0.000 claims abstract description 13
- 239000000203 mixture Substances 0.000 claims description 55
- 239000003507 refrigerant Substances 0.000 claims description 40
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 22
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 11
- 239000001294 propane Substances 0.000 claims description 11
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 7
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 6
- 239000001273 butane Substances 0.000 claims description 5
- FGUUSXIOTUKUDN-IBGZPJMESA-N C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 Chemical compound C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 FGUUSXIOTUKUDN-IBGZPJMESA-N 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 238000010992 reflux Methods 0.000 claims description 3
- GNFTZDOKVXKIBK-UHFFFAOYSA-N 3-(2-methoxyethoxy)benzohydrazide Chemical compound COCCOC1=CC=CC(C(=O)NN)=C1 GNFTZDOKVXKIBK-UHFFFAOYSA-N 0.000 claims description 2
- 239000012071 phase Substances 0.000 description 10
- 229930195733 hydrocarbon Natural products 0.000 description 6
- 150000002430 hydrocarbons Chemical class 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 238000005057 refrigeration Methods 0.000 description 3
- 239000002151 riboflavin Substances 0.000 description 3
- 125000004432 carbon atom Chemical group C* 0.000 description 2
- 239000012809 cooling fluid Substances 0.000 description 2
- 239000008246 gaseous mixture Substances 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000001282 iso-butane Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
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- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0219—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. using a deep flash recycle loop
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0235—Heat exchange integration
- F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant 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
- F25J3/0204—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
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- 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
- 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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- 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
- F25J3/0257—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 nitrogen
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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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- 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
- F25J2200/30—Processes or apparatus using separation by rectification using a side column in a single pressure column system
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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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
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- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/04—Mixing or blending of fluids with the feed stream
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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
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- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising loop
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- 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
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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
- 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 the field of liquefaction of natural gas.
- the liquefaction of natural gas consists of condensing the natural gas and subcooling it to a temperature sufficiently low that it can remain liquid at atmospheric pressure. It is then transported in LNG carriers.
- US 6,105,389 proposes a liquefaction process comprising two refrigerant mixtures flowing in two closed and independent circuits. Each of the circuits operates through a compressor communicating to the refrigerant mixture the power required to cool the natural gas. Each compressor is driven by a gas turbine which is selected from the standard ranges proposed in the trade. However, the power of currently available gas turbines is limited.
- US 6,763,680 discloses a liquefaction process in which the pressurized liquefied natural gas is expanded in at least two stages so as to obtain at least two gaseous fractions.
- the pressurized liquefied natural gas is cooled by reboiling a denitrogenation column.
- a first liquid fraction depleted of nitrogen and a first gas fraction enriched in nitrogen are obtained.
- This liquid fraction is expanded again to give a liquefied natural gas low in nitrogen and a second gaseous fraction. At least one gaseous fraction is re-compressed and then mixed with the natural gas before condensation.
- a liquefaction process for natural gas as described in the prior art is not suitable when said natural gas to be liquefied comprises too high a nitrogen level, that is to say greater than 4%.
- the present invention proposes to improve the process disclosed by US 6,763,680.
- One of the objects of the present invention is to allow a reduction in the investment cost required for a liquefaction plant.
- Another object of the The present invention is to achieve, under better conditions, a separation of nitrogen that can be contained in the gas.
- the inventors of the present invention have developed a solution for producing, from a fixed amount of natural gas, liquefied natural gas low in nitrogen whose flow is increased and while minimizing the costs required for deployment. of this type of process.
- the present invention relates to a method of liquefying a natural gas feed stream comprising the following steps:
- step b) characterized in that at least a portion of the liquid stream from step b) is used during step c) to cool the vapor stream from step b) in said heat exchanger.
- the subject of the invention is also:
- step a) said natural gas supply stream is cooled and a second refrigerant mixture by indirect heat exchange with at least a first refrigerant mixture for cooling. obtain a cooled natural gas and a cooled second cooling mixture, then the cooled natural gas is condensed and cooled by indirect heat exchange with the cooled second cooling mixture and with at least a portion of the gas stream obtained in step d) for obtain a liquefied natural gas.
- step b) the stream from step a) is cooled in a means for reboiling said denitrogenation column to the temperature T2.
- a process as defined above characterized in that the stream cooled to the temperature T2 is expanded in an expansion means prior to introduction into the denitrogenation column.
- a process as defined above characterized in that at least a portion of the liquid stream from step d) is used as reflux at the top of the denitrogenation column.
- a method as defined above characterized in that it comprises the following steps:
- T1 is between - 140 ° C and -120 ° C.
- a process as defined above characterized in that P2 is between 3 bar abs and 10 bar abs, P1 is between 4 MPa and 7 MPa.
- step b) the mixture of natural gas and the second refrigerant mixture are cooled to a temperature between -70 ° C and -35 ° C by heat exchange with the first refrigerant mixture.
- the method according to the invention makes it possible to substantially increase the production capacity by adding a limited number of additional equipment.
- the method according to the invention is particularly advantageous when each of the refrigeration circuits uses a refrigerant mixture which is completely condensed, expanded and vaporized.
- feed stream refers to any composition containing hydrocarbons including at least methane.
- the heat exchanger may be any heat exchanger, unit or other arrangement adapted to allow the passage of a number of flows, and thus allow a direct or indirect heat exchange between one or more lines of refrigerant, and a or multiple feed streams.
- a natural gas feed stream 1 is introduced into a heat exchange unit E1 at a temperature T1.
- the feed stream 1 may contain methane, ethane, propane, hydrocarbons having at least four carbon atoms. This stream may contain traces of contaminants eg H2O 0-1 ppm, H2S 4 ppm, CO2 50 ppm.
- the natural gas feed stream comprises strictly more than 1 mol% of nitrogen, but the specifications impose a maximum content of 1 mol% nitrogen in the LNG.
- the unit E1 can contain several heat exchangers (2, 3, 1 12).
- the stream 1 natural gas arrives via the pipe 51 for example at a pressure of between 4 MPa and 7 MPa and at a temperature between 0 ° C and 60 ° C.
- the natural gas flowing in the duct 51 is combined with the gas 50 to form a mixture of natural gas circulating in the duct 51.
- the gas flowing in the duct 51, a first refrigerant mixture 201 and a second refrigerant mixture 109 enter the exchanger E1 to circulate in parallel directions and co-current.
- the natural gas exits the exchanger E1 through line 4, for example at a temperature between -35 ° C and -70 ° C.
- the second refrigerant mixture exits completely condensed from the exchanger E1 through the duct 100, for example at a temperature of between -35 ° C. and -70 ° C.
- the exchanger E1 three fractions (202, 212, 222) of the first refrigerant mixture in the liquid phase are successively withdrawn.
- the fractions are expanded (207, 217 and 227) through the expansion valves 21 1, 221 and 231 at three different pressure levels, and then vaporized in the exchanger E 1 by heat exchange with the natural gas stream circulating in the conduit. 51, the second refrigerant mixture and a portion of the first refrigerant mixture.
- the three vaporized fractions (208, 218, 228) are sent to different stages (257, 253, 250) of the compressor K1.
- the vaporized fractions are compressed in the compressor K1 and then condensed in the condenser E101 by heat exchange with an external cooling fluid, for example water or air.
- the first refrigerant mixture 201 from the condenser E101 is sent into the exchanger E1.
- the pressure of the first refrigerant mixture at the outlet of the compressor K1 may be between 2 MPa and 6 MPa.
- the temperature of the first refrigerant mixture at the outlet of the condenser E101 can be between 10 ° C. and 55 ° C.
- the first refrigerant mixture may be formed by a mixture of hydrocarbons such as a mixture of ethane and propane, but may also contain methane, butane and / or pentane.
- the proportions in molar fraction (%) of the components of the first refrigerant mixture may be:
- the natural gas flowing in the duct 4 can be fractionated, that is to say that a portion of the hydrocarbons containing at least two carbon atoms is separated from the natural gas, using a device known from the state of the art.
- the fractionated natural gas is sent into an E2 heat exchanger.
- the C2 + hydrocarbons collected are sent to fractionation columns comprising a deethanizer.
- the light fraction collected at the top of the deethanizer can be mixed with the natural gas circulating in the conduit 4.
- the liquid fraction collected at the bottom of the deethanizer is sent to a depropanizer.
- the gas flowing in the duct 4 and the second refrigerant mixture flowing in the duct 100 enter the exchanger E2 to circulate in parallel directions and co-current.
- the second refrigerant mixture leaving the exchanger E2 through the conduit 101 is expanded by the expansion member T3.
- the expansion member T3 may be a turbine, a valve or a combination of a turbine and a valve.
- the second refrigerated mixture expanded from the turbine T3 is sent through the conduit 102 in the exchanger E2 to be vaporized by countercurrently cooling the natural gas and the second refrigerant mixture.
- the second vaporized refrigerant mixture 103 is compressed by the compressor K2 and then cooled in the indirect heat exchanger C2 by heat exchange with an external cooling fluid, for example water or water. 'air.
- the second refrigerant mixture 109 from the exchanger C2 is sent into the exchanger.
- the pressure of the second refrigerant mixture at the outlet of the compressor K2 may be between 2 MPa and 8 MPa.
- the temperature of the second refrigerant mixture at the outlet of exchanger C2 may be between 10 ° C. and 55 ° C.
- the second refrigerant mixture is not split into separate fractions, but, to optimize the approach in the exchanger E2, the second refrigerant mixture can also be used. be separated into two or three fractions, each fraction being expanded to a different pressure level and then sent to different stages of the compressor K2.
- the second refrigerant mixture is formed for example by a mixture of hydrocarbons and nitrogen such as a mixture of methane, ethane and nitrogen but may also contain propane and / or butane.
- the proportions in mole fraction (%) of the components of the second refrigerant mixture may be:
- the natural gas comes out of the heat exchanger E2 through line 10 at a temperature which is preferably at least 10 ° C. higher than the bubble temperature of the liquefied natural gas produced at atmospheric pressure (bubble temperature means the temperature at which the first vapor bubbles are formed in a liquid natural gas at a given pressure) and at a pressure P1b identical to the inlet pressure P1 of the natural gas, with the pressure drops close to it.
- bubble temperature means the temperature at which the first vapor bubbles are formed in a liquid natural gas at a given pressure
- P1b identical to the inlet pressure P1 of the natural gas
- the natural gas flowing in the pipe 10 is cooled in the reboiler E4 of a denitrogenation column C0.
- the natural gas 12 is cooled by heating the bottom (25, 26) of the column C0 by indirect heat exchange, then is expanded in the expansion member V1.
- the diphasic mixture 13 obtained at the outlet of the member V1 is introduced into the column C0 at a level N1.
- a gas fraction 38 enriched in nitrogen is recovered. It is sent to be cooled in a heat exchanger E5 and then separated in a phase separator pot B2 in the form of a gaseous fraction 21 and a liquid fraction 21 '.
- the gaseous fraction 21 discharged from the pot B2 is introduced into the exchanger E2.
- the gaseous fraction countercurrently cools the stream 4 of natural gas, then is directed via the conduit 22 into the compressor K4.
- the liquid fraction 21 'discharged from the pot B2 is used as reflux at the top of the column CO.
- the liquid fraction 31, depleted in nitrogen, discharged in the column tank CO is separated into two parts 32 and 34.
- a first part 32 is cooled in a heat exchanger E3, then is expanded in an expansion member 33 'at a pressure between 0.05MPa and 0.5MPa.
- the second portion 34 of the liquid fraction 31 is expanded in an expansion member 34 'and then fed to a heat exchanger E5.
- the vaporization of this stream 35 gives a current 36 and represents the majority of the refrigeration necessary for cooling the gas stream 38 from the head of the column CO in the heat exchanger E5.
- the expansion members such as V1, 33 'and 34' may be an expansion turbine, an expansion valve or a combination of a turbine and a valve.
- the two-phase mixture obtained at the outlet of the expansion element 33 ' is mixed with the flow 36 to give the two-phase mixture 37.
- the flow 37 is separated in a phase separator pot B1 in the form of a gas fraction 41 and a liquid fraction 61.
- the gaseous fraction 41 is introduced into the exchanger E3.
- the gaseous fraction 41 cools the liquid fraction 32 coming from the liquid stream 31 recovered in the vat of the column C1, then is directed by the duct 42 into the compressor K3.
- the gaseous mixture 49 leaving the compressor K3 is sent to a heat exchanger C3 to be cooled by air or water.
- the gaseous mixture 50 leaving the exchanger C3 is then mixed with the stream 1 of natural gas flowing in the pipe 51.
- the liquid fraction 61 discharged from the flask B1 forms the liquefied natural gas (LNG) produced.
- the gas 28 flowing through the conduit 27 may serve as fuel gas, energy source for the operation of a liquefaction plant.
- the denitrogenated LNG stream 31 produced at the bottom of the column CO is divided into two parts:
- stream 32 is countercurrently cooled with the flash gas, stream 41, to give the stream 33 which is expanded to the pressure P3 to be mixed with the stream 36 and to give the stream 37 which feeds the flash balloon LNG B1.
- Natural gas arrives via line 01 at a pressure of 60 bar and a temperature of 15 ° C.
- the composition of this gas in molar fraction is as follows:
- the mixed refrigerant of the pre-cooling cycle (PR) is the same for both processes: 50% ethane and 50% propane. It is implemented in the same way, only flows are adapted to the needs.
- LR the refrigerant performing the subcooling of natural gas.
- the new process makes it possible to produce LNG that is low in nitrogen while saving energy.
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AU2018392161A AU2018392161A1 (en) | 2017-12-21 | 2018-12-17 | Method for liquefying a natural gas stream containing nitrogen |
RU2020121187A RU2797474C2 (en) | 2017-12-21 | 2018-12-17 | Method for liquefying a natural gas stream containing nitrogen |
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FR1762736A FR3075940B1 (en) | 2017-12-21 | 2017-12-21 | PROCESS FOR LIQUEFACTION OF A NITROGEN-CONTAINING NATURAL GAS STREAM |
FR1762736 | 2017-12-21 |
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WO2019122656A1 true WO2019122656A1 (en) | 2019-06-27 |
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PCT/FR2018/053334 WO2019122656A1 (en) | 2017-12-21 | 2018-12-17 | Method for liquefying a natural gas stream containing nitrogen |
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Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6105389A (en) | 1998-04-29 | 2000-08-22 | Institut Francais Du Petrole | Method and device for liquefying a natural gas without phase separation of the coolant mixtures |
US6449984B1 (en) * | 2001-07-04 | 2002-09-17 | Technip | Process for liquefaction of and nitrogen extraction from natural gas, apparatus for implementation of the process, and gases obtained by the process |
US6763680B2 (en) | 2002-06-21 | 2004-07-20 | Institut Francais Du Petrole | Liquefaction of natural gas with natural gas recycling |
US20110239701A1 (en) * | 2008-11-03 | 2011-10-06 | Sander Kaart | Method of rejecting nitrogen from a hydrocarbon stream to provide a fuel gas stream and an apparatus therefor |
US20120090355A1 (en) * | 2009-03-25 | 2012-04-19 | Costain Oil, Gas & Process Limited | Process and apparatus for separation of hydrocarbons and nitrogen |
-
2017
- 2017-12-21 FR FR1762736A patent/FR3075940B1/en active Active
-
2018
- 2018-12-17 AU AU2018392161A patent/AU2018392161A1/en active Pending
- 2018-12-17 WO PCT/FR2018/053334 patent/WO2019122656A1/en active Application Filing
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6105389A (en) | 1998-04-29 | 2000-08-22 | Institut Francais Du Petrole | Method and device for liquefying a natural gas without phase separation of the coolant mixtures |
US6449984B1 (en) * | 2001-07-04 | 2002-09-17 | Technip | Process for liquefaction of and nitrogen extraction from natural gas, apparatus for implementation of the process, and gases obtained by the process |
US6763680B2 (en) | 2002-06-21 | 2004-07-20 | Institut Francais Du Petrole | Liquefaction of natural gas with natural gas recycling |
US20110239701A1 (en) * | 2008-11-03 | 2011-10-06 | Sander Kaart | Method of rejecting nitrogen from a hydrocarbon stream to provide a fuel gas stream and an apparatus therefor |
US20120090355A1 (en) * | 2009-03-25 | 2012-04-19 | Costain Oil, Gas & Process Limited | Process and apparatus for separation of hydrocarbons and nitrogen |
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FR3075940B1 (en) | 2020-05-22 |
RU2020121187A (en) | 2021-12-27 |
AU2018392161A1 (en) | 2020-07-09 |
FR3075940A1 (en) | 2019-06-28 |
RU2020121187A3 (en) | 2022-04-04 |
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