WO2019122654A1 - Procédé de production d'azote pur à partir d'un courant de gaz naturel contenant de l'azote - Google Patents
Procédé de production d'azote pur à partir d'un courant de gaz naturel contenant de l'azote Download PDFInfo
- Publication number
- WO2019122654A1 WO2019122654A1 PCT/FR2018/053332 FR2018053332W WO2019122654A1 WO 2019122654 A1 WO2019122654 A1 WO 2019122654A1 FR 2018053332 W FR2018053332 W FR 2018053332W WO 2019122654 A1 WO2019122654 A1 WO 2019122654A1
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- WO
- WIPO (PCT)
- Prior art keywords
- stream
- nitrogen
- cooled
- natural gas
- gas
- Prior art date
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 112
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 96
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 56
- 239000003345 natural gas Substances 0.000 title claims abstract description 34
- 238000004519 manufacturing process Methods 0.000 title description 3
- 238000000034 method Methods 0.000 claims abstract description 41
- 239000007788 liquid Substances 0.000 claims abstract description 34
- 239000007789 gas Substances 0.000 claims abstract description 33
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 26
- 238000001816 cooling Methods 0.000 claims abstract description 10
- 238000004821 distillation Methods 0.000 claims abstract description 4
- 239000000203 mixture Substances 0.000 claims description 31
- 239000003507 refrigerant Substances 0.000 claims description 20
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 14
- GNFTZDOKVXKIBK-UHFFFAOYSA-N 3-(2-methoxyethoxy)benzohydrazide Chemical compound COCCOC1=CC=CC(C(=O)NN)=C1 GNFTZDOKVXKIBK-UHFFFAOYSA-N 0.000 claims description 8
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 7
- 239000001294 propane Substances 0.000 claims description 7
- 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
- 238000010992 reflux Methods 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 3
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 3
- YTAHJIFKAKIKAV-XNMGPUDCSA-N [(1R)-3-morpholin-4-yl-1-phenylpropyl] N-[(3S)-2-oxo-5-phenyl-1,3-dihydro-1,4-benzodiazepin-3-yl]carbamate Chemical compound O=C1[C@H](N=C(C2=C(N1)C=CC=C2)C1=CC=CC=C1)NC(O[C@H](CCN1CCOCC1)C1=CC=CC=C1)=O YTAHJIFKAKIKAV-XNMGPUDCSA-N 0.000 claims description 2
- 239000001273 butane Substances 0.000 claims description 2
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 2
- 238000005057 refrigeration Methods 0.000 description 4
- 239000004229 Alkannin Substances 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 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
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000001282 iso-butane Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000002040 relaxant effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 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
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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
- F25J1/0032—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
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- 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
- 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
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- F25J1/005—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 expansion of a gaseous refrigerant stream with extraction of work
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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
- F25J1/0047—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
- 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
- F25J1/0211—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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- 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
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- 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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- 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
- F25J1/02—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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- 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
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- 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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- 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
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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
- F25J3/0257—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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- 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
- F25J3/0295—Start-up or control of the process; Details of the apparatus used, e.g. sieve plates, packings
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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
- F25J2270/12—External refrigeration with liquid vaporising loop
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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
- F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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. At the outlet of the 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.
- 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 present invention is to achieve, under better conditions, a separation of the nitrogen that may be contained in the gas and to discharge a portion of the nitrogen contained in the natural gas to the atmosphere in the form of pure nitrogen.
- Nitrogen is pure nitrogen containing between 50 ppm and 1% methane according to the legislation in force.
- the inventors of the present invention have developed a solution for producing liquefied natural gas low in nitrogen from a feed stream of natural gas that may contain more than 4 mol% of nitrogen, while saving energy and while minimizing the cost of deploying this type of process.
- the present invention relates to a method of liquefying a natural gas feed stream comprising the following steps:
- step b) is used during step c) to cool said at least a portion of the nitrogen-enriched vapor stream from step b) into said heat exchanger.
- the subject of the invention is also: A process as defined above, characterized in that during 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 to obtain a cooled natural gas and a cooled second refrigerant mixture, and then condensing and cooling the cooled natural gas by indirect heat exchange with the cooled second cooling mixture and with at least a portion of the gaseous stream obtained in step d) to obtain a liquefied natural gas.
- a process as defined above characterized in that the stream enriched in nitrogen produced during stage e) contains less than 100 ppm molar methane and the liquid stream produced during stage e) contains less than 4% molar nitrogen.
- 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.
- step a) wherein in step a) 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 S1 at a temperature T1.
- This unit S1 may comprise one or more heat exchangers E1, E2 and one or more refrigerant compressors K1, K2.
- the feed stream 1 may contain methane, ethane, propane, hydrocarbons having at least four carbon atoms.
- This stream may contain traces of contaminants, for example from 0 to 1 ppm of H2O,
- the molar percentage of nitrogen in this feed stream may be greater than 4%.
- the stream 1 of natural gas is introduced at a pressure P1 of between 4 MPa and 7 MPa and at a temperature between 0 ° C. and 60 ° C. in the unit S1. .
- the main stream of natural gas 1 is mixed with the gas 50 to form a mixture of natural gas flowing in the unit S1.
- the mixture thus formed liquefies from unit S1 via line 10 at a temperature which is preferably at least 10 ° C.
- bubble temperature means the temperature at which the first vapor bubbles are formed in a liquid natural gas at a given pressure
- P1b the pressure at which the first vapor bubbles are formed in a liquid natural gas at a given pressure
- the natural gas leaves the unit S1 at a temperature of between -105 ° C. and -145 ° C. and at a pressure of between 4 MPa and 7 MPa. Under these conditions of temperature and pressure, the natural gas does not remain completely liquid after expansion to atmospheric pressure.
- the natural gas flowing in the duct 10 is cooled in the reboiler E4 of a denitrogenation column C1.
- the natural gas is cooled 12 by heating the bottom (25, 26) of the column C1 by indirect heat exchange, then is expanded in the expansion member V1.
- the diphasic mixture 13 obtained at the output of the member V1 is introduced into the column C1 at a level N1.
- a gaseous fraction 100 enriched in nitrogen is recovered.
- the gaseous fraction 100 is separated into two parts 38 and 22.
- a portion 22 is heated, compressed with the aid of the compressor K4 and sent to the network, which can serve as fuel gas, energy source for the operation of a plant. liquefaction.
- the other part 38 is sent, to be cooled 39, 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 40.
- the liquid fraction 40 evacuated of pot B2 is used as reflux at the top of column C1.
- the liquid fraction 31, depleted of nitrogen, discharged in column vessel C1 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 C1 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 separated in a phase separator pot B1 in the form of a gaseous 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 gas mixture 49 leaving the compressor K3 is sent to a heat exchanger E103 to be cooled by air or water.
- the gas mixture 50 leaving the exchanger E103 is then mixed with the stream 1 of natural gas flowing in the unit S1.
- the liquid fraction 61 discharged from the flask B1 forms the liquefied natural gas (LNG) produced. More particularly, the denitrogenated LNG stream 31 produced at the bottom of the column CO is divided into two parts:
- a first minority part, flow 34 is expanded in the valve 34 'to a low pressure P3 between 0.05 MPa and 0.5 MPa to give the flow 35 and feeds the exchanger E5.
- the vaporization of this stream which gives the flow 36 provides the bulk of the refrigeration necessary for the cooling of the overhead steam in the exchanger E5.
- a second majority part, stream 32, is countercurrently cooled with the flash gas, stream 41, to give the flow which is expanded 33 to the pressure P3 to be mixed with the stream 36 and to give the flow 37 which feeds the flash balloon LNG B1.
- the gaseous fraction 21 discharged from the pot B2 is introduced, at the pressure P2, into a distillation column C2 producing, at the top, pure nitrogen 41 1 and, in the bottom, a liquid with a low nitrogen content 421, c '. that is to say containing less than 10 mol% of nitrogen, preferably less than 4%.
- a flow portion 414 is compressed to a high pressure P4 in the multi-stage compressor K5 to form, after cooling to ambient temperature, the flow 418.
- P4 is typically greater than 15 bar abs.
- P2 is for example between 3 bar abs and 10 bar abs.
- the flow 418 is then expanded for example in the valve V2 (or in a hydraulic turbine) and feeds the column C2 on the head plate. It constitutes a reflux.
- a very minor portion of the stream 1 is taken to give the current 452 which is cooled in the exchanger E1 1.
- This current 452 makes it possible to maintain, in the exchanger E1 1, temperature conditions that are compatible with the use of a plate heat exchanger.
- additional refrigeration is provided by relaxing a portion of this current 452.
- the current 421 is expanded by means of a valve V3.
- the expanded stream 422 is introduced into the exchanger E1 1 against the current flow 418, then discharged 423 and finally mixed with the stream 37 which is introduced into the balloon B1.
- the method according to the present invention thus makes it possible to produce a liquefied natural gas low in nitrogen by saving energy from a stream of natural gas containing a much larger quantity of nitrogen than the specifications allow.
- the process according to the invention makes it possible to produce fuel gas whose nitrogen content is compatible with the specifications of the different equipment and pure nitrogen. Pure nitrogen nitrogen containing between 50 ppm molar and 1 mol% methane according to the legislation in force.
- 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 composed of 50% ethane and 50% propane, the flow rates are adapted to the needs.
- the flow 22 sent to the gas network is intended to supply the turbines.
- the nitrogen content of the gas on the network must be compatible with the operation of the gas turbines.
- Stream 22 in the numerical example above contains 44 mol% of nitrogen.
- the method according to the invention has the advantage of allowing a great deal of flexibility in the choice of the flow rate of the flow 22 in order to obtain the desired nitrogen content on the network by mixing with the feed gas or other gas sources intended to the network.
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
RU2020121255A RU2797978C9 (ru) | 2017-12-21 | 2018-12-17 | Способ получения чистого азота из потока природного газа, содержащего азот |
AU2018392159A AU2018392159A1 (en) | 2017-12-21 | 2018-12-17 | Method for producing pure nitrogen from a natural gas stream containing nitrogen |
US16/954,769 US11604024B2 (en) | 2017-12-21 | 2018-12-17 | Method for producing pure nitrogen from a natural gas stream containing nitrogen |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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FR1762735 | 2017-12-21 | ||
FR1762735A FR3075939B1 (fr) | 2017-12-21 | 2017-12-21 | Procede de production d'azote pur a partir d'un courant de gaz naturel contenant de l'azote |
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WO2019122654A1 true WO2019122654A1 (fr) | 2019-06-27 |
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PCT/FR2018/053332 WO2019122654A1 (fr) | 2017-12-21 | 2018-12-17 | Procédé de production d'azote pur à partir d'un courant de gaz naturel contenant de l'azote |
Country Status (4)
Country | Link |
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US (1) | US11604024B2 (fr) |
AU (1) | AU2018392159A1 (fr) |
FR (1) | FR3075939B1 (fr) |
WO (1) | WO2019122654A1 (fr) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
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US20210140710A1 (en) * | 2019-11-07 | 2021-05-13 | Conocophillips Company | Systems and methods for removing nitrogen during liquefaction of natural gas |
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US20230076428A1 (en) * | 2021-09-02 | 2023-03-09 | Air Products And Chemicals, Inc. | Integrated nitrogen rejection for liquefaction of natural gas |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5617741A (en) * | 1995-02-10 | 1997-04-08 | Air Products And Chemicals, Inc. | Dual column process to remove nitrogen from natural gas |
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 |
US20120090355A1 (en) * | 2009-03-25 | 2012-04-19 | Costain Oil, Gas & Process Limited | Process and apparatus for separation of hydrocarbons and nitrogen |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7850763B2 (en) * | 2007-01-23 | 2010-12-14 | Air Products And Chemicals, Inc. | Purification of carbon dioxide |
WO2010060735A2 (fr) | 2008-11-03 | 2010-06-03 | Shell Internationale Research Maatschappij B.V. | Procede de rejet d'azote d'un flux d'hydrocarbure pour produire un flux de gaz combustible et appareil associe method of rejecting nitrogen from a hydrocarbon stream to provide a fuel gas stream and an apparatus therefor |
DE102009036366A1 (de) | 2009-08-06 | 2011-02-10 | Linde Aktiengesellschaft | Verfahren zum Abtrennen von Stickstoff |
-
2017
- 2017-12-21 FR FR1762735A patent/FR3075939B1/fr active Active
-
2018
- 2018-12-17 WO PCT/FR2018/053332 patent/WO2019122654A1/fr active Application Filing
- 2018-12-17 AU AU2018392159A patent/AU2018392159A1/en active Pending
- 2018-12-17 US US16/954,769 patent/US11604024B2/en active Active
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5617741A (en) * | 1995-02-10 | 1997-04-08 | Air Products And Chemicals, Inc. | Dual column process to remove nitrogen from natural gas |
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 |
US20120090355A1 (en) * | 2009-03-25 | 2012-04-19 | Costain Oil, Gas & Process Limited | Process and apparatus for separation of hydrocarbons and nitrogen |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20210140710A1 (en) * | 2019-11-07 | 2021-05-13 | Conocophillips Company | Systems and methods for removing nitrogen during liquefaction of natural gas |
Also Published As
Publication number | Publication date |
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RU2020121255A3 (fr) | 2022-03-31 |
FR3075939A1 (fr) | 2019-06-28 |
US11604024B2 (en) | 2023-03-14 |
FR3075939B1 (fr) | 2020-06-19 |
US20210088276A1 (en) | 2021-03-25 |
AU2018392159A1 (en) | 2020-07-09 |
RU2020121255A (ru) | 2021-12-27 |
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