EP2724100B1 - Method for liquefying natural gas with a triple closed circuit of coolant gas - Google Patents
Method for liquefying natural gas with a triple closed circuit of coolant gas Download PDFInfo
- Publication number
- EP2724100B1 EP2724100B1 EP12731601.6A EP12731601A EP2724100B1 EP 2724100 B1 EP2724100 B1 EP 2724100B1 EP 12731601 A EP12731601 A EP 12731601A EP 2724100 B1 EP2724100 B1 EP 2724100B1
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- EP
- European Patent Office
- Prior art keywords
- compressor
- flow
- gas
- exchanger
- pressure
- Prior art date
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- 239000007789 gas Substances 0.000 title claims description 308
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims description 257
- 238000000034 method Methods 0.000 title claims description 142
- 239000003345 natural gas Substances 0.000 title claims description 102
- 239000002826 coolant Substances 0.000 title claims description 38
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 144
- 239000000203 mixture Substances 0.000 claims description 91
- 229910052757 nitrogen Inorganic materials 0.000 claims description 66
- 239000003949 liquefied natural gas Substances 0.000 claims description 54
- 238000009434 installation Methods 0.000 claims description 50
- 239000001257 hydrogen Substances 0.000 claims description 32
- 229910052739 hydrogen Inorganic materials 0.000 claims description 32
- 238000001816 cooling Methods 0.000 claims description 20
- 238000007667 floating Methods 0.000 claims description 19
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N dimethylmethane Natural products CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 15
- TUVQIHHKIZFJTE-UHFFFAOYSA-N [N].[Ne] Chemical compound [N].[Ne] TUVQIHHKIZFJTE-UHFFFAOYSA-N 0.000 claims description 8
- 239000001273 butane Substances 0.000 claims description 7
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 7
- 239000001294 propane Substances 0.000 claims description 7
- 238000011084 recovery Methods 0.000 claims description 5
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 2
- 239000003507 refrigerant Substances 0.000 description 182
- 230000008569 process Effects 0.000 description 103
- 230000004907 flux Effects 0.000 description 100
- 239000012071 phase Substances 0.000 description 56
- 238000010586 diagram Methods 0.000 description 35
- 229910052754 neon Inorganic materials 0.000 description 33
- GKAOGPIIYCISHV-UHFFFAOYSA-N neon atom Chemical compound [Ne] GKAOGPIIYCISHV-UHFFFAOYSA-N 0.000 description 33
- 238000005265 energy consumption Methods 0.000 description 31
- 239000012530 fluid Substances 0.000 description 22
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 19
- 230000008859 change Effects 0.000 description 19
- 238000012550 audit Methods 0.000 description 17
- 238000007906 compression Methods 0.000 description 14
- 230000006835 compression Effects 0.000 description 13
- 238000002347 injection Methods 0.000 description 13
- 239000007924 injection Substances 0.000 description 13
- 239000007788 liquid Substances 0.000 description 9
- 238000004519 manufacturing process Methods 0.000 description 8
- 150000002431 hydrogen Chemical class 0.000 description 7
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 6
- 229940082150 encore Drugs 0.000 description 6
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 6
- 230000008901 benefit Effects 0.000 description 5
- 235000021183 entrée Nutrition 0.000 description 5
- -1 comprising methane Chemical compound 0.000 description 4
- 230000007423 decrease Effects 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 4
- 238000007796 conventional method Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 238000004880 explosion Methods 0.000 description 3
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- 238000012552 review Methods 0.000 description 3
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- 230000033228 biological regulation Effects 0.000 description 2
- 230000000295 complement effect Effects 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000003673 groundwater Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- PQVHMOLNSYFXIJ-UHFFFAOYSA-N 4-[2-(2,3-dihydro-1H-inden-2-ylamino)pyrimidin-5-yl]-1-[2-oxo-2-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)ethyl]pyrazole-3-carboxylic acid Chemical compound C1C(CC2=CC=CC=C12)NC1=NC=C(C=N1)C=1C(=NN(C=1)CC(N1CC2=C(CC1)NN=N2)=O)C(=O)O PQVHMOLNSYFXIJ-UHFFFAOYSA-N 0.000 description 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- 241000287107 Passer Species 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000001747 exhibiting effect Effects 0.000 description 1
- 238000009472 formulation Methods 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000007726 management method Methods 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 230000033764 rhythmic process Effects 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 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
- 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
- F25J1/0002—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
- F25J1/0025—Boil-off gases "BOG" from storages
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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
- F25J1/005—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
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/007—Primary atmospheric gases, mixtures thereof
- F25J1/0072—Nitrogen
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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
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
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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
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- 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
- F25J1/0203—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle
- F25J1/0204—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a single flow SCR cycle
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- 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
- F25J1/0212—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 as a single flow MCR cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- 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
- F25J1/0244—Operation; Control and regulation; Instrumentation
- F25J1/0254—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- 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.
- F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
- F25J1/0283—Gas turbine as the prime mechanical driver
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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
- F25J1/02—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
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- F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
- F25J1/0284—Electrical motor as the prime mechanical driver
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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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- 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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- F25J1/0287—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings including an electrical motor
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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.
- F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
- F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
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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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- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0289—Use of different types of prime drivers of at least two refrigerant compressors in a cascade refrigeration system
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- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
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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
- F25J2230/22—Compressor driver arrangement, e.g. power supply by motor, gas or steam turbine
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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
- F25J2270/14—External refrigeration with work-producing gas expansion 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
- F25J2270/14—External refrigeration with work-producing gas expansion loop
- F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant
Definitions
- the present invention relates to a process for liquefying natural gas to produce LNG, or Liquefied Natural Gas, also called LNG. More particularly still, the present invention relates to the liquefaction of natural gas mainly comprising methane, preferably at least 85% of methane, the other main constituents being chosen from nitrogen and C-2 to C-4 alkanes. namely ethane, propane, butane.
- the present invention also relates to a liquefaction installation arranged on a ship or a floating support at sea, either in the open sea or in a protected area, such as a port, or even an onshore installation in the case of small or medium-sized vessels. liquefaction of natural gas.
- the present invention relates more particularly to a process for re-liquefying gas on board an LNG transport ship called a “methane tanker”, said gas to be re-liquefied being the result of reheating and partial evaporation of the LNG contained in the tanks of said vessel, said evaporated gas, in general mainly methane, being called in English “boil off”.
- Methane-based natural gas is either a by-product of oil fields, produced in small or medium quantities, usually associated with crude oil, or a major product in the case of gas fields, where it is then in combination with other gases, mainly C-2 to C-4 alkanes, CO2, nitrogen.
- cryogenic liquid -165 ° C
- LNG carriers Specialized transport vessels have very large tanks with extreme insulation so as to limit evaporation during the voyage.
- the liquefaction of gas for transport is generally carried out near the production site, generally on land, and requires considerable facilities to reach capacities of several million tonnes per year, the largest existing units grouping together three or four liquefaction units of 3-4 Mt per year of unit capacity.
- This liquefaction process requires considerable amounts of mechanical energy, the mechanical energy being generally produced on site by taking part of the gas to produce the energy necessary for the liquefaction process. Part of the gas is then used as fuel in gas turbines, steam turbines or reciprocating heat engines.
- thermodynamic cycles have been developed in order to optimize the overall energy efficiency.
- a first type based on the compression and expansion of refrigerant fluid, with phase change
- a second type based on the compression and expansion of refrigerant gas without phase change.
- refrigerant fluid or “refrigerant gas” is used to refer to a gas or mixture of gases, circulating in a closed circuit and undergoing compression phases, where appropriate liquefaction, then heat exchanges with the external environment, then subsequently phases of expansion, where appropriate of evaporation, and finally of heat exchanges with the natural gas to be liquefied comprising methane, which gradually cools down to reach its liquefaction temperature at atmospheric pressure, i.e. approximately - 165 ° C in the case of LNG.
- Said first type of cycle, with phase change, is in general used on land installations and requires a large amount of equipment and a considerable footprint.
- refrigerant fluids generally in the form of mixtures, consist of butane, propane, ethane and methane, these gases being dangerous because they risk, in the event of leakage, causing explosions or considerable fires. .
- they remain the most efficient and require energy of the order of 0.3 kWh per kg of LNG produced.
- the second type of liquefaction process a process without phase change of the refrigerant gas
- the efficiency of this second type is lower, because it generally requires an energy of the order of 0.5 kWh / kg of LNG produced, i.e. about 20.84 kW x day / t and, on the other hand, it has a considerable advantage in terms of safety, because the refrigerant gas of the cycle, nitrogen, is inert and therefore incombustible, which is very interesting when the installations are concentrated in a small space, for example on the deck of a floating support installed in the open sea, said equipment often being installed on several levels, one above the other on a small surface to the bare minimum.
- a refrigerant gas leak there is no danger of explosion and it is then sufficient to reinject the lost refrigerant gas fraction into the circuit.
- this method of liquefying natural gas without phase change is very advantageous in the case of floating supports, because, due to the absence of a liquid phase in the refrigerant gas, the equipment is of much simpler design. In fact, in such installations, all of the equipment moves almost continuously to the rhythm of the movements of the floating support (roll, pitch, yaw, sheer, swing, heave). And the management of a process with phase change involving a liquid phase of the refrigerant would be extremely delicate even for weak movements of the floating support, or even almost impossible for extreme movements, whereas in fixed installations on land the problem of movements does not arise.
- the refrigerant in the case of the phase change cycle of the refrigerant fluid, for the yields to remain optimum, the refrigerant must be adapted to the nature and composition of the gas to be liquefied. and the composition of the refrigerant fluid must, if necessary, be modified over time, depending on the composition of the mixture of natural gas to be liquefied produced by the oil field.
- the refrigerant gas remains in the gaseous state and circulates continuously as explained previously: it gradually gives up frigories, therefore gradually absorbs calories from the gas to be liquefied, namely a mixture consisting mainly of of methane and other traces of gas.
- the circulation of the gas to be liquefied takes place against the current of the refrigerant gas, that is to say that said natural gas comprising methane enters substantially at ambient temperature into the exchanger at the level of the refrigerant gas outlet where the latter is then substantially at room temperature.
- said natural gas comprising methane progresses through the exchanger towards the colder zones and transfers its calories to the refrigerant fluid: the natural gas comprising methane cools and the refrigerant gas heats up.
- T3 -165 ° C for a gas containing 85% methane.
- Phase 2 consumes the most energy, because the gas must be supplied with all the energy corresponding to its latent heat of vaporization. Phase 1 consumes a little less energy, and phase 3 consumes the least energy, on the other hand it is done at the lowest temperatures, i.e. around -165 ° C.
- T1, T2 and T3 are suitable for a natural gas consisting of 85% methane and 15% of said other components nitrogen and C-2 to C-4 alkanes, and can vary significantly for a gas of different composition.
- FIG. 1 there is shown an installation diagram of a standard natural gas liquefaction process involving a refrigerant gas consisting of nitrogen without phase change of the refrigerant gas as described above and the description of the process of which is explained later. .
- the pressure levels P1 and P2 of the gases leaving the turbines 112 and 111 are different and therefore the flow rates passing through the regulators 111 and 112 are different and in particular in practice in a ratio of 10-20% of the total flow for the flow rate of the flow from expander 112 against 80-90% for the flow rate from expander 111.
- compressor 115b only recovers 10-20% of the total power recovered compared to 80-90% of power recovered at the level compressor 115a.
- This disparity in power supplied to the two compressors 115a and 115b mounted in parallel results in a major difficulty in stabilizing the operation of the circuit.
- Stabilization of the operation of the circuit can be carried out conventionally by means of control valves upstream and / or downstream of said compressors 115a and 115b mounted in parallel, and / or upstream and / or downstream of said turbines 111 and 112 to control the compressors flow rates and operation.
- control valves upstream and / or downstream of said compressors 115a and 115b mounted in parallel, and / or upstream and / or downstream of said turbines 111 and 112 to control the compressors flow rates and operation.
- these control valves generate pressure losses, and therefore energy, which affects greatly the desired overall efficiency and / or the production capacity of the installation.
- the aim of the present invention is to provide a process for the liquefaction of natural gas of the type without phase change of the refrigerant gas capable of being installed on a ship or floating support which has improved energy efficiency, namely a total energy consumed in the tank. minimum process in terms of kWh to obtain 1 tonne of LNG and / or which exhibits increased heat transfers in the exchangers and / or which makes it possible to implement a more compact and efficient liquefaction installation.
- the term “compressor coupled to an expansion valve / turbine or engine” or “compressor actuated by an engine” (or vice versa a “expansion valve / turbine or engine coupled to the compressor”) is understood to mean that the output shaft of the turbine or respectively of the engine drives the input shaft of the compressor, that is to say, transfers mechanical energy to the shaft of the compressor. It is therefore a mechanical coupling of the compressor to the expansion valve / turbine or respectively of the compressor to the engine.
- said motor can be either a heat engine, or preferably an electric motor, or any other installation capable of supplying mechanical energy to the refrigerant gas; and the compressors are of the rotary turbine type, also called a centrifugal compressor.
- step (a) the liquefied natural gas leaving said third exchanger is depressurized at T3, from pressure P0 to atmospheric pressure where appropriate.
- the method according to the invention is advantageous over the method described in US 2011/0113825 in that all the compressors are mounted in series without requiring flow control with flow control valves to stabilize the operation of the installation. In fact, in the process according to the invention, there is no separation of flows in the compression chain. It follows that the regulation of flow rate of flow and / or energy at the level of the various compressors is obtained essentially by the regulation of the power input at the level of said first and second engines and said gas turbine. It is not essential to implement control valves at said compressors and said turbine because said first and second expansion valves are coupled to said first and second compressors mounted in series and are therefore not coupled to compressors mounted in series. parallels as in US 2011/0113825 .
- first and second compressors in series coupled to said first and second expansion valves also makes it possible to improve the compactness of the installation, which is particularly advantageous for the implementation of a process. aboard a floating support where space is limited.
- the method according to the invention with reference to figures 2- 3 is advantageous over that of figure 1 in that, first of all, rather than recycling after expansion a part D2 of the second flow at the outlet of the first exchanger to join the first flow at the inlet of the second exchanger, this part D2 is recycled from the second flow to the entry of the second exchanger at an intermediate pressure P2 greater than P1 in a third independent flow S3 and parallel to S1, that is to say in co-current of S1. And, because most of the energy is consumed for phase 2 of the process within said second exchanger, this makes it possible to increase the heat transfers and the energy efficiency of the process.
- the method according to the invention is advantageous over WO 2005/071333 and the method described in the GASTECH 2009 review cited above in that it allows said pressure P2 to be varied in a controlled manner so that the energy consumed for implementing the method (Ef) is minimal.
- the value of the pressure P2 can be modulated and specifically controlled by supplying a differentiated power to said first compressor thanks to said first motor, making it possible to modulate and control the power supplied to the various compressors in a differentiated manner and therefore to vary the value of P2.
- said pressure P2 is varied in a controlled manner by supplying power in a controlled manner to said first compressor with said first motor, so that the energy consumed for switching on.
- implementation of the process (Ef) is minimal, preferably when the composition of the natural gas to be liquefied varies.
- This process is more particularly advantageous because it thus makes it possible, by modulating and specifically controlling the value of the pressure P2 of said third flow, to modify and optimize the operating point of the process, namely to minimize the energy consumed and therefore to increase the efficiency in particular.
- the composition of the natural gas to be liquefied varies.
- said first motor provides at least 3%, preferably from 3 to 30% of the total power supplied to all of said compressors used, said gas turbine providing 97 to 70% of the power. total power supplied.
- a conventional liquefaction unit is dimensioned in relation to the power of the gas turbines available, high power turbines commonly being 25MW, or even 30MW when they are intended to be installed on a floating support. Fixed gas turbines installed on land can reach maximum powers of 90-100MW.
- the overall power is always the same, but in this case the efficiency of the assembly is improved, which represents a gain in energy consumed for the same power. overall, relative to a power injection at the second engine M2.
- This first variant embodiment is advantageous in that it allows for the most compact installation in terms of size on board the floating support.
- This second variant embodiment is advantageous in terms of thermodynamic efficiency and production capacity since a maximum capacity turbine available on the market can then be used advantageously as a gas turbine, that is to say 25-30MW in the case of gas turbine.
- turbines intended to be installed on a floating support plus a second electric motor, for example from 5 to 10 MW, connected to the second compressor, the overall power of the second motor and third motor (gas turbine) then being 30 to 40MW, therefore vastly superior to that of the largest gas turbines available on the market and intended for floating supports.
- the second engine can also be a gas turbine, preferably of identical power to the main gas turbine, which then makes it possible to achieve an overall power of 50 to 60 MW.
- the method according to the invention makes it possible, by varying the pressure P2 by supplying energy to said first compressor using said first motor, to implement a minimum total energy Ef consumed in the method of less than 21.5 kW x day / t, more particularly from 18.5 to 20.5 kW x day / t of liquefied gas produced.
- said refrigerant gas comprises nitrogen.
- said refrigerant gas consists of a single gas chosen from nitrogen, hydrogen and neon.
- neon is preferred in view of the greater explosion risk of hydrogen and the fact that hydrogen may have a certain propensity to percolate through elastomeric seals and even through low metal walls. thickness.
- the PFD Process Flow Diagram
- the process comprises compressors C1, C2 and C3, expansion valves E1 and E2, intercoolers H1 and H2 as well as cryogenic exchangers EC1, EC2 and EC3.
- the heat exchangers consist, in a known manner, of at least two fluid circuits juxtaposed but not communicating with each other at the level of said fluids, the fluids circulating in said circuits exchanging heat throughout the path within said exchanger thermal.
- a regulator achieves a pressure drop of a fluid or a gas and is represented by a symmetrical trapezoid, the small base of which represents the inlet 10a (high pressure), and the large base represents the outlet 10b (low pressure) as shown on figure 1 with reference to the regulator E2, said regulator can be a simple reduction in the diameter of the pipe, or else an adjustable valve, but in the case of the liquefaction process according to the invention, the regulator is generally a turbine intended to recover mechanical energy during said expansion, so that this energy is not lost.
- a compressor increases the pressure of a gas and is represented by a symmetrical trapezoid, the large base of which represents the inlet 11a (low pressure), and the small base represents the outlet 11b ( high pressure) as shown on figure 1 with reference to compressor C2, said compressor generally being a turbine or a piston compressor, or else a scroll compressor.
- the compressors C1 and C2 are mechanically connected to a motor M1 and M2 which can be either a heat engine, or an electric motor, or any other installation capable of providing mechanical energy.
- T0 a temperature
- T1 -50 ° C approximately.
- the natural gas cools by releasing calories to the refrigerant gas, which then heats up and must permanently undergo a complete thermodynamic cycle in order to be able to extract in a manner continues natural gas calories entering AA.
- the path of natural gas is represented on the left of the PFD, and said gas flows from top to bottom in the circuit Sg, the temperature decreasing from top to bottom, from a substantially ambient temperature T0 at the top in AA, to a temperature T3 of about -165 ° C at the bottom in DD.
- thermodynamic cycle of the double-loop refrigerant gas corresponding to circuits S1 and S2.
- the pressure levels in the main circuits are shown in thin lines for low pressure (P1 in circuit S1), in medium lines for intermediate pressure (P2), and in solid lines for high pressure (P3 in circuit S2).
- phases 1, 2 and 3 are carried out by a low pressure loop P1 at very low temperature at the lower inlet of EC3.
- a chiller H1, H2 can consist of a water exchanger, for example a sea or river water or cold air exchanger of the fan coil or cooling tower type, such as those used in nuclear power plants.
- C1 and C2 are therefore arranged in parallel and operate between the medium pressure P'3 and the high pressure P3 on the entire flow from C3.
- the refrigerant gas at the high outlet in AA of the circuit S1, at the level of the exchanger EC1 has a flow rate D: it is at low pressure P1 and at a temperature T'0 substantially lower than T0 and at ambient temperature. It is then compressed at C3 to pressure P'3 then passes through a cooler H1.
- the flow rate fluid D is then separated into two parts of flow rates D1 'and D2' which respectively supply the compressors C1 (D1 ') and C2 (D2') operating in parallel.
- the two streams at pressure P3 are then combined and then cooled substantially to ambient temperature T0 by passing through cooler H2.
- This overall flow D then enters the top of the cryogenic exchanger EC1 at the level of the circuit S2, then at the exit of the first level, in BB, a large part of the flow rate D2 (D2 greater than D1) is extracted and directed. to the turbine E2 coupled to the compressor C2. The rest of the flow D1 passes through the second stage of the cryogenic exchanger EC2, then to the level CC is directed to the turbine E1 coupled to the compressor C1.
- the flow D2 of refrigerant gas coming from the turbine E2 is at a pressure P1 and temperature T2 of about -120 ° C and is recombined within the circuit S1 to the flow D1 coming from the turbine E1 at the upper outlet. of the cryogenic exchanger EC3 in CC.
- the separation of the second flow S2 into two parts of different flow rates D1 and D2 at the outlet BB of the first exchanger, preferably with D2 greater than D1, is advantageous because most of the energy consumed occurs in phase 2 within the second exchanger EC2.
- the flow D of the circuit S1 is at the temperature T0 ′ substantially lower than the ambient temperature. Then, the flow D is again directed to the compressor C3 to continuously perform a new cycle.
- compressors C1 and C2 operate in parallel and must ensure the highest level of pressure in the cycle.
- the two compressors C1 and C2 process different refrigerant flow rates, respectively D1 'and D2', and are coupled directly to the turbines E1 and E2 which also process different flow rates, respectively D1 and D2.
- D1 / D 5 to 35%, preferably 10 to 25%.
- such an installation has an operating point which stabilizes itself at a given level of energy consumption Ef generally expressed in kW x day / t, that is to say in kW-day per tonne of LNG produced, or in kWh per kg of LNG produced, said operating point possibly being totally unstable. It is then very difficult to control the pressures of the high and low loops independently of one another. This may prove to be necessary in the case of variations in the composition of the natural gas to be liquefied. It is possible to modify the flows by locally constraining all or part of the D1-D'1-D2-D'1 flows, for example by creating localized pressure drops, but such arrangements lead to energy losses, therefore a drop in the overall efficiency of the liquefaction plant.
- the diagram of the figure 4 illustrates the change in enthalpy H, expressed in kJ / kg of LNG produced, in a natural gas liquefaction process.
- This diagram of the figure 4 is the result of a theoretical calculation relating to a natural gas comprising mainly methane (85%), the remainder (15%) consisting of nitrogen, ethane (C-2), propane (C-3) and butane (C-4).
- the curve 50 comprising triangles illustrates the variations in the enthalpy H of the fluids circulating in co-current in the circuits Sg and S2 as a function of the temperature of the gas to be liquefied comprising the methane / LNG for an ideal virtual process.
- Curve 51 corresponds to the variation in the enthalpy H of the refrigerant gas circulating in circuit S1 of the figure 1 , therefore represents the energy transferred to circuits Sg and S2 during the liquefaction process.
- the area 52 between the two curves 50 and 51 represents the overall loss of energy consumed Ef in the liquefaction process: it is therefore sought to minimize this area so as to obtain the best efficiency.
- curve 51 is no longer rectilinear, but is much closer to theoretical curve 50, which implies less losses, therefore improved efficiency, but the refrigerant phase change process is not suitable for liquefaction on board a floating support in a confined environment.
- this part D2 of the second flow at the CC inlet of the second exchanger is recycled at an intermediate pressure P2 greater than P1 in a third circuit S3 independent of S1, S2, SG, and parallel to S1, that is to say to co -current of S1.
- the entire flow of refrigerant gas D is at high pressure P3.
- the flow is then cooled in a cooler H2 before circulating in the circuit S2, from top to bottom, through each of the two cryogenic exchangers EC1-EC2.
- the refrigerant gas flow portion D2 is taken at BB at the outlet of the cryogenic exchanger EC1 and directed towards the inlet of the turbine E2, the remainder, that is to say the portion D1 of the flow of refrigerant gas being taken at DC at the outlet of the cryogenic exchanger EC2 and directed towards the inlet of the turbine E1.
- a cooler H2 operating at pressure P'3 is installed between two compression stages, said cooler H2 treating all of the stream D.
- the main advantage of the device according to the invention of the figure 2 lies in the possibility of optimizing the overall efficiency of the installations and of modifying at will the operating points of the various loops corresponding to the circuits S1-S2-S3, that is to say of minimizing the energy consumed by increasing or decreasing the power injected into one of the compressors C1-C2-C3, or by varying the distribution of the overall power Q injected into the system.
- Curve 53 corresponds to the variation of the enthalpy H of the refrigerant circulating in circuits S1 and S3 of the figure 2 , therefore represents the energy transferred during the liquefaction process to circuits Sg and S2 of the figure 2 .
- the surface 52 between the two curves 50 and 53 represents the overall energy loss in the liquefaction process with reference to the figure 2 : - We therefore seek to minimize this area so as to obtain the best performance.
- the low point 54 of the curve 50 corresponding to P0 and T2 at the end of LNG liquefaction may vary by a few%.
- the corresponding point 55 of the refrigerant gas circuit remains substantially fixed, and the surface 52, therefore the efficiency of the installation cannot be optimized.
- the position of point 56 can be advantageously varied, as we know thus move optimally in the direction of point 54, which makes it possible to reduce to a minimum the surface of the area 52 between the curves 50 and 53, and thus to optimize in real time the efficiency of the installation of liquefaction, depending on the composition of natural gas.
- the figure 3 shows the PFD diagram of a version of the invention exhibiting improved compactness compared to the method and installation of the figure 2 , in which the compressor C2 is integrated on the same shaft line as the compressor C3 and is driven by the gas turbine GT representing a mechanical energy input of 85 to 95% of the total energy Q.
- the expansion turbine E2 is then connected on the one hand to compressor C2 and on the other hand to the gas turbine GT.
- this compact version is advantageously justified in the event of a very limited available surface area, and in addition there are only two lines of rotating machine shafts and two compressors, whereas in the version with reference to the figure 2 , we must install three lines of rotating machine shafts and three compressors, which represents a significant additional cost, but provides greater flexibility in the fine adjustment of the various pressure loops, as well as a better final output, therefore a better profitability of installations in the long term, throughout the lifespan of the installations which exceeds 20 to 30 years, or even more.
- the operating point in the case of the conventional method of figure 1 with pure nitrogen is located at 60.
- the curve 70 (left portion) represents the variation of the energy yield as a function of the power injected into the process at the level of the motor M1 with reference to the figures 2 and 3 .
- Point W1 corresponds to a power W1> 0 supplied by said motor M1.
- Curve 90 represents the process according to figure 2 using a refrigerant gas composed of 100% nitrogen.
- Point W1 corresponds to a power W1> 0 supplied by said motor M1.
- the operating point W0 without energy input to the motor M1 corresponds, for a pure nitrogen process, to an energy consumption of approximately 21.25 kWxd / t, at the same pressure P1 of approximately 9 bars and a pressure P2 of about 11 bars: the energy efficiency is therefore improved by 7.06%.
- the energy yield is shown as a function of the pressure P3, and as a function of the various variants of the invention, in particular in the case of a neon nitrogen mixture.
- Points W0-W1-W2-W3-W4 correspond to the same levels of power injected into the motor M1 as described previously with reference to figures 5A - 6A .
- P3 thus represents the maximum pressure of the system at the level of circuit S3: it increases in proportion to the power injected, as well as to the percentage of neon in the refrigerant gas mixture.
- This minimum corresponds to the low point 71a of the curve 71 of the figure 5A , for a minimum energy consumption of approximately 19.4 kWxd / t, a pressure P1 of approximately 12.5 bars and a pressure P2 of approximately 33 bars.
- the operating point W0 of the same curve 91 corresponding to a 20% mixture of neon, without energy input to the motor M1 corresponds to an energy consumption of approximately 20.45 kW x day / t , at the same pressure P1 of approximately 12.5 bars and a pressure P2 of approximately 17 bars, which illustrates the improvement in energy efficiency when the increase in the percentage of neon is combined with the increase in the power injected at motor M1.
- the maximum pressure P3 is represented on the abscissa and the energy per unit mass of gas is on the ordinate.
- the operating point of the conventional process with reference to the figure 1 is located in 60 on this figure 7A .
- the efficiency of the installation can be varied according to curve 70 (20% neon) and other curves (40 - 50% of neon).
- thermodynamic efficiency can be increased by increasing the maximum pressure.
- a refrigerant gas consisting of 100% pure nitrogen by injecting part of the power at the level of the motor M1, and by operating at a pressure of approximately 68 bars, the consumption in energy drops to around 19.75 kWxd / t, which represents an efficiency gain of 7.28%.
- the volume flow rates are reduced in proportion to the increase in said pressure: - the pipes are of smaller diameter, but their mechanical resistance, therefore their thickness, their weight and cost are increased by as much: - on the other hand, the footprint is reduced accordingly, which is very interesting in the case of installations in a confined environment such as on an anchored floating support at sea, or on an LNG carrier in the case of a boil-off reliquefaction unit.
- compressors and turbines operating at higher pressure are much more compact.
- cryogenic exchangers the increase in pressure also improves heat transfers, but the heat exchange surfaces are not reduced in the same proportion as in the case of pipes and compressors and turbines.
- their weight increases significantly because they have to resist this increase in pressure.
- the method according to the invention of figures 2-3 leads to installations having greater compactness and to a significant improvement in energy efficiency when the refrigerant gas is pure nitrogen, said energy efficiency being further improved when the refrigerant gas is a mixture of nitrogen and either neon, or hydrogen.
- FIG 7A there is shown a performance diagram of a conventional process with reference to the figure 1 , and the method according to the invention of figures 2-3 using as refrigerant gas a mixture of nitrogen and neon, in which the maximum pressure P3 is represented on the abscissa and the energy per unit mass of gas is on the ordinate. Energy is represented in KW x day per tonne of natural gas (kW xd / t).
- the operating point of the conventional process with reference to the figure 1 is located in 60 on this figure 7A .
- the efficiency of the installation can be varied according to curve 61 with an optimum operating point 62 at approximately 68 bars, corresponding to an energy consumption of approximately 19.75 kWxd / t, which represents an efficiency gain of 7.28% compared to the operating point 60 of the conventional process.
- the pressure can be increased, as shown on curve 70, without the gas mixture reaching its dew point, up to an optimum value 70a of approximately 88 bars and for a minimum energy consumption of approximately 19.4 kWxd / t, which represents a gain in thermodynamic efficiency of 1.77% compared to the operating point 62 of the process according to invention with a refrigerant gas composed of 100% nitrogen and a thermodynamic efficiency gain of 8.92% over the operating point 60 of the conventional process.
- the pressure can be increased, as shown on curve 71, without the gas mixture reaching its dew point, up to an optimum value 71a of approximately 118 bars and for a minimum energy consumption of approximately 19.15 kWxd / t, which represents a gain in thermodynamic efficiency of 3.04% compared to the operating point 62 of the process according to the invention with a refrigerant gas composed of 100% nitrogen and a thermodynamic efficiency gain of 10.09% compared to the operating point 60 of the conventional process.
- the pressure can be increased, as shown on curve 72, without the gas mixture reaching its dew point, up to an optimum value 72a of approximately 145 bars and for a minimum energy consumption of approximately 18.8 kWxd / t, which represents a gain in thermodynamic efficiency of 4.81% compared to the operating point 62 of the process according to the invention with a refrigerant gas composed of 100% nitrogen and a thermodynamic efficiency gain of 11.74% compared to the operating point 60 of the conventional process.
- a mixture of nitrogen and hydrogen is advantageously used as refrigerant gas.
- the pressure can be increased, as shown on curve 80, without the gas mixture reaching its dew point, up to an optimum value 80a of around 94 bars and for a minimum energy consumption of around 19.2 kWxd / t, which represents a thermodynamic efficiency gain of 2.78% compared to the operating point 62 of the method according to the invention of figures 2-3 with a refrigerant gas composed of 100% nitrogen, and a thermodynamic efficiency gain of 9.86% compared to the operating point 60 of the conventional process of the figure 1 .
- the pressure can be increased, as shown in curve 81, without the gas mixture reaching its dew point, up to at an optimum value 81a of approximately 140 bars and for a minimum energy consumption of approximately 18.8 kWxd / t, which represents a gain in thermodynamic efficiency of 4.81% compared to the operating point 62 of the process according to the invention of figures 2-3 with a refrigerant gas composed of 100% nitrogen and a thermodynamic efficiency gain of 11.74% compared to the operating point 60 of the conventional process of the figure 1 .
- the pressure can be increased, as shown on curve 82, without the gas mixture reaching its dew point, up to at an optimum value 82a of approximately 186 bars and for a minimum energy consumption of approximately 18.7 kWxd / t, which represents a gain in thermodynamic efficiency of 5.32% compared to the operating point 62 of the process according to the invention of figures 2-3 with a refrigerant gas composed of 100% nitrogen and a thermodynamic efficiency gain of 12.21% compared to the operating point 60 of the conventional process of the figure 1 .
- the method according to the invention uses either a mixture of nitrogen and neon, or of nitrogen and hydrogen, and despite its slightly lower yield, the use of the mixture of nitrogen and neon will be preferred, because neon is an inert gas, while hydrogen is combustible and remains dangerous and difficult to operate, especially at high pressure in installations confined on board a floating medium.
- hydrogen is a gas which percolates very easily through elastomeric seals and even in certain cases through metals, especially at very high pressure, and therefore the process according to the invention based on the use of a nitrogen-hydrogen mixture does not constitute the preferred version of the invention: the preferred version of the invention remains the use as refrigerant gas of a mixture of nitrogen and neon in the devices described with reference to the various figures.
- curve 75 represents the variation in the yield of a conventional process according to the figure 1 , or its variants, depending on the percentage of neon gas in the refrigerant gas.
- the operating point is at 70b, which corresponds to a maximum pressure P3 of approximately 63 bars and an energy consumption of approximately 20.45 kWxd / t, which represents a gain in efficiency thermodynamic of 3.76% compared to the operating point 60 of the same conventional process with a refrigerant gas composed of 100% nitrogen.
- the operating point is at 71b, which corresponds to a maximum pressure P3 of approximately 90 bars and an energy consumption of approximately 19.70 kWxd / t, which represents a gain in efficiency thermodynamic of 7.29% compared to the operating point 60 of the same conventional process with a refrigerant gas composed of 100% nitrogen.
- the operating point is at 72b, which corresponds to a maximum pressure P3 of approximately 120 bars and an energy consumption of approximately 19.35 kWxd / t, which represents a gain in efficiency thermodynamic of 8.94% compared to the operating point 60 of the same conventional process with a refrigerant gas composed of 100% nitrogen.
- the operating point is located at 80b, which corresponds to a maximum pressure P3 of approximately 68 bars and an energy consumption of approximately 20.2 kWxd / t, which represents a gain in thermodynamic efficiency of 4.94% compared to the point operation 60 of the same conventional process with a refrigerant gas composed of 100% nitrogen.
- the operating point is at 81b, which corresponds to a maximum pressure P3 of approximately 108 bars and an energy consumption of approximately 19.8 kWxd / t, which represents a gain of thermodynamic efficiency of 6.82% compared to the operating point 60 of the same conventional process with a refrigerant gas composed of 100% nitrogen.
- the operating point is located at 82b, which corresponds to a maximum pressure P3 of approximately 150 bars and an energy consumption of approximately 19 kWxd / t, which represents a gain of thermodynamic efficiency of 10.59% compared to the operating point 60 of the same conventional process with a refrigerant gas composed of 100% nitrogen.
- a conventional liquefaction unit is dimensioned in relation to the powers of the gas turbines available, high power turbines are commonly 25MW.
- the overall power is still 30MW, but in this case the efficiency of the assembly is improved and significantly reaches the value of 19.8 kW x day / t of LNG produced, which represents a gain of 6.59% for the same overall power of 30MW, compared to a power injection of 5MW at the level of the second motor M2, as detailed previously.
- Said power input of 5 MW to the first motor M1 then represents 16.6% of the overall power and said efficiency (19.8 kW x day / t) corresponds substantially to point W2 of the diagram of the figure 7 .
- the overall power is still 30MW, but in this case the efficiency of the assembly is improved and significantly reaches the value of 19.8 kW x day / t of LNG produced, which represents a gain of 6.59% for the same overall power of 30MW, compared to a power injection of 5MW at the level of the second motor M2, as detailed previously.
- Said power input of 5 MW to the first motor M1 then represents 16.6% of the overall power and said efficiency (19.8 kW x day / t) corresponds substantially to point W2 of the diagram of the figure 7 .
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Description
La présente invention est relative à un procédé de liquéfaction de gaz naturel pour produire du GNL, ou Gaz Naturel Liquéfié, appelé aussi LNG en anglais. Plus particulièrement encore, la présente invention est relative à la liquéfaction de gaz naturel comportant majoritairement du méthane, de préférence au moins 85% de méthane, les autres principaux constituants étant choisis parmi l'azote et des alcanes en C-2 à C-4 à savoir de l'éthane, du propane, du butane.The present invention relates to a process for liquefying natural gas to produce LNG, or Liquefied Natural Gas, also called LNG. More particularly still, the present invention relates to the liquefaction of natural gas mainly comprising methane, preferably at least 85% of methane, the other main constituents being chosen from nitrogen and C-2 to C-4 alkanes. namely ethane, propane, butane.
La présente invention concerne aussi une installation de liquéfaction disposée sur un navire ou un support flottant en mer, soit en mer ouverte, soit en zone protégée, telle un port, ou encore une installation à terre dans le cas de petites ou de moyennes unités de liquéfaction de gaz naturel.The present invention also relates to a liquefaction installation arranged on a ship or a floating support at sea, either in the open sea or in a protected area, such as a port, or even an onshore installation in the case of small or medium-sized vessels. liquefaction of natural gas.
Dans le cas d'installation disposée sur un navire, la présente invention est plus particulièrement relative à un procédé de re-liquéfaction de gaz à bord de navire de transport de GNL appelé « méthanier », ledit gaz à re-liquéfier étant le résultat du réchauffage et évaporation partielle du GNL contenu dans les cuves dudit navire, ledit gaz évaporé, en général majoritairement du méthane étant appelé en anglais « boil off ».In the case of an installation placed on a ship, the present invention relates more particularly to a process for re-liquefying gas on board an LNG transport ship called a “methane tanker”, said gas to be re-liquefied being the result of reheating and partial evaporation of the LNG contained in the tanks of said vessel, said evaporated gas, in general mainly methane, being called in English “boil off”.
Le gaz naturel à base de méthane est soit un sous-produit des champs pétroliers, produit en quantité faible ou moyenne, en général associé à du pétrole brut, soit un produit majeur dans le cas des champs de gaz, où il est alors en combinaison avec d'autres gaz, principalement des alcanes en C-2 à C-4, du CO2, de l'azote.Methane-based natural gas is either a by-product of oil fields, produced in small or medium quantities, usually associated with crude oil, or a major product in the case of gas fields, where it is then in combination with other gases, mainly C-2 to C-4 alkanes, CO2, nitrogen.
Lorsque le gaz naturel est associé en faible quantité à du pétrole brut, il est en général traité et séparé, puis utilisé sur place comme carburant dans des turbines ou des moteurs à piston pour produire de l'énergie électrique et des calories utilisées dans les processus de séparation ou de production.When natural gas is combined in small quantities with crude oil, it is usually processed and separated, then used on-site as fuel in turbines or piston engines to produce electrical energy and heat used in processes. separation or production.
Lorsque les quantités de gaz naturel sont importantes, voire considérables, on cherche à le transporter de manière à pouvoir les utiliser dans des régions éloignées, en général sur d'autres continents et, pour ce faire, la méthode préférée est de le transporter à l'état de liquide cryogénique (-165°C) sensiblement à la pression atmosphérique ambiante. Des navires de transport spécialisés appelés « méthaniers » possèdent des cuves de très grandes dimensions et présentant une isolation extrême de manière à limiter l'évaporation pendant le voyage.When the quantities of natural gas are large, even Considerations are being made to transport it so that it can be used in remote areas, usually on other continents, and to do this the preferred method is to transport it in the state of cryogenic liquid (-165 ° C ) substantially at ambient atmospheric pressure. Specialized transport vessels called "LNG carriers" have very large tanks with extreme insulation so as to limit evaporation during the voyage.
La liquéfaction du gaz en vue de son transport s'effectue en général à proximité du site de production, en général à terre, et nécessite des installations considérables pour atteindre des capacités de plusieurs millions de tonnes par an, les plus grosses unités existantes regroupent trois ou quatre unités de liquéfaction de 3-4 Mt par an de capacité unitaire.The liquefaction of gas for transport is generally carried out near the production site, generally on land, and requires considerable facilities to reach capacities of several million tonnes per year, the largest existing units grouping together three or four liquefaction units of 3-4 Mt per year of unit capacity.
Ce procédé de liquéfaction nécessite des quantités d'énergie mécanique considérables, l'énergie mécanique étant en général produite sur place en prélevant une partie du gaz pour produire l'énergie nécessaire au procédé de liquéfaction. Une partie du gaz est alors utilisé comme carburant dans des turbines à gaz, des turbines à vapeur ou des moteurs thermiques à pistons.This liquefaction process requires considerable amounts of mechanical energy, the mechanical energy being generally produced on site by taking part of the gas to produce the energy necessary for the liquefaction process. Part of the gas is then used as fuel in gas turbines, steam turbines or reciprocating heat engines.
De multiples cycles thermodynamiques ont été développés en vue d'optimiser le rendement énergétique global. Il existe deux types principaux de cycles. Un premier type basé sur la compression et la détente de fluide réfrigérant, avec changement de phase, et un second type basé sur la compression et la détente de gaz réfrigérant sans changement de phase. On appelle « fluide réfrigérant », ou « gaz réfrigérant », un gaz ou mélange de gaz, circulant en circuit fermé et subissant des phases de compression, le cas échéant de liquéfaction, puis des échanges de chaleur avec le milieu extérieur, puis ensuite des phases de détente, le cas échéant d'évaporation, et enfin des échanges de chaleur avec le gaz naturel à liquéfier comprenant du méthane, qui peu à peu se refroidit pour atteindre sa température de liquéfaction à pression atmosphérique, c'est à dire environ -165°C dans le cas du GNL.Multiple thermodynamic cycles have been developed in order to optimize the overall energy efficiency. There are two main types of cycles. A first type based on the compression and expansion of refrigerant fluid, with phase change, and a second type based on the compression and expansion of refrigerant gas without phase change. The term “refrigerant fluid” or “refrigerant gas” is used to refer to a gas or mixture of gases, circulating in a closed circuit and undergoing compression phases, where appropriate liquefaction, then heat exchanges with the external environment, then subsequently phases of expansion, where appropriate of evaporation, and finally of heat exchanges with the natural gas to be liquefied comprising methane, which gradually cools down to reach its liquefaction temperature at atmospheric pressure, i.e. approximately - 165 ° C in the case of LNG.
Ledit premier type de cycle, avec changement de phase, est en général utilisé sur des installations à terre et nécessite une grande quantité d'équipements et une emprise au sol considérable. De plus, les fluides réfrigérants, en général sous forme de mélanges, sont constitués de butane, de propane, d'éthane et de méthane, ces gaz étant dangereux car ils risquent, en cas de fuite, de provoquer des explosions ou des incendies considérables. Par contre, malgré la complexité des équipements requis, ils demeurent les plus efficaces et nécessitent une énergie de l'ordre de 0.3kWh par kg de GNL produit.Said first type of cycle, with phase change, is in general used on land installations and requires a large amount of equipment and a considerable footprint. In addition, refrigerant fluids, generally in the form of mixtures, consist of butane, propane, ethane and methane, these gases being dangerous because they risk, in the event of leakage, causing explosions or considerable fires. . On the other hand, despite the complexity of the equipment required, they remain the most efficient and require energy of the order of 0.3 kWh per kg of LNG produced.
De nombreuses variantes de ce premier type de procédé avec changement de phase du fluide réfrigérant ont été développées et chaque fournisseur de technologie ou d'équipements, possède sa formulation de mélanges, associée à des équipements spécifiques, tant pour les procédés dits « en cascade », que pour les procédés dits en « cycle mixte ». La complexité des installations provient du fait que dans les phases où le fluide réfrigérant se trouve à l'état liquide, et plus particulièrement au niveau des séparateurs et des conduites de raccordement, il convient d'installer des collecteurs gravitaires pour rassembler la phase liquide et la diriger au cœur des échangeurs thermiques où elle se vaporisera alors au contact du méthane à refroidir et à liquéfier, pour obtenir du GNL. Ces dispositifs sont très encombrants, mais ceci ne pose pas de problèmes dans le cas d'installations à terre, car il est en général simple de disposer d'une surface de terrain suffisante pour loger tous ces équipements encombrants les uns à côté des autres. Ainsi, pour les installations à terre, tous ces équipements de compression, d'échangeurs et de collecteurs sont en général installés les uns à côté des autres sur des surfaces considérables de 25 à 50 000m2, voire plus.Many variants of this first type of process with phase change of the refrigerant fluid have been developed and each supplier of technology or equipment has its own formulation of mixtures, associated with specific equipment, both for the so-called “cascade” processes. , than for the so-called “mixed cycle” processes. The complexity of the installations comes from the fact that in the phases where the refrigerant is in the liquid state, and more particularly at the level of the separators and the connecting pipes, it is necessary to install gravity collectors to bring together the liquid phase and direct it to the heart of the heat exchangers where it will then vaporize on contact with the methane to be cooled and liquefied, to obtain LNG. These devices are very bulky, but this does not pose any problems in the case of land-based installations, since it is generally easy to have a sufficient land area to accommodate all these bulky equipment one beside the other. Thus, for onshore installations, all these compression equipment, exchangers and collectors are generally installed next to each other over considerable areas of 25 to 50,000 m 2 , or even more.
Le second type de procédé de liquéfaction, procédé sans changement de phase du gaz réfrigérant, est un cycle de Brayton inversé, ou cycle de Claude utilisant un gaz tel l'azote. L'efficacité de ce second type est moindre, car il nécessite en général une énergie de l'ordre de 0.5 kWh/kg de GNL produit, soit environ 20.84 kW x jour/t et, par contre, il présente un avantage considérable en termes de sécurité, car le gaz réfrigérant du cycle, l'azote, est inerte, donc incombustible, ce qui est très intéressant lorsque les installations sont concentrées sur un espace réduit, par exemple sur le pont d'un support flottant installé en mer ouverte, lesdits équipements étant souvent installés sur plusieurs niveaux, les uns au-dessus des autres sur une surface réduite au strict minimum. Ainsi, en cas de fuite du gaz réfrigérant, il n'y a aucun danger d'explosion et il suffit alors de réinjecter dans le circuit la fraction de gaz réfrigérant perdue.The second type of liquefaction process, a process without phase change of the refrigerant gas, is an inverted Brayton cycle, or Claude cycle using a gas such as nitrogen. The efficiency of this second type is lower, because it generally requires an energy of the order of 0.5 kWh / kg of LNG produced, i.e. about 20.84 kW x day / t and, on the other hand, it has a considerable advantage in terms of safety, because the refrigerant gas of the cycle, nitrogen, is inert and therefore incombustible, which is very interesting when the installations are concentrated in a small space, for example on the deck of a floating support installed in the open sea, said equipment often being installed on several levels, one above the other on a small surface to the bare minimum. Thus, in the event of a refrigerant gas leak, there is no danger of explosion and it is then sufficient to reinject the lost refrigerant gas fraction into the circuit.
De plus, ce procédé de liquéfaction de gaz naturel sans changement de phase est très intéressant dans le cas de supports flottants, car, du fait de l'absence de phase liquide dans le gaz réfrigérant, les équipements sont de conception beaucoup plus simple. En effet, dans de telles installations, l'ensemble des équipements bouge quasiment en permanence au rythme des mouvements du support flottant (roulis, tangage, lacet, embardée, cavalement, pilonnement). Et la gestion d'un procédé avec changement de phase impliquant une phase liquide du fluide réfrigérant serait extrêmement délicate même pour des mouvements faibles du support flottant, voire quasiment impossible pour les mouvements extrêmes, alors que dans des installations fixes à terre le problème des mouvements ne se pose pas.In addition, this method of liquefying natural gas without phase change is very advantageous in the case of floating supports, because, due to the absence of a liquid phase in the refrigerant gas, the equipment is of much simpler design. In fact, in such installations, all of the equipment moves almost continuously to the rhythm of the movements of the floating support (roll, pitch, yaw, sheer, swing, heave). And the management of a process with phase change involving a liquid phase of the refrigerant would be extremely delicate even for weak movements of the floating support, or even almost impossible for extreme movements, whereas in fixed installations on land the problem of movements does not arise.
Malgré le rendement énergétique inférieur du procédé de liquéfaction sans changement de phase du gaz réfrigérant, ce dernier reste très intéressant car les équipements, principalement les compresseurs, les détendeurs, en des turbines, et les échangeurs sont beaucoup plus simples que les équipements requis pour un procédé de liquéfaction impliquant des cycles à changement de phase d'un fluide réfrigérant, tant en termes de technologie desdits équipements que de maintenance de ces équipements dans un environnement confiné, à savoir un support flottant ancré en mer. De plus, la conduite des installations en fonctionnement reste plus simple, car ce type de cycle est peu sensible aux variations de composition du gaz à liquéfier, à savoir un gaz naturel constitué d'un mélange où prédomine du méthane. En effet, dans le cas du cycle à changement de phase du fluide réfrigérant, pour que les rendements restent optimum, le fluide réfrigérant doit être adapté à la nature et composition du gaz à liquéfier et la composition du fluide réfrigérant doit le cas échéant être modifiée au cours du temps, en fonction de la composition du mélange de gaz naturel à liquéfier produit par le champ pétrolier.Despite the lower energy efficiency of the liquefaction process without phase change of the refrigerant gas, the latter remains very interesting because the equipment, mainly compressors, expansion valves, in turbines, and exchangers are much simpler than the equipment required for a liquefaction process involving phase change cycles of a refrigerant fluid, both in terms of technology of said equipment and maintenance of this equipment in a confined environment, namely a floating support anchored at sea. In addition, the operation of the installations operation remains simpler, because this type of cycle is insensitive to variations in the composition of the gas to be liquefied, namely a natural gas consisting of a mixture in which methane predominates. In fact, in the case of the phase change cycle of the refrigerant fluid, for the yields to remain optimum, the refrigerant must be adapted to the nature and composition of the gas to be liquefied. and the composition of the refrigerant fluid must, if necessary, be modified over time, depending on the composition of the mixture of natural gas to be liquefied produced by the oil field.
Dans son principe la mise en œuvre d'un cycle du procédé de liquéfaction sans changement de phase du gaz réfrigérant tel que de l'azote comporte les 4 éléments principaux suivants:
- un compresseur qui augmente la pression du gaz réfrigérant et le fait passer de la température ambiante à basse pression à une température élevée à haute pression,
- un échangeur de chaleur qui refroidit le gaz réfrigérant de la température élevée et haute pression sensiblement jusqu'à la température ambiante et haute pression,
- un dispositif de détente, en général une turbine de décompression, dans laquelle le gaz réfrigérant se détend : sa pression baisse et sa température est alors très basse ; tandis que, simultanément, on récupère au niveau de la turbine de détente l'énergie mécanique qui est alors en général directement réinjectée au niveau du compresseur qui lui est couplé,
- un échangeur cryogénique dans lequel circule d'un côté le gaz réfrigérant à température cryogénique, et de l'autre le gaz à liquéfier, ledit gaz réfrigérant absorbant les calories du gaz à liquéfier, donc se réchauffant, tandis que ledit gaz à liquéfier, cédant ses calories, se refroidit jusqu'à atteindre l'état liquide recherché. En fin de cycle de circulation, le gaz réfrigérant se trouve sensiblement à la température ambiante et il est alors réintroduit dans le compresseur pour effectuer un nouveau cycle en circuit fermé.
- a compressor which increases the pressure of the refrigerant gas and changes it from ambient temperature at low pressure to a high temperature at high pressure,
- a heat exchanger which cools the refrigerant gas from high temperature and high pressure substantially down to ambient temperature and high pressure,
- an expansion device, in general a decompression turbine, in which the refrigerant gas expands: its pressure drops and its temperature is then very low; while, simultaneously, the mechanical energy is recovered at the level of the expansion turbine, which is then generally directly reinjected at the level of the compressor which is coupled to it,
- a cryogenic exchanger in which circulates on one side the refrigerant gas at cryogenic temperature, and on the other the gas to be liquefied, said refrigerant gas absorbing the calories of the gas to be liquefied, therefore heating up, while said gas to be liquefied, yielding its calories, cools down to the desired liquid state. At the end of the circulation cycle, the refrigerant gas is approximately at ambient temperature and it is then reintroduced into the compressor to perform a new cycle in closed circuit.
Pendant toute la durée du cycle le gaz réfrigérant reste à l'état gazeux et circule de manière continue comme expliqué précédemment : il cède peu à peu des frigories, donc absorbe peu à peu des calories du gaz à liquéfier, à savoir un mélange constitué majoritairement de méthane et d'autres traces de gaz.Throughout the cycle, the refrigerant gas remains in the gaseous state and circulates continuously as explained previously: it gradually gives up frigories, therefore gradually absorbs calories from the gas to be liquefied, namely a mixture consisting mainly of of methane and other traces of gas.
La circulation du gaz à liquéfier se fait à contre-courant du gaz réfrigérant, c'est à dire que ledit gaz naturel comprenant du méthane, entre sensiblement à température ambiante dans l'échangeur au niveau de la sortie du gaz réfrigérant où ce dernier est alors sensiblement à la température ambiante. Puis, ledit gaz naturel comprenant du méthane progresse dans l'échangeur vers les zones plus froides et transfert ses calories au fluide réfrigérant : le gaz naturel comprenant du méthane se refroidit et le gaz réfrigérant se réchauffe. Au fur et à mesure de la progression du gaz naturel méthane dans l'échangeur, sa température baisse, puis en fin de parcours il se liquéfie et sa température continue à baisser jusqu'à atteindre la température de T3=-165°C pour un gaz contenant 85% de méthane.The circulation of the gas to be liquefied takes place against the current of the refrigerant gas, that is to say that said natural gas comprising methane enters substantially at ambient temperature into the exchanger at the level of the refrigerant gas outlet where the latter is then substantially at room temperature. Then, said natural gas comprising methane progresses through the exchanger towards the colder zones and transfers its calories to the refrigerant fluid: the natural gas comprising methane cools and the refrigerant gas heats up. As the natural gas methane progresses in the exchanger, its temperature drops, then at the end of its journey it liquefies and its temperature continues to drop until it reaches the temperature of T3 = -165 ° C for a gas containing 85% methane.
Pendant tout son parcours dans le ou les échangeurs de chaleur, la liquéfaction du gaz naturel se fait sous pression P0 de 5 à 50 bars, en général 10 à 20 bars, en quatre phases principales :
- phase 1 : refroidissement du gaz naturel depuis la température ambiante T0 jusqu'à T1= -50°C environ (cette température dépend de la composition du gaz naturel),
- phase 2 : liquéfaction du gaz naturel (passage de l'état gazeux à l'état liquide). Comme le gaz naturel est un mélange gazeux sous une pression P0 d'environ quelques dizaines de bars, ce changement d'état s'échelonne entre T1= -50°C et T2=-120°C environ,
- phase 3 : le gaz naturel une fois entièrement liquéfié (GNL) est alors à environ T2=-120°C, toujours sous une pression P0 d'environ quelques dizaines de bars. Au sein du ou des échangeurs, le GNL continue son refroidissement pour atteindre la température T3 de - 165°C, température correspondant à une phase liquide du GNL sous la pression atmosphérique,
- phase 4 : Le liquide obtenu ou GNL est alors dépressurisé jusqu'à la pression atmosphérique où il reste à l'état liquide en raison de sa température T3 inférieure ou égale à -165°C, et peut être transféré vers un réservoir de stockage isolé, ou le cas échéant chargé directement sur un navire de transport tel un méthanier.
- phase 1: cooling of natural gas from ambient temperature T0 to T1 = approximately -50 ° C (this temperature depends on the composition of the natural gas),
- phase 2: liquefaction of natural gas (transition from the gaseous state to the liquid state). As natural gas is a gaseous mixture under a pressure P0 of around a few tens of bars, this change of state ranges between T1 = -50 ° C and T2 = -120 ° C approximately,
- phase 3: once completely liquefied natural gas (LNG) is then at approximately T2 = -120 ° C, still under a pressure P0 of approximately a few tens of bars. Within the exchanger (s), the LNG continues to cool to reach the temperature T3 of - 165 ° C, a temperature corresponding to a liquid phase of the LNG under atmospheric pressure,
- phase 4: The liquid obtained or LNG is then depressurized to atmospheric pressure where it remains in the liquid state due to its temperature T3 less than or equal to -165 ° C, and can be transferred to an isolated storage tank , or if necessary loaded directly on a transport vessel such as an LNG carrier.
La phase 2 est la plus consommatrice en énergie, car il faut fournir au gaz toute l'énergie correspondant à sa chaleur latente de vaporisation. La phase 1 est un peu moins consommatrice en énergie, et la phase 3 est la moins consommatrice en énergie, par contre elle se fait aux températures les plus basses, c'est à dire aux environs de -165°C.
Les valeurs mentionnées ci-dessus pour T1, T2 et T3 sont adaptées à un gaz naturel constitué de 85% de méthane et 15% des dits autres composants azote et alcanes en C-2 à C-4, et peuvent varier sensiblement pour un gaz de composition différente.The values mentioned above for T1, T2 and T3 are suitable for a natural gas consisting of 85% methane and 15% of said other components nitrogen and C-2 to C-4 alkanes, and can vary significantly for a gas of different composition.
Sur la
Dans
- (a) circulation dudit gaz naturel à liquéfier circulant à une pression P0 supérieure ou égale à la pression atmosphérique, dans 3 échangeurs de chaleur cryogéniques disposés en série dont :
- un premier échangeur (101/5) dans lequel ledit gaz naturel entrant à une température T0 est refroidi et sort à une température T1 inférieure à T0, puis
- un deuxième échangeur (102/6) dans lequel le gaz naturel est entièrement liquéfié et sort à une température T2 inférieure à T1 et supérieure à T3, T3 étant inférieur à la température de liquéfaction du GNL, et
- un troisième échangeur (103/7) dans lequel ledit gaz naturel liquéfié est refroidi de T2 à T3, et
- (b) circulation à circuit fermé de deux flux de gaz réfrigérant à l'état gazeux dénommés premier et troisième flux respectivement à des pressions différentes P1 et P2, traversant deux dits échangeurs en contact indirect avec et à contre-courant du flux de gaz naturel, comprenant :
- un premier flux de gaz réfrigérant à une pression P1 inférieure à P3 traversant les 3 échangeurs entrant dans ledit troisième échangeur à une température T3' inférieure à T3, puis entrant à T2' inférieure à T2 dans ledit deuxième échangeur, puis entrant à T1' inférieure à T1 dans ledit premier échangeur et sortant dudit premier échangeur à une température T0' inférieure ou égale à T0, ledit premier flux de gaz réfrigérant à P1 et T3' étant obtenu par détente dans un premier détendeur (112/9) d'une première partie (122/16B) d'un deuxième flux de gaz réfrigérant (22/15) comprimé à la pression P3 supérieure à P2, ladite première partie de deuxième flux circulant en contact indirect avec et à co-courant dudit flux de gaz naturel, en entrant dans ledit premier échangeur à T0 et sortant dudit deuxième échangeur sensiblement à T2, et
- un troisième flux à une pression P2 supérieure à P1 et inférieure à P3 circulant en contact indirect avec et à co-courant dudit premier flux, traversant uniquement les dits deuxième et premier échangeurs, entrant dans ledit deuxième échangeur sensiblement à une température T2' et sortant dudit premier échangeur sensiblement à T0', ledit troisième flux de gaz réfrigérant à P2 et T2 étant obtenu par détente dans un deuxième détendeur (111/8) d'une deuxième partie (121/17) dudit deuxième flux de gaz réfrigérant (22/15) sortant dudit premier échangeur sensiblement à T1,
- (c) ledit deuxième flux de gaz réfrigérant comprimé à la pression P3 étant obtenu par compression par trois ou quatre compresseurs, et refroidissement desdits premier et troisième flux de gaz réfrigérant sortant du dit premier échangeur à P1 et respectivement P2.
- (a) circulation of said natural gas to be liquefied circulating at a pressure P0 greater than or equal to atmospheric pressure, in 3 cryogenic heat exchangers arranged in series, including:
- a first exchanger (101/5) in which said natural gas entering at a temperature T0 is cooled and exiting at a temperature T1 lower than T0, then
- a second exchanger (102/6) in which the natural gas is completely liquefied and leaves at a temperature T2 lower than T1 and higher than T3, T3 being lower than the liquefaction temperature of the LNG, and
- a third exchanger (103/7) in which said liquefied natural gas is cooled from T2 to T3, and
- (b) closed circuit circulation of two streams of refrigerant gas in the gaseous state called the first and third stream respectively at different pressures P1 and P2, passing through two said exchangers in indirect contact with and against the flow of the natural gas stream , comprising:
- a first flow of refrigerant gas at a pressure P1 lower than P3 passing through the 3 exchangers entering said third exchanger at a temperature T3 'lower than T3, then entering at T2' lower than T2 in said second exchanger, then entering at T1 'lower at T1 in said first exchanger and leaving said first exchanger at a temperature T0 'less than or equal to T0, said first flow of refrigerant gas at P1 and T3' being obtained by expansion in a first expansion valve (112/9) of a first part (122 / 16B) of a second flow of refrigerant gas (22/15) compressed at a pressure P3 greater than P2, said first part of the second flow circulating in indirect contact with and co-current with said flow of natural gas, entering said first exchanger at T0 and leaving said second exchanger substantially at T2, and
- a third flow at a pressure P2 greater than P1 and less than P3 circulating in indirect contact with and in co-current with said first flow, passing only through said second and first exchangers, entering said second exchanger at substantially a temperature T2 'and exiting of said first exchanger substantially at T0 ', said third flow of refrigerant gas at P2 and T2 being obtained by expansion in a second expansion valve (111/8) of a second part (121/17) of said second flow of refrigerant gas (22 / 15) leaving said first exchanger substantially at T1,
- (c) said second flow of refrigerant gas compressed to pressure P3 being obtained by compression by three or four compressors, and cooling said first and third flow of refrigerant gas leaving said first exchanger at P1 and P2 respectively.
Dans
Dans
Dans le compte-rendu de la
Le procédé décrit ci-dessus est avantageux par rapport à celui de la
Toutefois, dans le mode de réalisation de
Les niveaux de pression P1 et P2 des gaz sortant des turbines 112 et 111 sont différents et donc les débits de flux traversant les détendeurs 111 et 112 sont différents et notamment en pratique dans un rapport de 10-20% du débit total pour le débit du flux provenant du détendeur 112 contre 80-90% pour le débit du flux provenant du détendeur 111. Il en résulte que le compresseur 115b récupère seulement 10-20% de la puissance totale récupérée par rapport au 80-90% de puissance récupérée au niveau du compresseur 115a. Il résulte de cette disparité de puissance apportée aux deux compresseurs 115a et 115b montés en parallèle, une difficulté importante pour stabiliser le fonctionnement du circuit. En effet, le fonctionnement de deux compresseurs en parallèle peut conduire à des phénomènes de pompage, c'est-à-dire que l'un des compresseur prend le pas sur les autres en perturbant leurs pressions d'entrée et de sortie : il y a alors un risque de fonctionnement du ou des compresseurs de plus faible capacité en « mode turbine ». Ce mode de fonctionnement est à proscrire impérativement puisque toute ou partie du fluide tourne alors en boucle entre les compresseurs, l'un en mode compresseur, le ou les autres en « mode turbine » : le processus de compression se trouve alors radicalement perturbé, voire stoppé et le rendement global de l'installation s'effondre alors.The pressure levels P1 and P2 of the gases leaving the turbines 112 and 111 are different and therefore the flow rates passing through the regulators 111 and 112 are different and in particular in practice in a ratio of 10-20% of the total flow for the flow rate of the flow from expander 112 against 80-90% for the flow rate from expander 111. As a result, compressor 115b only recovers 10-20% of the total power recovered compared to 80-90% of power recovered at the level compressor 115a. This disparity in power supplied to the two compressors 115a and 115b mounted in parallel results in a major difficulty in stabilizing the operation of the circuit. Indeed, the operation of two compressors in parallel can lead to pumping phenomena, that is to say that one of the compressors takes precedence over the others by disturbing their inlet and outlet pressures: there is there is then a risk of the lower capacity compressor (s) operating in "turbine mode". This operating mode is to be avoided absolutely since all or part of the fluid then rotates in a loop between the compressors, one in compressor mode, the other or others in "turbine mode": the compression process is then radically disturbed, or even stopped and the overall efficiency of the installation then collapses.
La stabilisation du fonctionnement du circuit peut être réalisée classiquement au moyen de vannes de régulation en amont et/ou en aval desdits compresseurs 115a et 115b montés en parallèle, et/ou en amont et/ou en aval desdites turbines 111 et 112 pour contrôler les débits et fonctionnement des compresseurs. Toutefois, ces vannes de régulation engendrent des pertes des charges, donc d'énergie, ce qui affecte grandement le rendement global recherché et/ou la capacité de production de l'installation.Stabilization of the operation of the circuit can be carried out conventionally by means of control valves upstream and / or downstream of said compressors 115a and 115b mounted in parallel, and / or upstream and / or downstream of said turbines 111 and 112 to control the compressors flow rates and operation. However, these control valves generate pressure losses, and therefore energy, which affects greatly the desired overall efficiency and / or the production capacity of the installation.
Dans
Le but de la présente invention est de fournir un procédé de liquéfaction de gaz naturel du type sans changement de phase du gaz réfrigérant apte à être installé sur un navire ou support flottant qui présente un rendement énergétique amélioré, à savoir une énergie totale consommée dans le procédé minimale en termes de kWh pour obtenir 1 tonne de GNL et/ou qui, présente des transferts thermiques dans les échangeurs accru et/ou qui permette de mettre en œuvre une installation de liquéfaction plus compacte et plus efficace.The aim of the present invention is to provide a process for the liquefaction of natural gas of the type without phase change of the refrigerant gas capable of being installed on a ship or floating support which has improved energy efficiency, namely a total energy consumed in the tank. minimum process in terms of kWh to obtain 1 tonne of LNG and / or which exhibits increased heat transfers in the exchangers and / or which makes it possible to implement a more compact and efficient liquefaction installation.
Pour ce faire, la présente invention fournit un procédé de liquéfaction d'un gaz naturel comprenant majoritairement du méthane, de préférence, au moins 85% de méthane, les autres composants comprenant essentiellement de l'azote et des alcanes en C-2 à C-4, dans lequel on liquéfie ledit gaz naturel à liquéfier par circulation dudit gaz naturel à une pression P0 supérieure ou égale à la pression atmosphérique (Patm.), de préférence P0 étant supérieure à la pression atmosphérique, dans au moins 1 échangeur de chaleur cryogénique (EC1, EC2, EC3) par circulation en circuit fermé à contre-courant en contact indirect avec au moins un flux de gaz réfrigérant restant à l'état gazeux comprimé à une pression P1 entrant dans ledit échangeur cryogénique à une température T3' inférieure à T3, T3 étant la température en sortie dudit échangeur cryogénique, et T3 étant inférieure ou égale à la température de liquéfaction du dit gaz naturel liquéfié à la pression atmosphérique, dans lequel on liquéfie ledit gaz naturel à liquéfier en réalisant les étapes concomitantes suivantes de :
- (a) circulation dudit gaz naturel à liquéfier circulant à une pression P0 supérieure ou égale à la pression atmosphérique, de préférence P0 étant supérieure à la pression atmosphérique, dans au moins 3 échangeurs de chaleur cryogéniques disposés en série dont :
- un premier échangeur dans lequel ledit gaz naturel entrant à une température T0 est refroidi et sort à une température T1 inférieure à T0, puis
- un deuxième échangeur dans lequel le gaz naturel est entièrement liquéfié et sort à une température T2 inférieure à T1 et supérieure à T3, et
- un troisième échangeur dans lequel ledit gaz naturel liquéfié est refroidi de T2 à T3, et
- (b) circulation à circuit fermé d'au moins deux flux de gaz réfrigérant à l'état gazeux dénommés premier et troisième flux respectivement à des pressions différentes P1 et P2, traversant au moins deux dits échangeurs en contact indirect avec et à contre-courant du flux de gaz naturel, comprenant :
- un premier flux de gaz réfrigérant à une pression P1 inférieure à P3 traversant les 3 échangeurs entrant dans ledit troisième échangeur à une température T3' inférieure à T3, puis entrant à T2' inférieure à T2 dans ledit deuxième échangeur, puis entrant à T1' inférieure à T1 dans ledit premier échangeur et sortant dudit premier échangeur à une température T0' inférieure ou égale à T0, ledit premier flux de gaz réfrigérant à P1 et T3' étant obtenu par détente dans au moins un premier détendeur d'une première partie d'un deuxième flux de gaz réfrigérant comprimé à la pression P3 supérieure à P2, ledit deuxième flux circulant en contact indirect avec et à co-courant dudit flux de gaz naturel, en entrant dans ledit premier échangeur à T0 et ladite première partie dudit deuxième flux sortant dudit deuxième échangeur sensiblement à T2, et
- un troisième flux à une pression P2 supérieure à P1 et inférieure à P3 circulant en contact indirect avec et à co-courant dudit premier flux, traversant uniquement les dits deuxième et premier échangeurs, entrant dans ledit deuxième échangeur sensiblement à une température T2' et sortant dudit premier échangeur sensiblement à T0', ledit troisième flux de gaz réfrigérant à P2 et T2 étant obtenu par détente dans un deuxième détendeur d'une deuxième partie dudit deuxième flux de gaz réfrigérant sortant dudit premier échangeur sensiblement à T1, le débit D2 de ladite deuxième partie de deuxième flux étant de préférence supérieur au débit D1 de la première partie de deuxième flux,
- (c) ledit deuxième flux de gaz réfrigérant comprimé à la pression P3 étant obtenu par compression par au moins deux compresseurs et refroidissement desdits premier et troisième flux de gaz réfrigérant sortant du dit premier échangeur à P1 et respectivement P2, un premier compresseur comprimant de P1 à P2 la totalité du dit premier flux de gaz réfrigérant sortant dudit premier échangeur, et au moins un deuxième compresseur, comprimant de P2 à au moins P'3, P'3 étant une pression inférieure ou égale à P3 et supérieure à P2, d'une part ledit troisième flux de gaz réfrigérant sortant à P2 du dit premier échangeur et d'autre part ledit premier flux de gaz réfrigérant comprimé à P2 sortant dudit premier compresseur, pour obtenir ledit deuxième flux de gaz réfrigérant à P3 et T0 après refroidissement, ledit deuxième compresseur étant monté en série avec ledit premier compresseur, caractérisé en ce que :
- les deux premier et deuxième compresseurs disposés en série sont couplés auxdits premier et respectivement deuxième détendeurs consistant en des turbines de récupération d'énergie, et
- au moins le dit premier compresseur est couplé à un premier moteur, et permet de moduler et contrôler spécifiquement la valeur de pression P2 en apportant une puissance différentiée audit premier compresseur par rapport à la puissance apportée aux autres compresseurs, et
- au moins une turbine à gaz est couplée
- soit audit deuxième compresseur, celui-ci comprimant ledit deuxième flux de gaz réfrigérant directement à P3,
- soit, à un troisième compresseur monté en série après le deuxième compresseur, le dit troisième compresseur comprimant de P'3 à P3 ledit deuxième flux de gaz réfrigérant,
- ledit premier moteur apportant au moins 3% de la puissance totale apportée à l'ensemble desdits compresseurs mis en œuvre, ladite turbine à gaz fournissant de 97 à 70% de la puissance totale apportée à l'ensemble des dits compresseurs mis en œuvre.
- (a) circulation of said natural gas to be liquefied circulating at a pressure P0 greater than or equal to atmospheric pressure, from preferably P0 being greater than atmospheric pressure, in at least 3 cryogenic heat exchangers arranged in series, including:
- a first exchanger in which said natural gas entering at a temperature T0 is cooled and exiting at a temperature T1 lower than T0, then
- a second exchanger in which the natural gas is completely liquefied and leaves at a temperature T2 lower than T1 and higher than T3, and
- a third exchanger in which said liquefied natural gas is cooled from T2 to T3, and
- (b) closed circuit circulation of at least two streams of refrigerant gas in the gaseous state called first and third stream respectively at different pressures P1 and P2, passing through at least two said exchangers in indirect contact with and against the current natural gas flow, comprising:
- a first flow of refrigerant gas at a pressure P1 lower than P3 passing through the 3 exchangers entering said third exchanger at a temperature T3 'lower than T3, then entering at T2' lower than T2 in said second exchanger, then entering at T1 'lower at T1 in said first exchanger and leaving said first exchanger at a temperature T0 'less than or equal to T0, said first flow of refrigerant gas at P1 and T3' being obtained by expansion in at least a first regulator of a first part of a second flow of refrigerant gas compressed at a pressure P3 greater than P2, said second flow circulating in indirect contact with and co-current with said flow of natural gas, entering said first exchanger at T0 and said first part of said second outgoing flow of said second exchanger substantially at T2, and
- a third flow at a pressure P2 greater than P1 and less than P3 circulating in indirect contact with and co-current with said first flow, passing only through said second and first exchangers, entering said second exchanger substantially at a temperature T2 'and leaving said first exchanger substantially at T0', said third flow of refrigerant gas at P2 and T2 being obtained by expansion in a second pressure regulator of a second part of said second flow of refrigerant gas leaving said first exchanger substantially at T1, the flow rate D2 of said second part of the second flow being preferably greater than the flow rate D1 of the first part of the second flow,
- (c) said second flow of refrigerant gas compressed to pressure P3 being obtained by compression by at least two compressors and cooling of said first and third flow of refrigerant gas leaving said first exchanger at P1 and P2 respectively, a first compressor compressing from P1 at P2 the entire said first flow of refrigerant gas leaving said first exchanger, and at least one second compressor, compressing from P2 to at least P'3, P'3 being a pressure less than or equal to P3 and greater than P2, d 'on the one hand said third flow of refrigerant gas leaving at P2 from said first exchanger and on the other hand said first flow of refrigerant gas compressed at P2 leaving said first compressor, to obtain said second flow of refrigerant gas at P3 and T0 after cooling, said second compressor being mounted in series with said first compressor, characterized in that:
- the two first and second compressors arranged in series are coupled to said first and respectively second expansion valves consisting of energy recovery turbines, and
- at least said first compressor is coupled to a first motor, and makes it possible to modulate and specifically control the pressure value P2 by providing a differentiated power to said first compressor with respect to the power supplied to the other compressors, and
- at least one gas turbine is coupled
- either to said second compressor, the latter compressing said second flow of refrigerant gas directly to P3,
- or, to a third compressor mounted in series after the second compressor, said third compressor compressing said second flow of refrigerant gas from P'3 to P3,
- said first motor providing at least 3% of the total power supplied to all of said compressors used, said gas turbine supplying from 97 to 70% of the total power supplied to all of said compressors used.
Dans la présente description, on entend par « compresseur couplé à un détendeur/turbine ou moteur » ou encore « compresseur actionné par un moteur » (ou vice versa un « détendeur/turbine ou moteur couplé au compresseur ») que l'arbre de sortie de la turbine ou respectivement du moteur entraine l'arbre d'entrée du compresseur, c'est-à-dire, transfère une énergie mécanique à l'arbre du compresseur. Il s'agit donc d'un couplage mécanique du compresseur au détendeur/turbine ou respectivement du compresseur au moteur.In the present description, the term “compressor coupled to an expansion valve / turbine or engine” or “compressor actuated by an engine” (or vice versa a “expansion valve / turbine or engine coupled to the compressor”) is understood to mean that the output shaft of the turbine or respectively of the engine drives the input shaft of the compressor, that is to say, transfers mechanical energy to the shaft of the compressor. It is therefore a mechanical coupling of the compressor to the expansion valve / turbine or respectively of the compressor to the engine.
Plus particulièrement, ledit moteur peut être soit un moteur thermique, soit de préférence un moteur électrique, ou toute autre installation capable de fournir de l'énergie mécanique au gaz réfrigérant ; et les compresseurs sont du type rotatif à turbine, encore dénommé compresseur centrifuge.More particularly, said motor can be either a heat engine, or preferably an electric motor, or any other installation capable of supplying mechanical energy to the refrigerant gas; and the compressors are of the rotary turbine type, also called a centrifugal compressor.
De préférence, après l'étape (a) on dépressurise le gaz naturel liquéfié sortant dudit troisième échangeur à T3, depuis la pression P0 à la pression atmosphérique le cas échéant.Preferably, after step (a), the liquefied natural gas leaving said third exchanger is depressurized at T3, from pressure P0 to atmospheric pressure where appropriate.
Le procédé selon l'invention est avantageux par rapport au procédé décrit dans
D'autre part, dans la présente invention, l'essentiel de la puissance apportée auxdits compresseurs est injecté au niveau des deuxième et/ou troisième compresseurs comprimant le flux de gaz réfrigérant à haute pression P'3/P3 et la récupération d'énergie au niveau des premier et deuxième détendeurs est réinjectée au niveau des premier et deuxième compresseurs, comprimant les gaz réfrigérants circulant à basse et moyenne pression P1 et P2. En effet, la fraction de fluide traversant le compresseur C1 représente une faible fraction du débit total (par exemple 10-15%) et l'énergie nécessaire est du même ordre de grandeur que l'énergie récupérée par la turbine E1. Il est donc intéressant de coupler les deux. De plus un ajout contrôlé de puissance en C1 permet d'améliorer le rendement énergétique du système en pilotant P1 et P2 indépendamment l'une de l'autre.On the other hand, in the present invention, most of the power supplied to said compressors is injected at the level of the second and / or third compressors compressing the flow of refrigerant gas at high pressure P'3 / P3 and the recovery of energy. at the level of the first and second expansion valves is reinjected at the level of the first and second compressors, compressing the refrigerant gases circulating at low and medium pressure P1 and P2. Indeed, the fraction of fluid passing through the compressor C1 represents a small fraction of the total flow (for example 10-15%) and the energy required is of the same order of magnitude as the energy recovered by the turbine E1. It is therefore interesting to combine the two. Moreover, a controlled addition of power in C1 makes it possible to improve the energy efficiency of the system by controlling P1 and P2 independently of one another.
D'autre part, la plus grande part de la puissance apportée aux compresseurs est injectée dans les compresseurs fournissant la plus grande pression (P'3, P3), ce qui permet d'augmenter la capacité de production du procédé, tout en améliorant son rendement énergétique.On the other hand, most of the power supplied to the compressors is injected into the compressors supplying the greatest pressure (P'3, P3), which makes it possible to increase the production capacity of the process, while improving its performance. energy efficiency.
En outre, la mise en oeuvre desdits premier et deuxième compresseurs en série couplés à desdits premier et deuxièmes détendeurs selon la présente invention permet aussi d'améliorer la compacité de l'installation ce qui est particulièrement avantageux pour la mise en œuvre d'un procédé à bord d'un support flottant où la place est limitée.In addition, the implementation of said first and second compressors in series coupled to said first and second expansion valves according to the present invention also makes it possible to improve the compactness of the installation, which is particularly advantageous for the implementation of a process. aboard a floating support where space is limited.
Le procédé selon l'invention en référence aux
D'autre part, le procédé selon l'invention est avantageux par rapport à
Ainsi, selon une caractéristique originale de la présente invention, on fait varier de façon contrôlée ladite pression P2 en apportant de la puissance de façon contrôlée audit premier compresseur avec le dit premier moteur, de manière à ce que l'énergie consommée pour la mise en œuvre du procédé (Ef) soit minimale, de préférence lorsque la composition du gaz naturel à liquéfier varie.Thus, according to an original characteristic of the present invention, said pressure P2 is varied in a controlled manner by supplying power in a controlled manner to said first compressor with said first motor, so that the energy consumed for switching on. implementation of the process (Ef) is minimal, preferably when the composition of the natural gas to be liquefied varies.
Ce procédé est plus particulièrement avantageux car il permet ainsi, en modulant et contrôlant spécifiquement la valeur de la pression P2 dudit troisième flux, de modifier et optimiser le point de fonctionnement du procédé, à savoir minimiser l'énergie consommée et donc augmenter le rendement notamment lorsque, comme cela arrive en cours d'exploitation, la composition du gaz naturel à liquéfier varie.This process is more particularly advantageous because it thus makes it possible, by modulating and specifically controlling the value of the pressure P2 of said third flow, to modify and optimize the operating point of the process, namely to minimize the energy consumed and therefore to increase the efficiency in particular. when, as happens during operation, the composition of the natural gas to be liquefied varies.
Selon l'invention, ledit premier moteur apporte au moins 3%, de préférence de 3 à 30% de la puissance totale apportée à l'ensemble des dits compresseurs mis en œuvre, la dite turbine à gaz fournissant de 97 à 70% de la puissance totale apportée.According to the invention, said first motor provides at least 3%, preferably from 3 to 30% of the total power supplied to all of said compressors used, said gas turbine providing 97 to 70% of the power. total power supplied.
Plus particulièrement encore, on observe que lorsque l'on augmente la puissance injectée au niveau dudit premier moteur, la pression P1 reste sensiblement constante, la pression P2 augmente et le rendement augmente, c'est à dire que la consommation en énergie exprimée en kW x jour/t diminue, jusqu'à atteindre un minimum, puis en augmentant encore la puissance apportée par ledit moteur, notamment au-delà de 30% de la puissance totale, ladite consommation en énergie augmente à nouveau.More particularly still, it is observed that when the power injected into said first motor is increased, the pressure P1 remains substantially constant, the pressure P2 increases and the efficiency increases, that is to say that the energy consumption expressed in kW x day / t decreases, until a minimum is reached, then by further increasing the power supplied by said engine, in particular beyond 30% of the total power, said energy consumption increases again.
Une unité de liquéfaction conventionnelle est dimensionnée par rapport aux puissances des turbines à gaz disponibles, les turbines de forte puissance étant couramment de 25MW, voire 30MW lorsqu'elles sont destinées à être installées sur un support flottant. Les turbines à gaz fixes installées à terre peuvent atteindre des puissances maximales de 90-100MW.A conventional liquefaction unit is dimensioned in relation to the power of the gas turbines available, high power turbines commonly being 25MW, or even 30MW when they are intended to be installed on a floating support. Fixed gas turbines installed on land can reach maximum powers of 90-100MW.
On cherche en général à augmenter la puissance de l'installation, et il est alors possible d'installer en parallèle deux turbines à gaz identiques pour obtenir une puissance double, mais on alors deux lignes de machines tournantes, ce qui augmente les encombrements, les quantités de conduites et bien sûr les coûts.In general, we seek to increase the power of the installation, and it is then possible to install two identical gas turbines in parallel to obtain double power, but we then have two lines of rotating machines, which increases the dimensions, the quantities of pipes and of course the costs.
En installant une seule turbine GT de n MW et en rajoutant de la puissance inférieure à n MW au niveau d'un dit deuxième moteur M2, le fonctionnement du procédé est identique en termes de rendement à celui utilisant deux turbines à gaz de n MW en parallèle.By installing a single GT turbine of n MW and adding power of less than n MW at the level of a said second motor M2, the operation of the process is identical in terms of efficiency to that using two gas turbines of n MW in parallel.
Ainsi, l'ajout de puissance au niveau du deuxième moteur M2, de préférence grâce à une motorisation électrique, donne plus de souplesse au fonctionnement et permet ainsi un accroissement de puissance. En revanche le rendement de l'ensemble reste inchangé.Thus, the addition of power at the level of the second motor M2, preferably by virtue of an electric motor, gives more flexibility in operation and thus allows an increase in power. On the other hand, the yield of the whole remains unchanged.
Si par contre, on fournit la même puissance au niveau du premier moteur M1, la puissance globale est toujours la même, mais dans ce cas le rendement de l'ensemble est amélioré, ce qui représente un gain d'énergie consommée pour la même puissance globale, par rapport à une injection de puissance au niveau du deuxième moteur M2.If, on the other hand, the same power is supplied to the level of the first motor M1, the overall power is always the same, but in this case the efficiency of the assembly is improved, which represents a gain in energy consumed for the same power. overall, relative to a power injection at the second engine M2.
Ainsi, en fonction de la production de gaz naturel, tant en quantité qu'en qualité, en provenance des nappes souterraines, on utilisera avantageusement une turbine à gaz GT, par exemple de 25MW, à plein régime en permanence que l'on complètera, voire le cas échéant modulera, par :
- injection de puissance au niveau de la turbine GT ou du deuxième moteur M2 sans changer le rendement global, et/ou
- injection de puissance au niveau du premier moteur M1 ce qui a pour effet d'améliorer le rendement global, jusqu'à atteindre un optimum, c'est à dire un minimum de consommation d'énergie.
- power injection at the GT turbine or second motor M2 without changing the overall efficiency, and / or
- power injection at the level of the first motor M1 which has the effect of improving the overall efficiency, until an optimum is reached, ie a minimum of energy consumption.
Dans une première variante de réalisation du procédé, on met en œuvre deux compresseurs montés en série, comprenant :
- (i) ledit premier compresseur couplé audit premier détendeur, comprimant de P1 à P2 la totalité du dit premier flux de gaz réfrigérant sortant dudit premier échangeur, et
- (ii) ledit deuxième compresseur couplé audit deuxième détendeur, comprimant de P2 à au moins P'3, P'3 étant supérieure à P2 et inférieure ou égale à P3, d'une part ledit troisième flux de gaz réfrigérant sortant à P2 du dit premier échangeur, et d'autre part ledit premier flux de gaz réfrigérant comprimé à P2 sortant dudit premier compresseur, pour obtenir ledit deuxième flux de gaz réfrigérant à P3 et T0 après refroidissement, et
- iii) ledit premier compresseur est actionné par ledit premier moteur, ledit deuxième compresseur étant actionné par au moins ladite turbine à gaz.
- (i) said first compressor coupled to said first expander, compressing from P1 to P2 all of said first flow of refrigerant gas exiting from said first exchanger, and
- (ii) said second compressor coupled to said second expansion valve, compressing from P2 to at least P'3, P'3 being greater than P2 and less than or equal to P3, on the one hand said third flow of refrigerant gas exiting at P2 from said first exchanger, and on the other hand said first flow of refrigerant gas compressed at P2 leaving said first compressor, to obtain said second flow of refrigerant gas at P3 and T0 after cooling, and
- iii) said first compressor is operated by said first engine, said second compressor being operated by at least said gas turbine.
Cette première variante de réalisation est avantageuse en ce qu'elle permet en œuvre une installation la plus compacte en termes d'encombrement à bord du support flottant.This first variant embodiment is advantageous in that it allows for the most compact installation in terms of size on board the floating support.
Dans une deuxième variante de réalisation, on met en œuvre trois compresseurs montés en série, comprenant :
- (i) ledit premier compresseur actionné par ledit premier moteur et couplé audit premier détendeur, comprimant de P1 à P2 la totalité du dit premier flux de gaz réfrigérant sortant dudit premier échangeur, et
- (ii) ledit deuxième compresseur actionné par un deuxième moteur et couplé audit deuxième détendeur, comprimant de P2 à P'3, P'3 étant supérieur à P2 et inférieure à P3, d'une part ledit troisième flux de gaz réfrigérant sortant à P2 du dit premier échangeur, et d'autre part ledit premier flux de gaz réfrigérant comprimé à P2 sortant dudit premier compresseur, et
- (iii) ledit troisième compresseur actionné par ladite turbine à gaz pour fournir la majeure partie de l'énergie et comprimer de P'3 à P3 la totalité des premier et troisième flux de gaz réfrigérant comprimés par le deuxième compresseur, pour obtenir ledit deuxième flux de gaz réfrigérant à P3 et T0 après refroidissement, et
- (iv) ledit premier moteur apporte au moins 3%, de préférence encore de 3 à 30% de la puissance totale apportée à l'ensemble des dits compresseurs mis en œuvres, la turbine à gaz couplée au dit troisième compresseur, ainsi que ledit deuxième moteur couplé au deuxième compresseur fournissant ensemble de 97 à 70% de la puissance totale apportée à l'ensemble des dits compresseurs mis en œuvre.
- (i) said first compressor actuated by said first motor and coupled to said first expander, compressing from P1 to P2 all of said first flow of refrigerant gas exiting from said first exchanger, and
- (ii) said second compressor actuated by a second motor and coupled to said second expander, compressing from P2 to P'3, P'3 being greater than P2 and less than P3, on the one hand said third flow of refrigerant gas exiting at P2 said first exchanger, and on the other hand said first flow of refrigerant gas compressed to P2 leaving said first compressor, and
- (iii) said third compressor actuated by said gas turbine to supply the major part of the energy and compress from P'3 to P3 all of the first and third streams of refrigerant gas compressed by the second compressor, to obtain said second stream refrigerant gas at P3 and T0 after cooling, and
- (iv) said first engine provides at least 3%, more preferably from 3 to 30% of the total power supplied to all of said compressors implemented, the gas turbine coupled to said third compressor, as well as said second motor coupled to the second compressor together providing 97 to 70% of the total power supplied to all of said compressors used.
Cette deuxième variante de réalisation est avantageuse en termes de rendement thermodynamique et de capacité de production car on peut utiliser alors avantageusement comme turbine à gaz une turbine de capacité maximale disponible sur le marché, c'est-à-dire 25-30MW dans le cas de turbines destinées à être installées sur un support flottant, plus un deuxième moteur électrique par exemple de 5 à 10 MW relié au deuxième compresseur, la puissance globale des deuxième moteur et troisième moteur (turbine à gaz) étant alors de 30 à 40MW, donc largement supérieure à celle des turbine à gaz les plus grosses disponibles sur le marché et destinées à des supports flottants. Avantageusement, le deuxième moteur peut être lui aussi une turbine à gaz, de préférence de puissance identique à la turbine à gaz principale, ce qui permet alors d'atteindre une puissance globale de 50 à 60MW.This second variant embodiment is advantageous in terms of thermodynamic efficiency and production capacity since a maximum capacity turbine available on the market can then be used advantageously as a gas turbine, that is to say 25-30MW in the case of gas turbine. turbines intended to be installed on a floating support, plus a second electric motor, for example from 5 to 10 MW, connected to the second compressor, the overall power of the second motor and third motor (gas turbine) then being 30 to 40MW, therefore vastly superior to that of the largest gas turbines available on the market and intended for floating supports. Advantageously, the second engine can also be a gas turbine, preferably of identical power to the main gas turbine, which then makes it possible to achieve an overall power of 50 to 60 MW.
Le procédé selon l'invention permet, en faisant varier la pression P2 par apport d'énergie audit premier compresseur à l'aide dudit premier moteur, de mettre en œuvre une énergie totale Ef minimale consommée dans le procédé inférieur à 21.5 kW x jour/t, plus particulièrement de 18.5 à 20.5 kW x jour/t de gaz liquéfié produit.The method according to the invention makes it possible, by varying the pressure P2 by supplying energy to said first compressor using said first motor, to implement a minimum total energy Ef consumed in the method of less than 21.5 kW x day / t, more particularly from 18.5 to 20.5 kW x day / t of liquefied gas produced.
D'une manière générale, on fonctionnera avec une turbine à gaz GT à plein régime, que l'on complètera par un apport de puissance au niveau du premier moteur M1, ledit apport étant limité à moins de 30% de la puissance globale de manière à optimiser le rendement à la valeur minimale de 18.5 à 21.5 kW x jour/t, puis en cas de nécessité, on augmentera la puissance globale par injection de puissance au niveau du deuxième moteur M2, et concomitamment on réajustera la puissance injectée au niveau du premier moteur M1, de manière à ce que ladite puissance soit toujours sensiblement égale à moins de 30% de la puissance globale de manière à conserver le rendement de l'installation à la valeur optimale de 18.5 à 21.5 kW x jour/t.In general, we will operate with a gas turbine GT at full speed, which will be completed by a power supply to the first engine M1, said input being limited to less than 30% of the overall power so to optimize the output to the minimum value of 18.5 to 21.5 kW x day / t, then if necessary, the overall power will be increased by power injection at the level of the second motor M2, and concomitantly the power injected at the level of the engine will be readjusted first motor M1, so that said power is always substantially equal to less than 30% of the overall power so as to keep the efficiency of the installation at the optimum value of 18.5 to 21.5 kW x day / t.
Ledit rendement optimal de 19.75 kW x jour/t pour une puissance du premier moteur M1 représentant 24% de la puissance totale est valable pour un fluide réfrigérant constitué de 100% d'azote. Dans le cas d'autres gaz tels que n éon ou hydrogène ou de mélanges azote-néon ou azote-hydrogène, le rendement optimal ainsi que le pourcentage de puissance varient de 18.5 à 21.5 kW x jour/t en fonction du gaz ou du mélange et des pourcentages de néon ou d'hydrogène, mais les avantages détaillés précédemment restent valables et même se cumulent.Said optimum efficiency of 19.75 kW x day / t for a power of the first motor M1 representing 24% of the total power is valid for a coolant consisting of 100% nitrogen. In the case of other gases such as neon or hydrogen or nitrogen-neon or nitrogen-hydrogen mixtures, the optimum efficiency as well as the power percentage vary from 18.5 to 21.5 kW x day / t depending on the gas or the mixture and percentages of neon or hydrogen, but the advantages detailed previously remain valid and even accumulate.
Plus particulièrement, ledit gaz réfrigérant comprend de l'azote.More particularly, said refrigerant gas comprises nitrogen.
Dans une variante de réalisation, ledit gaz réfrigérant consiste en un gaz unique choisi parmi l'azote, l'hydrogène et le néon.In an alternative embodiment, said refrigerant gas consists of a single gas chosen from nitrogen, hydrogen and neon.
De préférence, le néon est préféré au regard des risque d'explosion plus important de l'hydrogène et du fait que l'hydrogène peut présenter une certaine propension à percoler à travers les joints en élastomères et même à travers les parois métalliques de faible épaisseur.Preferably, neon is preferred in view of the greater explosion risk of hydrogen and the fact that hydrogen may have a certain propensity to percolate through elastomeric seals and even through low metal walls. thickness.
Selon d'autres caractéristiques particulières :
- la composition du gaz naturel à liquéfier est comprise dans les fourchettes suivantes pour un total de 100% :
Méthane de 80 à 100%,- azote de 0 à 20 %
- éthane de 0 à 20%
propane de 0 à 20 %, etbutane de 0 à 20 % ; et- les températures suivantes :
- T0 et T0' sont de 10 à 35 °C (température en AA), et
- T3 et T3' sont de -160 à -170°C (température en DD), et
- T2 et T2' sont de -100 à - 140°C (température en CC), et
- T1 et T1' sont de -30 à -70°C (température en CC) ;
- the composition of the natural gas to be liquefied is included in the following ranges for a total of 100%:
- 80 to 100% methane,
- nitrogen from 0 to 20%
- ethane from 0 to 20%
- propane from 0 to 20%, and
- butane from 0 to 20%; and
- the following temperatures:
- T0 and T0 'are 10 to 35 ° C (temperature in AA), and
- T3 and T3 'are from -160 to -170 ° C (temperature in DD), and
- T2 and T2 'are from -100 to - 140 ° C (temperature in CC), and
- T1 and T1 'are -30 to -70 ° C (temperature in CC);
Pour les pressions suivantes :
- P0 est de 0.5 à 5 MPa (5 à 50 bars), et
- P1 est de 0.5 à 5 MPa, et
- P2 est de 1 à 10 MPa (10 à 100bars), et
- P3 est de 5 à 20 MPa (50 à 200bars).
- P0 is 0.5 to 5 MPa (5 to 50 bars), and
- P1 is 0.5 to 5 MPa, and
- P2 is 1 to 10 MPa (10 to 100 bars), and
- P3 is 5 to 20 MPa (50 to 200 bars).
La présente invention fournit également une installation embarquée sur un navire ou support flottant pour mettre en œuvre un procédé selon l'invention caractérisé en ce qu'elle comprend :
- au moins 3 dits échangeurs de chaleur cryogéniques en série comprenant au moins :
- un premier conduit de circulation à contre-courant apte à faire circuler un premier flux de gaz réfrigérant à l'état gazeux comprimés à P1 traversant à contre-courant successivement les 3 troisième, deuxième et premier échangeurs,
- un deuxième conduit de circulation à co-courant apte à faire circuler un dit deuxième flux de gaz réfrigérant à l'état gazeux comprimé à P3 traversant à co-courant uniquement successivement les dits premier et deuxième échangeurs,
- un troisième conduit de circulation à contre-courant du dit gaz réfrigérant apte à la circulation circuler un dit troisième flux de gaz réfrigérant à l'état gazeux comprimé à P2 traversant à contre-courant uniquement successivement les dits deuxième et premier échangeurs,
- un quatrième conduit apte à faire circuler ledit gaz naturel à liquéfier traversant successivement les 3 premier, deuxième et troisième échangeurs,
- un premier détendeur entre la sortie dudit deuxième conduit et l'entrée dudit premier conduit,
- un deuxième détendeur entre (i) une dérivation dudit deuxième conduit située entre les dits premier et deuxième échangeur et (ii) l'entrée dudit troisième conduit, et
- un premier compresseur à la sortie dudit premier conduit couplé à une turbine constituant ledit premier détendeur,
- un deuxième compresseur à la sortie du dit deuxième conduit couplé à une turbine constituant ledit deuxième détendeur, ledit deuxième compresseur étant monté en série avec ledit premier compresseur, notamment en sortie dudit premier compresseur, et
- un conduit de circulation de la totalité du gaz comprimé à P2 par le premier compresseur vers le deuxième compresseur ainsi monté en série dudit premier compresseur, et
- au moins un premier moteur couplé audit premier compresseur, apte à apporter au moins 3%, de préférence 3 à 30% de la puissance totale apportée à l'ensemble desdits compresseurs mis en œuvre, et
- une turbine à gaz couplée soit audit deuxième compresseur, celui-ci comprimant ledit deuxième flux de gaz réfrigérant directement à P3, soit à un troisième compresseur monté en série après le deuxième compresseur, ledit troisième compresseur comprimant de P3' à P3 ledit deuxième flux de gaz réfrigérant; et
- ladite turbine à gaz fournissant de 97 à 70% de la puissance totale apportée à l'ensemble des dits compresseurs mis en œuvre.
- at least 3 said cryogenic heat exchangers in series comprising at least:
- a first counter-current circulation duct capable of circulating a first flow of refrigerant gas in the gaseous state compressed at P1 passing through the 3 third, second successively and first interchange,
- a second co-current circulation duct able to circulate a said second flow of refrigerant gas in the gaseous state compressed at P3 passing through only successively said first and second exchangers in co-current,
- a third countercurrent circulation duct of said refrigerant gas suitable for circulation to circulate a said third flow of refrigerant gas in the gaseous state compressed at P2 passing through countercurrently only successively said second and first exchangers,
- a fourth conduit capable of circulating said natural gas to be liquefied passing successively through the first, second and third exchangers,
- a first pressure regulator between the outlet of said second duct and the inlet of said first duct,
- a second regulator between (i) a bypass of said second duct located between said first and second exchanger and (ii) the inlet of said third duct, and
- a first compressor at the outlet of said first duct coupled to a turbine constituting said first expander,
- a second compressor at the outlet of said second duct coupled to a turbine constituting said second expansion valve, said second compressor being mounted in series with said first compressor, in particular at the outlet of said first compressor, and
- a conduit for circulating all of the gas compressed at P2 by the first compressor to the second compressor thus mounted in series with said first compressor, and
- at least a first motor coupled to said first compressor, capable of providing at least 3%, preferably 3 to 30% of the total power supplied to all of said compressors used, and
- a gas turbine coupled either to said second compressor, the latter compressing said second flow of refrigerant gas directly to P3, or to a third compressor mounted in series after the second compressor, said third compressor compressing from P3 'to P3 said second flow of refrigerant gas; and
- said gas turbine supplying from 97 to 70% of the total power supplied to all of said compressors used.
Plus particulièrement encore, une dite installation comprend seulement deux compresseurs montés en série, comprenant :
- (i) ledit premier compresseur couplé audit premier détendeur, apte à comprimer de P1 à P2 la totalité du dit premier flux de gaz réfrigérant sortant dudit premier échangeur, et
- (ii) ledit deuxième compresseur couplé audit deuxième détendeur, apte à comprimer de P2 à P3, d'une part ledit troisième flux de gaz réfrigérant sortant à P2 du dit premier échangeur et d'autre part ledit premier flux de gaz réfrigérant comprimé à P2 sortant dudit premier compresseur, pour obtenir ledit deuxième flux de gaz réfrigérant à P3 et T0 après refroidissement, et
- (iii) ledit premier moteur couplé au dit premier compresseur, et ladite turbine à gaz couplée au dit deuxième compresseur, ledit premier moteur étant apte à apporter au moins 3%, de préférence encore de 3 à 30% de la puissance totale apportée à l'ensemble des dits compresseurs mis en oeuvre, et
- (iv) ladite turbine à gaz couplée audit deuxième compresseur étant apte à fournir de 97 à 70% de la puissance totale apportée.
- (i) said first compressor coupled to said first expander, capable of compressing from P1 to P2 all of said first flow of refrigerant gas leaving said first exchanger, and
- (ii) said second compressor coupled to said second expansion valve, capable of compressing from P2 to P3, on the one hand said third flow of refrigerant gas leaving at P2 from said first exchanger and on the other hand said first flow of compressed refrigerant gas at P2 leaving said first compressor, to obtain said second flow of refrigerant gas at P3 and T0 after cooling, and
- (iii) said first motor coupled to said first compressor, and said gas turbine coupled to said second compressor, said first motor being able to provide at least 3%, more preferably from 3 to 30% of the total power supplied to it. 'all of the said compressors used, and
- (iv) said gas turbine coupled to said second compressor being able to deliver from 97 to 70% of the total power supplied.
Plus particulièrement encore, une installation selon l'invention comprend :
seulement trois compresseurs montés en série comprenant :
- (i) ledit premier compresseur couplé audit premier détendeur et au dit premier moteur, et
- (ii) ledit deuxième compresseur couplé audit deuxième détendeur et à un dit deuxième moteur, et
- (iii) ledit troisième compresseur couplé à ladite turbine à gaz apte à fournir la majeure partie de l'énergie et apte à comprimer à P3 la totalité des premier et troisième flux de gaz réfrigérant comprimés par ledit deuxième compresseur, pour obtenir ledit troisième flux de gaz réfrigérant à P3 et T0 après refroidissement, et
- (iv) ledit premier moteur étant apte à apporter au moins 3%, de préférence encore de 3 à 30% de la puissance totale apportée à l'ensemble des dits compresseurs mis en œuvres, la turbine à gaz couplée au dit troisième compresseur, ainsi que ledit deuxième moteur couplé au deuxième compresseur étant apte à fournir ensemble de 97 à 70% de la puissance totale apportée à l'ensemble des dits compresseurs mis en oeuvre.
only three compressors mounted in series comprising:
- (i) said first compressor coupled to said first expander and to said first motor, and
- (ii) said second compressor coupled to said second expansion valve and to a said second motor, and
- (iii) said third compressor coupled to said gas turbine capable of supplying the major part of the energy and capable of compressing to P3 all of the first and third streams of refrigerant gas compressed by said second compressor, to obtain said third stream of refrigerant gas at P3 and T0 after cooling, and
- (iv) said first motor being able to provide at least 3%, more preferably from 3 to 30% of the total power supplied to all of said compressors used, the gas turbine coupled to said third compressor, thus that said second motor coupled to the second compressor being able to supply together from 97 to 70% of the total power supplied to all of said compressors used.
D'autres caractéristiques et avantages de la présente invention apparaîtront à la lumière de la description détaillée de différents modes de réalisation qui va suivre, en référence aux figures suivantes.
- la
figure 1 représente le diagramme d'un procédé standard de liquéfaction à double boucle utilisant l'azote comme gaz réfrigérant, - la
figure 2 représente le diagramme d'un procédé de liquéfaction selon l'invention à triple boucle utilisant l'azote ou un mélange comportant de l'azote comme gaz réfrigérant, dans une version dite « équilibrée », - la
figure 3 représente le diagramme d'un procédé de liquéfaction selon l'invention à triple boucle utilisant l'azote ou un mélange comportant de l'azote comme gaz réfrigérant, dans une version dite « compacte », - la
figure 4 représente un diagramme de refroidissement et de liquéfaction d'un gaz naturel dans le cadre d'un procédé de liquéfaction selon l'invention représentant l'enthalpie du gaz naturel et du fluide réfrigérant (kJ/kg) en fonction de la température de T0 à T3, - les
figures 5 et5A représentent des diagrammes de l'énergie totale consommée (Ef) en kW x jour par tonne de GNL produit (kW x jour/t) d'un procédé de liquéfaction selon l'invention utilisant un mélange d'azote et de néon comme gaz réfrigérant, en fonction de la pression P1 et des divers pourcentages en néon dudit mélange, - les
figures 5 et5B représentent des diagrammes l'énergie totale consommée (Ef) kW x jour/t de GNL produit d'un procédé de liquéfaction selon l'invention utilisant un mélange d'azote et d'hydrogène comme gaz réfrigérant, en fonction de la pression P1 et des divers pourcentages en hydrogène dudit mélange, - la
figure 6A représente un diagramme de l'énergie totale consommée (Ef) en kW x jour/t de GNL produit d'un procédé de liquéfaction selon l'invention utilisant un mélange d'azote et de néon comme gaz réfrigérant en fonction de la pression P2 et divers pourcentages en néon dudit mélange, - la
figure 6B représente des diagrammes de l'énergie totale consommée (Ef) en kW x jour/t de GNL produit d'un procédé de liquéfaction selon l'invention utilisant un mélange d'azote et d'hydrogène comme gaz réfrigérant, en fonction de la pression P2 et divers pourcentages en hydrogène dudit mélange, - la
figure 7 représente un diagramme de l'énergie totale consommée (Ef) en kW x jour/t de GNL produit de GNL produit dans un procédé de liquéfaction de la technique antérieure (60) et d'un procédé de liquéfaction selon l'invention, utilisant de l'azote comme gaz réfrigérant selon le niveau de la pression P3, - la
figure 7A représente un diagramme de l'énergie totale consommée (Ef) en kW x jour/t de GNL produit d'un procédé de liquéfaction selon l'invention utilisant un mélange d'azote et de néon comme gaz réfrigérant en fonction de la pression P3 et divers pourcentages en néon dudit mélange, - la
figure 7B représente un diagramme de l'énergie totale consommée (Ef) en kW x jour/t de GNL produit d'un procédé de liquéfaction selon l'invention utilisant un mélange d'azote et d'hydrogène comme gaz réfrigérant en fonction de la pression P3 et divers pourcentages en hydrogène dudit mélange.
- the
figure 1 represents the diagram of a standard double loop liquefaction process using nitrogen as refrigerant gas, - the
figure 2 represents the diagram of a triple-loop liquefaction process according to the invention using nitrogen or a mixture comprising nitrogen as refrigerant gas, in a so-called “balanced” version, - the
figure 3 represents the diagram of a triple-loop liquefaction process according to the invention using nitrogen or a mixture comprising nitrogen as refrigerant gas, in a so-called “compact” version, - the
figure 4 represents a diagram of cooling and liquefaction of a natural gas in the context of a liquefaction process according to the invention representing the enthalpy of natural gas and of the refrigerant fluid (kJ / kg) as a function of the temperature from T0 to T3, - the
figures 5 and5A represent energy diagrams total consumed (Ef) in kW x day per tonne of LNG produced (kW x day / t) of a liquefaction process according to the invention using a mixture of nitrogen and neon as refrigerant gas, as a function of the pressure P1 and the various neon percentages of said mixture, - the
figures 5 and5B represent diagrams the total energy consumed (Ef) kW x day / t of LNG produced from a liquefaction process according to the invention using a mixture of nitrogen and hydrogen as refrigerant gas, as a function of the pressure P1 and various percentages of hydrogen in said mixture, - the
figure 6A represents a diagram of the total energy consumed (Ef) in kW x day / t of LNG produced from a liquefaction process according to the invention using a mixture of nitrogen and neon as refrigerant gas as a function of the pressure P2 and various neon percentages of said mixture, - the
figure 6B represents diagrams of the total energy consumed (Ef) in kW x day / t of LNG produced from a liquefaction process according to the invention using a mixture of nitrogen and hydrogen as refrigerant gas, as a function of the pressure P2 and various percentages of hydrogen of said mixture, - the
figure 7 represents a diagram of the total energy consumed (Ef) in kW x day / t of LNG produced from LNG produced in a prior art liquefaction process (60) and a liquefaction process according to the invention, using nitrogen as refrigerant gas according to the pressure level P3, - the
figure 7A represents a diagram of the total energy consumed (Ef) in kW x day / t of LNG produced from a liquefaction process according to the invention using a mixture of nitrogen and neon as refrigerant gas as a function of the pressure P3 and various neon percentages of said mixture, - the
figure 7B represents a diagram of the total energy consumed (Ef) in kW x day / t of LNG produced from a liquefaction process according to the invention using a mixture of nitrogen and hydrogen as refrigerant gas as a function of the pressure P3 and various percentages of hydrogen of said mixture.
Sur la
Des échangeurs de ce type sont connus de l'homme de l'Art et commercialisés par les sociétés LINDE (France) ou FIVE Cryogénie (France). Ainsi, tous les circuits d'un échangeur cryogénique sont en contact thermique les uns avec les autres pour échanger des calories, mais les fluides qui y circulent ne se mélangent pas. Chacun des circuits est dimensionné pour présenter un minimum de pertes de charges au débit maximal de fluide réfrigérant et une résistance suffisante pour résister à la pression dudit fluide réfrigérant existant dans la boucle concernée.Exchangers of this type are known to those skilled in the art and marketed by the companies LINDE (France) or FIVE Cryogénie (France). Thus, all the circuits of a cryogenic exchanger are in thermal contact with each other to exchange calories, but the fluids which circulate therein do not mix. Each of the circuits is dimensioned to have a minimum of pressure drops at the maximum flow rate of refrigerant fluid and sufficient resistance to withstand the pressure of said refrigerant fluid existing in the loop concerned.
De manière conventionnelle, un détendeur réalise une chute de pression d'un fluide ou d'un gaz et est représenté par un trapèze symétrique, dont la petite base représente l'entrée 10a (haute pression), et la grande base représente la sortie 10b (basse pression) comme illustré sur la
De la même manière, et de manière conventionnelle, un compresseur augmente la pression d'un gaz et est représenté par un trapèze symétrique, dont la grande base représente l'entrée 11a (basse pression), et la petite base représente la sortie 11b (haute pression) comme illustré sur la
Le gaz naturel circule dans le circuit Sg et entre en AA dans le premier échangeur cryogénique EC1 à une température T0, supérieure ou sensiblement égale à la température ambiante, et T1=-50°C environ. Dans cet échangeur EC1, le gaz naturel se refroidit, mais reste à l'état de gaz. Puis il passe en BB dans l'échangeur cryogénique EC2 dont la température est comprise entre T1=-50°C environ et T2=-120°C environ.The natural gas circulates in the circuit Sg and enters at AA in the first cryogenic exchanger EC1 at a temperature T0, greater than or substantially equal to the ambient temperature, and T1 = -50 ° C approximately. In this exchanger EC1, the natural gas cools, but remains in the gas state. Then it passes to BB in the cryogenic exchanger EC2, the temperature of which is between T1 = approximately -50 ° C and T2 = approximately -120 ° C.
Dans cet échangeur EC2, la totalité du gaz naturel se liquéfie en GNL à une température de T2=-120°C environ, puis le GNL passe en CC dans l'échangeur cryogénique EC3. Dans cet échangeur EC3, le GNL est refroidi jusqu'à la température de T3=-165°C ce qui permet d'évacuer le GNL en partie basse en DD, puis de le dépressuriser en EE pour enfin le stocker liquide à la pression atmosphérique ambiante, c'est à dire à une pression absolue de 1 bar environ (soit environ 0.1MPa). Tout au long de ce parcours du gaz naturel dans le circuit Sg dans les divers échangeurs, le gaz naturel se refroidit en cédant des calories au gaz réfrigérant, lequel se réchauffe alors et doit subir de manière permanente un cycle thermodynamique complet pour pouvoir extraire de manière continue des calories au gaz naturel entrant en AA.In this exchanger EC2, all of the natural gas liquefies into LNG at a temperature of T2 = -120 ° C approximately, then the LNG passes to CC in the cryogenic exchanger EC3. In this EC3 exchanger, the LNG is cooled to a temperature of T3 = -165 ° C which allows the LNG to be discharged in the lower part in DD, then to depressurize it in EE to finally store it liquid at atmospheric pressure. ambient, that is to say at an absolute pressure of approximately 1 bar (i.e. approximately 0.1 MPa). Throughout this natural gas journey in the Sg circuit in the various exchangers, the natural gas cools by releasing calories to the refrigerant gas, which then heats up and must permanently undergo a complete thermodynamic cycle in order to be able to extract in a manner continues natural gas calories entering AA.
Ainsi, le parcours du gaz naturel est représenté sur la gauche du PFD, et ledit gaz circule du haut vers le bas dans le circuit Sg, la température étant décroissante du haut vers le bas, depuis une température T0 sensiblement ambiante en haut en AA, jusqu'à une température T3 d'environ -165°C en bas en DD.Thus, the path of natural gas is represented on the left of the PFD, and said gas flows from top to bottom in the circuit Sg, the temperature decreasing from top to bottom, from a substantially ambient temperature T0 at the top in AA, to a temperature T3 of about -165 ° C at the bottom in DD.
Sur la partie droite du PFD, on a représenté le cycle thermodynamique du gaz réfrigérant à double boucle correspondant aux circuits S1 et S2. Pour la clarté des explications, les niveaux de pression dans les principaux circuits sont représentés en trait fin pour la basse pression (P1 dans le circuit S1), en trait moyen pour la pression intermédiaire (P2), et en trait fort pour la haute pression (P3 dans le circuit S2).On the right side of the PFD, there is shown the thermodynamic cycle of the double-loop refrigerant gas corresponding to circuits S1 and S2. For clarity of explanation, the pressure levels in the main circuits are shown in thin lines for low pressure (P1 in circuit S1), in medium lines for intermediate pressure (P2), and in solid lines for high pressure (P3 in circuit S2).
Dans un schéma classique représenté sur la
L'installation est composé de :
- un moteur, en général une turbine à gaz GT qui actionne le compresseur C3 et fournit l'intégralité de la puissance mécanique,
- de 3 compresseurs :
- C3 qui comprime l'intégralité du flux de réfrigérant,
- C2 qui est accouplé à la turbine E2 et qui comprime la portion D'2 du flux total D, et
- C1 qui est accouplé à la turbine E1 et qui comprime la portion complémentaire D'1 du flux total D,
de 2 turbines,- E2 couplé en direct sur le compresseur C2, et qui détend la portion D2 du flux total D, depuis la haute pression P3 jusqu'à la basse pression P1,
- E1 couplé en direct sur le compresseur C1, et qui détend la portion D1 du flux total D, depuis la haute pression P3 jusqu'à la basse pression P1,
- d'un échangeur cryogénique en trois parties ou 3 échangeurs en série EC1, EC2 et EC3, correspondant respectivement aux
phase 1,phase 2 et phase 3 de la liquéfaction, comportant trois circuits, respectivement SG (gaz naturel) et S1-S2 (gaz réfrigérant), - de deux refroidisseurs au minimum, H1 et H2, situés respectivement en sortie du compresseur principal C3 (H1) et sur la boucle haute pression (H2), avant l'entrée dans les échangeurs cryogéniques.
- an engine, generally a gas turbine GT which drives the compressor C3 and provides all of the mechanical power,
- of 3 compressors:
- C3 which compresses the entire flow of refrigerant,
- C2 which is coupled to the turbine E2 and which compresses the portion D'2 of the total flow D, and
- C1 which is coupled to the turbine E1 and which compresses the complementary portion D'1 of the total flow D,
- 2 turbines,
- E2 coupled directly to compressor C2, and which expands portion D2 of total flow D, from high pressure P3 to low pressure P1,
- E1 coupled directly to compressor C1, and which expands portion D1 of total flow D, from high pressure P3 to low pressure P1,
- a cryogenic exchanger in three parts or 3 exchangers in series EC1, EC2 and EC3, corresponding respectively to
phase 1,phase 2 and phase 3 of liquefaction, comprising three circuits, respectively SG (natural gas) and S1-S2 (gas refrigerant), - at least two coolers, H1 and H2, located respectively at the outlet of the main compressor C3 (H1) and on the high pressure loop (H2), before entering the cryogenic exchangers.
Un refroidisseur H1, H2 peut être constitué d'un échangeur à eau, par exemple un échangeur à eau de mer ou de rivière ou air froid du type ventilo convecteur ou tour de refroidissement, telle que celles utilisées dans les centrales nucléaires.A chiller H1, H2 can consist of a water exchanger, for example a sea or river water or cold air exchanger of the fan coil or cooling tower type, such as those used in nuclear power plants.
Plus précisément sur la
- (a) circulation dudit gaz naturel à liquéfier circulant Sg à une pression P0 supérieure ou égale à la pression atmosphérique (Patm), de préférence P0 étant supérieure à la pression atmosphérique, dans 3 échangeurs de chaleur cryogéniques EC1,EC2, et EC3 disposés en série dont :
- un premier échangeur EC1 dans lequel ledit gaz naturel entrant à une température T0 est refroidi et sort BB à une température T1 inférieure à T0 à laquelle tous les composants dudit gaz naturel sont encore à l'état gazeux, puis
- un deuxième échangeur EC2 dans lequel le gaz naturel est entièrement liquéfié et sort en CC à une température T2 inférieure à T1, et
- un troisième échangeur EC3 dans lequel ledit gaz naturel liquéfié est refroidi de T2 à T3, T3 étant inférieure à T2 et T3 étant inférieure ou égale à la température de liquéfaction dudit gaz naturel à pression atmosphérique, et
- (b) circulation en circuit fermé à contre-courant d'un premier flux S1 de gaz réfrigérant à l'état gazeux comprimé à une pression P1 inférieure à P3 en contact indirect avec et à contre-courant du flux de gaz naturel Sg, ledit premier flux S1 à une pression P1 traversant les 3 échangeurs EC3, EC2, et EC1 entrant en DD dans ledit troisième échangeur EC3 à une température T3' inférieure à T3 puis sortant dudit troisième échangeur et entrant dans ledit deuxième échangeur EC2 en CC à une température T2' inférieure à T2, puis sortant du deuxième échangeur et entrant dans le premier échangeur EC1 en BB à une température T1' inférieure à T1 et sortant en AA dudit premier échangeur EC1 à une température T0' inférieure ou égale à T0,
- ledit premier flux S1 de gaz réfrigérant à P1 et T3' étant obtenu par détente dans un premier détendeur E1 d'une première partie D1 d'un deuxième flux S2 de gaz réfrigérant comprimé à P3 supérieure à P1 circulant à co-courant dudit gaz naturel entrant en AA dans ledit premier échangeur EC1 à T0 et sortant CC dudit deuxième échangeur EC2 sensiblement à T2, et
- une deuxième partie D2 dudit deuxième flux S2 de gaz réfrigérant comprimé P3 circulant à co-courant dudit gaz naturel entrant en AA dans ledit premier échangeur EC1 à T0 et sortant dudit premier échangeur sensiblement à T1 est détendue dans un deuxième détendeur E2 à ladite pression P1 et à une dite température T2', et est recyclée pour rejoindre ledit premier flux à l'entrée en CC dudit deuxième échangeur, et
- (c) ledit deuxième flux S2 comprimé à P3 est obtenu par compression par trois compresseurs C1, C2, et C3 suivi d'au moins deux refroidissements H1 et H2 dudit premier flux S1 de gaz réfrigérant recyclé sortant en AA du dit premier échangeur EC1, par un premier compresseur C1 couplé audit premier détendeur E1, et
- (d) après l'étape (a) on dépressurise le gaz naturel liquéfié depuis la pression P0 à la pression atmosphérique.
- (a) circulation of said natural gas to be liquefied circulating Sg at a pressure P0 greater than or equal to atmospheric pressure (Patm), preferably P0 being greater than atmospheric pressure, in 3 cryogenic heat exchangers EC1, EC2, and EC3 arranged in series including:
- a first exchanger EC1 in which said natural gas entering at a temperature T0 is cooled and exits BB at a temperature T1 below T0 at which all the components of said natural gas are still in the gaseous state, then
- a second exchanger EC2 in which the natural gas is completely liquefied and leaves in CC at a temperature T2 lower than T1, and
- a third exchanger EC3 in which said liquefied natural gas is cooled from T2 to T3, T3 being less than T2 and T3 being less than or equal to the liquefaction temperature of said natural gas at atmospheric pressure, and
- (b) circulation in a closed circuit against the current of a first flow S1 of refrigerant gas in the gaseous state compressed at a pressure P1 less than P3 in indirect contact with and against the current of the flow of natural gas Sg, said first flow S1 at a pressure P1 passing through the 3 exchangers EC3, EC2, and EC1 entering at DD in said third exchanger EC3 at a temperature T3 'lower than T3 then leaving said third exchanger and entering said second exchanger EC2 at DC at a temperature T2 'less than T2, then leaving the second exchanger and entering the first exchanger EC1 at BB at a temperature T1' lower than T1 and exiting at AA from said first exchanger EC1 at a temperature T0 'less than or equal to T0,
- said first flow S1 of refrigerant gas at P1 and T3 'being obtained by expansion in a first regulator E1 of a first part D1 of a second flow S2 of refrigerant gas compressed at P3 greater than P1 circulating in co-current with said natural gas entering at AA in said first exchanger EC1 to T0 and leaving CC from said second exchanger EC2 substantially at T2, and
- a second part D2 of said second stream S2 of compressed refrigerant gas P3 circulating in co-current with said natural gas entering at AA in said first exchanger EC1 at T0 and leaving said first exchanger substantially at T1 is expanded in a second expansion valve E2 at said pressure P1 and at a said temperature T2 ', and is recycled to join said first flow at the DC inlet of said second exchanger, and
- (c) said second stream S2 compressed at P3 is obtained by compression by three compressors C1, C2, and C3 followed by at least two coolings H1 and H2 of said first stream S1 of recycled refrigerant gas leaving at AA from said first exchanger EC1, by a first compressor C1 coupled to said first expansion valve E1, and
- (d) after step (a), the liquefied natural gas is depressurized from pressure P0 to atmospheric pressure.
Plus précisément, sur la
- un troisième compresseur C3 actionné par un moteur de préférence une turbine à gaz GT pour comprimer de P1 à P'3, P'3 étant compris entre P1 et P3, la totalité du premier flux de gaz réfrigérant provenant de la sortie en AA dudit premier échangeur EC1, et
- un premier compresseur C1 couplé au premier détendeur E1 consistant en une turbine, pour comprimer de P2 à P'3, une partie D1' dudit premier flux de gaz réfrigérant, comprimé par le troisième compresseur C3, et
- un deuxième compresseur C2 couplé au deuxième détendeur E2 consistant en une turbine, pour comprimer de P'3 à P3 une partie D2' dudit premier flux de gaz réfrigérant comprimé par le troisième compresseur C3.
- a third compressor C3 actuated by an engine, preferably a gas turbine GT for compressing from
P 1 to P'3, P'3 being between P1 and P3, all of the first flow of refrigerant gas coming from the outlet at AA of said first exchanger EC1, and - a first compressor C1 coupled to the first expansion valve E1 consisting of a turbine, for compressing from P2 to P'3, a part D1 'of said first flow of refrigerant gas, compressed by the third compressor C3, and
- a second compressor C2 coupled to the second expansion valve E2 consisting of a turbine, for compressing from P'3 to P3 a part D2 'of said first flow of refrigerant gas compressed by the third compressor C3.
Dans la
Le gaz réfrigérant en sortie haute en AA du circuit S1, au niveau de l'échangeur EC1 a un débit D : il est à la basse pression P1 et à une température T'0 sensiblement inférieure à T0 et à la température ambiante. Il est alors comprimé en C3 à la pression P'3 puis passe à travers un refroidisseur H1. Le fluide de débit D est alors séparé en deux partie de débits D1' et D2' qui alimentent respectivement les compresseurs C1 (D1') et C2 (D2') opérant en parallèle. Les deux flux à la pression P3 sont ensuite rassemblés puis refroidis sensiblement jusqu'à la température ambiante T0 en passant dans le refroidisseur H2. Ce flux global D entre alors dans le haut de l'échangeur cryogénique EC1 au niveau du circuit S2, puis à la sortie du premier niveau, en BB, un large partie du flux de débit D2 (D2 supérieure à D1) est extraite et dirigée vers la turbine E2 couplée au compresseur C2. Le reste du flux D1 traverse le deuxième étage de l'échangeur cryogénique EC2, puis au niveau CC est dirigé vers la turbine E1 couplée au compresseur C1.The refrigerant gas at the high outlet in AA of the circuit S1, at the level of the exchanger EC1 has a flow rate D: it is at low pressure P1 and at a temperature T'0 substantially lower than T0 and at ambient temperature. It is then compressed at C3 to pressure P'3 then passes through a cooler H1. The flow rate fluid D is then separated into two parts of flow rates D1 'and D2' which respectively supply the compressors C1 (D1 ') and C2 (D2') operating in parallel. The two streams at pressure P3 are then combined and then cooled substantially to ambient temperature T0 by passing through cooler H2. This overall flow D then enters the top of the cryogenic exchanger EC1 at the level of the circuit S2, then at the exit of the first level, in BB, a large part of the flow rate D2 (D2 greater than D1) is extracted and directed. to the turbine E2 coupled to the compressor C2. The rest of the flow D1 passes through the second stage of the cryogenic exchanger EC2, then to the level CC is directed to the turbine E1 coupled to the compressor C1.
A la sortie de la turbine E1 le gaz réfrigérant, à une température T3' inférieure à T3=-165°C, est alors dirigé vers le bas de l'échangeur cryogénique EC3 dans le circuit S1 et remonte à contre-courant du gaz à liquéfier circulant dans le circuit Sg, dont il assure la phase finale 3 de la liquéfaction.At the outlet of the turbine E1, the refrigerant gas, at a temperature T3 'lower than T3 = -165 ° C, is then directed towards the bottom of the cryogenic exchanger EC3 in the circuit S1 and goes up against the current of the gas at liquefy circulating in the circuit Sg, of which it ensures the final phase 3 of the liquefaction.
Le flux D2 de gaz réfrigérant en provenance de la turbine E2 est à une pression P1 et température T2 d'environ -120°C et est recombiné au sein du circuit S1 au flux D1 en provenance de la turbine E1 au niveau de la sortie supérieure de l'échangeur cryogénique EC3 en CC.The flow D2 of refrigerant gas coming from the turbine E2 is at a pressure P1 and temperature T2 of about -120 ° C and is recombined within the circuit S1 to the flow D1 coming from the turbine E1 at the upper outlet. of the cryogenic exchanger EC3 in CC.
La séparation du deuxième flux S2 en deux parties de débits différents D1 et D2 en sortie BB du premier échangeur, de préférence avec D2 supérieur à D1, est avantageuse car l'essentiel de l'énergie consommée se produit dans la phase 2 au sein du deuxième échangeur EC2. Ainsi seule une partie mineure de débit D1 traverse le troisième échangeur EC3 où se produit la phase 3, tandis que le flux total D=D1+D2 du circuit S1 traverse alors l'échangeur cryogénique EC2 pour assurer la phase 2 de la liquéfaction (température de T1= -50°C à T2= -120°C).The separation of the second flow S2 into two parts of different flow rates D1 and D2 at the outlet BB of the first exchanger, preferably with D2 greater than D1, is advantageous because most of the energy consumed occurs in
Le même flux D du circuit S1 traverse enfin l'échangeur cryogénique EC1 pour assurer la phase 1 du processus de liquéfaction (température de T1= -50°C à T0= température ambiante). A la sortie supérieure de l'échangeur cryogénique EC1, le flux D du circuit S1 est à la température T0' sensiblement inférieure à la température ambiante. Puis, le flux D est de nouveau dirigé vers le compresseur C3 pour effectuer de manière continue un nouveau cycle.The same flow D of circuit S1 finally passes through cryogenic exchanger EC1 to provide
Dans cette configuration, les compresseurs C1 et C2 fonctionnent en parallèle et doivent assurer le plus haut niveau de pression du cycle. Les deux compresseurs C1 et C2 traitent des débits de fluide réfrigérant différents, respectivement D1' et D2', et sont accouplés directement aux turbines E1 et E2 lesquelles elles aussi traitent des débits différents, respectivement D1 et D2.In this configuration, compressors C1 and C2 operate in parallel and must ensure the highest level of pressure in the cycle. The two compressors C1 and C2 process different refrigerant flow rates, respectively D1 'and D2', and are coupled directly to the turbines E1 and E2 which also process different flow rates, respectively D1 and D2.
On a la relation :
D1 + D2 = D = D'1 + D'2, avec D1 différent de D'1 et D2 différent de D'2. En pratique, de préférence D1/D= 5 à 35%, de préférence de 10 à 25%.We have the relation:
D1 + D2 = D = D'1 + D'2, with D1 different from D'1 and D2 different from D'2. In practice, preferably D1 / D = 5 to 35%, preferably 10 to 25%.
Ainsi, dans ce type d'installation, l'intégralité de la puissance est injectée dans le système au niveau du compresseur C3 (par la turbine à gaz GT), les transferts de puissance au niveau des couples turbine compresseur E2-C2 et E1-C1 étant variables en fonction des pressions dans les divers circuits (P1-P2-P3), des niveaux de température à l'entrée des échangeurs cryogéniques, ainsi que des transferts thermiques au sein de chacun de ces dits échangeurs cryogéniques.Thus, in this type of installation, all of the power is injected into the system at the level of compressor C3 (by the gas turbine GT), the power transfers at the level of the turbine compressor pairs E2-C2 and E1- C1 being variable according to the pressures in the various circuits (P1-P2-P3), the temperature levels at the inlet of the cryogenic exchangers, as well as the heat transfers within each of these said cryogenic exchangers.
Ainsi, une telle installation présente un point de fonctionnement qui s'auto-stabilise à un niveau d'énergie de consommation donnée Ef exprimé en général en kW x jour/t c'est à dire en kW-jour par tonne de GNL produit, ou encore en kWh par kg de GNL produit, ledit point de fonctionnement pouvant le cas échéant être totalement instable. Il est alors très difficile de piloter les pressions des boucles haute et basse indépendamment l'une de l'autre. Cela peut se révéler nécessaire dans le cas de variations de composition du gaz naturel à liquéfier. Il est possible de modifier les flux en contraignant localement tout ou partie des flux D1-D'1-D2-D'1, par exemple en créant des pertes de charge localisées, mais de telles dispositions conduisent à des pertes d'énergie, donc à une baisse du rendement global de l'installation de liquéfaction.Thus, such an installation has an operating point which stabilizes itself at a given level of energy consumption Ef generally expressed in kW x day / t, that is to say in kW-day per tonne of LNG produced, or in kWh per kg of LNG produced, said operating point possibly being totally unstable. It is then very difficult to control the pressures of the high and low loops independently of one another. This may prove to be necessary in the case of variations in the composition of the natural gas to be liquefied. It is possible to modify the flows by locally constraining all or part of the D1-D'1-D2-D'1 flows, for example by creating localized pressure drops, but such arrangements lead to energy losses, therefore a drop in the overall efficiency of the liquefaction plant.
Le diagramme de la
On y a représenté :
la phase 1 de refroidissement du gaz naturel entre les points AA et BB correspondant à l'étage EC1 du PFD de lafigure 1 , correspondant à des températures comprises entre la température ambiante T0 et T1= -50°C,la phase 2 de liquéfaction du gaz naturel entre les points BB et CC, correspondant à l'étage EC2 du PFD de lafigure 1 , correspondant à des températures comprises entre T1= -50°C et T2= -120°C,- la phase 3 de refroidissement du GNL entre les points CC et DD, correspondant à l'étage EC3 du PFD de la
figure 1 , correspondant à des températures comprises entre T2= -120°C et T3= -165°C.
-
phase 1 for cooling natural gas between points AA and BB corresponding to stage EC1 of the PFD of thefigure 1 , corresponding to temperatures between ambient temperature T0 and T1 = -50 ° C, -
phase 2 of natural gas liquefaction between points BB and CC, corresponding to stage EC2 of the PFD of thefigure 1 , corresponding to temperatures between T1 = -50 ° C and T2 = -120 ° C, - LNG cooling phase 3 between points CC and DD, corresponding to stage EC3 of the PFD of the
figure 1 , corresponding to temperatures between T2 = -120 ° C and T3 = -165 ° C.
La courbe 50 comportant des triangles, illustre les variations de l'enthalpie H des fluides circulant à co-courant dans les circuits Sg et S2 en fonction de la température du gaz à liquéfier comportant le méthane/GNL pour un procédé virtuel idéal.The
La courbe 51 correspond à la variation de l'enthalpie H du gaz réfrigérant circulant dans le circuit S1 de la
La surface 52 comprise entre les deux courbes 50 et 51 représente la perte d'énergie globale consommée Ef dans le procédé de liquéfaction : - on cherche donc à minimiser cette surface de manière à obtenir le meilleur rendement. Dans les procédé à terre utilisant des procédés à changement de phase du fluide réfrigérant, la courbe 51 n'est plus rectiligne, mais se rapproche beaucoup plus de la courbe théorique 50, ce qui implique moins de pertes, donc un rendement amélioré, mais le procédé à changement de phase du fluide réfrigérant n'est pas adapté à la liquéfaction à bord d'un support flottant en environnement confiné.The
Les
Sur les
Du fait que l'essentiel de l'énergie est consommée pour la phase 2 du procédé au sein dudit deuxième échangeur, ceci permet d'augmenter encore les transferts thermiques et le rendement énergétique global du procédé. Mais de façon plus importante, on permet en outre de moduler et contrôler spécifiquement la valeur de la pression P2 en montant en série les deux compresseurs C1 et C2 et en couplant C1 avec un moteur M1 permettant de moduler et contrôler la puissance supplémentaire apportée à C1 déjà couplé à la turbine E1, et donc de contrôler la valeur de la pression P2 comme décrit ci-après.Because most of the energy is consumed for
Plus précisément, sur les
- (a) circulation dudit gaz naturel à liquéfier circulant Sg à une pression P0 supérieure ou égale à la pression atmosphérique (Patm), P0 étant supérieure à la pression atmosphérique, dans 3 échangeurs de chaleur cryogéniques EC1, EC2, et EC3 disposés en série dont :
- un premier échangeur EC1 dans lequel ledit gaz naturel entrant à une température T0 est refroidit et sort en BB à une température T1 inférieure à T0, température T1 à laquelle tous les composants du gaz naturel sont encore à l'état gazeux, puis
- un deuxième échangeur EC2 dans lequel le gaz naturel est entièrement liquéfié et sort en CC à une température T2 inférieure à T1, et
- un troisième échangeur EC3 dans lequel ledit gaz naturel liquéfié est refroidit de T2 à T3, T3 étant inférieure à T2 et T3 étant inférieure à la température de liquéfaction dudit gaz naturel à pression atmosphérique, et
- (b) circulation à circuit fermé de deux flux S1 et S3 de gaz réfrigérant à l'état gazeux dénommés respectivement premier et troisième flux, respectivement à des pressions différentes P1 (S1) et P2 (S2), traversant deux dits échangeurs en contact indirect avec et à contre-courant du flux de gaz naturel Sg, comprenant :
- un premier flux de gaz réfrigérant S1 à une pression P1 inférieure à P3 traversant les 3 échangeurs EC1, EC2 et EC3 entrant en DD dans ledit troisième échangeur EC3 à une température T3' inférieure à T3 puis sortant dudit troisième échangeur et entrant dans ledit deuxième échangeur EC2 en CC à une température T2' inférieure à T2, puis sortant du deuxième échangeur et entrant dans le premier échangeur EC1 en BB à une température T1' inférieure à T1 et sortant en AA dudit premier échangeur à une température T0' inférieure à T0, ledit premier flux de gaz réfrigérant à P1 et T3' étant obtenu par détente dans un premier détendeur E1 d'une partie D1 d'un deuxième flux S2 de gaz réfrigérant comprimé à la pression P3 supérieure à P2, ledit deuxième flux S2 circulant en contact indirect avec et à co-courant dudit flux gaz naturel Sg en entrant en AA dans ledit premier échangeur EC1 sensiblement à T0 et sortant en CC dudit deuxième échangeur EC) sensiblement à la température T2, et
- un troisième flux S3 à une pression P2 supérieure à P1 et inférieure à P3 circulant en contact indirect avec et à co-courant dudit premier flux, traversant uniquement les dits deuxième et premier échangeurs EC2 et EC1, entrant en CC dans ledit deuxième échangeur sensiblement à une température T2' inférieure à T2 et sortant en AA dudit premier échangeur EC sensiblement à une température T0', ledit troisième flux S3 de gaz réfrigérant à P2 et T2 étant obtenu par détente dans un deuxième détendeur E2 d'une partie D2 dudit deuxième flux S2 de gaz réfrigérant sortant dudit premier échangeur sensiblement à T1,
- (c) ledit deuxième flux de gaz réfrigérant S2 comprimé à la pression P3 étant obtenu par compression desdits premier et troisième flux de gaz réfrigérant sortant en AA du dit premier échangeur EC1 à P1 et respectivement P2, par deux premier et deuxième compresseurs, respectivement C1 et C2 disposés en série et couplés respectivement auxdits premier et deuxième détendeurs E1 et E2 consistant en des turbines, et
- (d) après l'étape (a) on dépressurise le gaz naturel liquéfié sortant en DD dudit troisième échangeur à T3, depuis la pression P0 à la pression atmosphérique le cas échéant.
- (a) circulation of said natural gas to be liquefied circulating Sg at a pressure P0 greater than or equal to atmospheric pressure (Patm), P0 being greater than atmospheric pressure, in 3 cryogenic heat exchangers EC1, EC2, and EC3 arranged in series including :
- a first exchanger EC1 in which said natural gas entering at a temperature T0 is cooled and exiting at BB at a temperature T1 lower than T0, temperature T1 at which all the components of the natural gas are still in the gaseous state, then
- a second exchanger EC2 in which the natural gas is completely liquefied and leaves in CC at a temperature T2 lower than T1, and
- a third exchanger EC3 in which said liquefied natural gas is cooled from T2 to T3, T3 being lower than T2 and T3 being lower than the liquefaction temperature of said natural gas at atmospheric pressure, and
- (b) closed circuit circulation of two streams S1 and S3 of refrigerant gas in the gaseous state called the first and third stream, respectively, at different pressures P1 (S1) and P2 (S2), passing through two said exchangers in indirect contact with and against the flow of natural gas Sg, comprising:
- a first flow of refrigerant gas S1 at a pressure P1 less than P3 passing through the 3 exchangers EC1, EC2 and EC3 entering DD into said third exchanger EC3 at a temperature T3 'lower than T3 then leaving said third exchanger and entering said second exchanger EC2 in CC at a temperature T2 'lower than T2, then leaving the second exchanger and entering the first exchanger EC1 at BB at a temperature T1' lower than T1 and exiting at AA from said first exchanger at a temperature T0 'lower than T0, said first flow of refrigerant gas at P1 and T3 'being obtained by expansion in a first regulator E1 of a part D1 of a second flow S2 of refrigerant gas compressed at the pressure P3 greater than P2, said second flow S2 circulating in contact indirect with and co-current of said natural gas flow Sg entering at AA in said first exchanger EC1 substantially at T0 and exiting at CC from said second exchanger EC) substantially at temperature T2, and
- a third flow S3 at a pressure P2 greater than P1 and less than P3 circulating in indirect contact with and co-current with said first flow, passing only through said second and first exchangers EC2 and EC1, entering at DC in said second exchanger substantially at a temperature T2 'lower than T2 and leaving at AA from said first exchanger EC substantially at a temperature T0', said third flow S3 of refrigerant gas at P2 and T2 being obtained by expansion in a second regulator E2 of a part D2 of said second flow S2 of refrigerant gas leaving said first exchanger substantially at T1,
- (c) said second flow of refrigerant gas S2 compressed to pressure P3 being obtained by compressing said first and third flow of refrigerant gas leaving at AA from said first exchanger EC1 to P1 and respectively P2, by two first and second compressors, respectively C1 and C2 arranged in series and coupled respectively to said first and second regulators E1 and E2 consisting of turbines, and
- (d) after step (a) the liquefied natural gas exiting at DD from said third exchanger at T3 is depressurized, from pressure P0 to atmospheric pressure where appropriate.
Plus précisément, sur la
- (1) trois compresseurs C1, C2 et C3 montés en série, comprenant :
- (i) un premier compresseur C1 couplé audit premier détendeur E1, comprimant de P1 à P2 la totalité du dit premier flux de gaz réfrigérant sortant en AA dudit premier échangeur EC1, et
- (ii) un deuxième compresseur C2 couplé audit deuxième détendeur E2, comprimant de P2 à P'3, P'3 étant supérieure à P2 et inférieure ou égal à P3, d'une part ledit troisième flux S3 de gaz réfrigérant sortant à P2 du dit premier échangeur EC1, et d'autre part ledit premier flux de gaz réfrigérant comprimé à P2 sortant dudit premier compresseur C1, et
- (iii) un troisième compresseur C3 actionné par une turbine à gaz GT pour fournir la majeure partie de l'énergie et comprimer de P'3 à P3 la totalité des premier et troisième flux de gaz réfrigérant comprimés par le deuxième compresseur C2, pour obtenir ledit deuxième flux de gaz réfrigérant à P3 et T0 après refroidissement (H1, H2), et
- (2) ledit premier compresseur C1 est couplé à un premier moteur M1, permettant de faire varier de façon contrôlée la pression P2 en apportant de la puissance de façon contrôlée audit premier compresseur C1, ledit premier moteur M1 apportant au moins 3%, de préférence encore de 3 à 30% de la puissance totale apportée à l'ensemble des dits compresseurs mis en œuvre C1, C2 et C3, la turbine à gaz GT couplée au dit troisième compresseur C3, ainsi que le deuxième moteur M2 couplé au deuxième compresseur C2 fournissant ensemble de 97 à 70% de la puissance totale apportée à l'ensemble des dits compresseurs mis en œuvre C1, C2 et C3.
- (1) three compressors C1, C2 and C3 mounted in series, comprising:
- (i) a first compressor C1 coupled to said first expander E1, compressing from P1 to P2 all of said first flow of refrigerant gas exiting at AA from said first exchanger EC1, and
- (ii) a second compressor C2 coupled to said second expansion valve E2, compressing from P2 to P'3, P'3 being greater than P2 and less than or equal to P3, on the one hand said third flow S3 of refrigerant gas exiting at P2 from the said first exchanger EC1, and on the other hand said first flow of refrigerant gas compressed to P2 leaving said first compressor C1, and
- (iii) a third compressor C3 actuated by a gas turbine GT to supply the major part of the energy and compress from P'3 to P3 all of the first and third streams of refrigerant gas compressed by the second compressor C2, to obtain said second flow of refrigerant gas at P3 and T0 after cooling (H1, H2), and
- (2) said first compressor C1 is coupled to a first motor M1, making it possible to vary the pressure P2 in a controlled manner by supplying power in a controlled manner to said first compressor C1, said first motor M1 providing at least 3%, more preferably from 3 to 30% of the total power supplied to the 'set of said compressors C1, C2 and C3 used, the gas turbine GT coupled to said third compressor C3, as well as the second motor M2 coupled to the second compressor C2 together providing 97 to 70% of the total power supplied to all of the said compressors C1, C2 and C3 implemented.
L'installation de la
- une pluralité de moteurs, en général une turbine à gaz GT qui actionne le compresseur C3 et des moteurs M1-M2, par exemple soit électriques soit thermiques, tels des turbines à gaz, connectés respectivement aux compresseurs C1-C2,
- 3 compresseurs :
- C3 qui comprime l'intégralité du flux de gaz réfrigérant D,
- C2 qui est accouplé au moteur M2 et à la turbine E2, et qui comprime l'intégralité du flux de gaz réfrigérant D,
- C1 qui est accouplé au moteur M1 et à la turbine E1, et qui comprime la portion D1 de premier flux de gaz réfrigérant,
- 2 détendeurs, par exemple des turbines,
- E2 couplé au compresseur C2 et au moteur M2,
- E1 couplé au compresseur C1 et au moteur M1,
- d'un échangeur cryogénique en trois parties ou 3 échangeurs en série EC1, EC2 et EC3, correspondant respectivement aux phases 1, 2 et 3 de la liquéfaction et comportant quatre circuits, respectivement SG (gaz naturel et S1-S2-S3 (gaz réfrigérant),
- de deux refroidisseurs, H1 et H2, situés respectivement en sortie du compresseur principal C3 (H2) avant l'entrée dans le circuit S2 des échangeurs cryogéniques, et sur la boucle haute pression (H1).
- a plurality of engines, in general a gas turbine GT which drives the compressor C3 and M1-M2 engines, for example either electric or thermal, such as gas turbines, respectively connected to the compressors C1-C2,
- 3 compressors:
- C3 which compresses the entire flow of refrigerant gas D,
- C2 which is coupled to the motor M2 and to the turbine E2, and which compresses the entire flow of refrigerant gas D,
- C1 which is coupled to the motor M1 and to the turbine E1, and which compresses the portion D1 of the first flow of refrigerant gas,
- 2 regulators, for example turbines,
- E2 coupled to compressor C2 and motor M2,
- E1 coupled to compressor C1 and motor M1,
- a cryogenic exchanger in three parts or 3 exchangers in series EC1, EC2 and EC3, corresponding respectively to
1, 2 and 3 of liquefaction and comprising four circuits, respectively SG (natural gas and S1-S2-S3 (refrigerant gas),phases - two coolers, H1 and H2, located respectively at the outlet of the main compressor C3 (H2) before the entry into the circuit S2 of the cryogenic exchangers, and on the high pressure loop (H1).
Les compresseurs C1 et C2 sont montés en série.
- C1 opère entre la basse pression P1 et la moyenne pression P2, sur la portion D1 du flux de gaz réfrigérant en provenance de la turbine E1 circulant dans le circuit S1, du bas vers le haut, à travers chacun des trois échangeurs cryogéniques EC3-EC2-EC1.
- C2 opère entre la moyenne pression P2 et la haute pression intermédiaire P'3 sur l'intégralité du flux D, composé de la portion D1 de flux en provenance du compresseur C1 et de la portion D2 du flux de gaz réfrigérant en provenance de la turbine E2 circulant dans le circuit S3, du bas vers le haut, à travers chacun des deux échangeurs cryogéniques EC2-EC1.
- C1 operates between low pressure P1 and medium pressure P2, on portion D1 of the refrigerant gas flow coming from turbine E1 circulating in circuit S1, from bottom to top, through each of the three cryogenic exchangers EC3-EC2 -EC1.
- C2 operates between the medium pressure P2 and the intermediate high pressure P'3 on the entire flow D, composed of the portion D1 of the flow coming from the compressor C1 and the portion D2 of the refrigerant gas flow coming from the turbine E2 circulating in circuit S3, from bottom to top, through each of the two cryogenic exchangers EC2-EC1.
L'intégralité du flux de gaz réfrigérant D sortant du compresseur C2 est refroidie dans un refroidisseur H1 avant de rentrer à la pression P'3 dans le compresseur C3, ce dernier étant connecté à un moteur (GT), en général une turbine à gaz. Ladite turbine à gaz ainsi que le moteur (M2) fournissent ensemble au gaz réfrigérant de 70 à 97% de la puissance globale Q, le reliquat de puissance étant fourni au système au niveau du moteur M1, à savoir de 30 à 3% de la puissance globale Q.The entire flow of refrigerant gas D leaving compressor C2 is cooled in a cooler H1 before returning to pressure P'3 in compressor C3, the latter being connected to an engine (GT), generally a gas turbine. . Said gas turbine and the engine (M2) together supply the refrigerant gas from 70 to 97% of the overall power Q, the remainder of the power being supplied to the system at the level of the engine M1, namely 30 to 3% of the overall power Q.
En sortie du compresseur C3, l'intégralité du flux de gaz réfrigérant D est à la haute pression P3. Le flux est alors refroidi dans un refroidisseur H2 avant de circuler dans le circuit S2, du haut vers le bas, à travers chacun des deux échangeurs cryogéniques EC1-EC2.At the outlet of the compressor C3, the entire flow of refrigerant gas D is at high pressure P3. The flow is then cooled in a cooler H2 before circulating in the circuit S2, from top to bottom, through each of the two cryogenic exchangers EC1-EC2.
La portion D2 de flux de gaz réfrigérant est prélevée en BB à la sortie de l'échangeur cryogénique EC1 et dirigé vers l'entrée de la turbine E2, le complément, c'est à dire la portion D1 de flux de gaz réfrigérant étant prélevée en CC à la sortie de l'échangeur cryogénique EC2 et dirigé vers l'entrée de la turbine E1.The refrigerant gas flow portion D2 is taken at BB at the outlet of the cryogenic exchanger EC1 and directed towards the inlet of the turbine E2, the remainder, that is to say the portion D1 of the flow of refrigerant gas being taken at DC at the outlet of the cryogenic exchanger EC2 and directed towards the inlet of the turbine E1.
Au sein du compresseur C3, on installe entre deux étages de compression un refroidisseur H2 fonctionnant à la pression P'3, ledit refroidisseur H2 traitant l'intégralité du flux D.Within the compressor C3, a cooler H2 operating at pressure P'3 is installed between two compression stages, said cooler H2 treating all of the stream D.
Dans ce procédé selon l'invention, on a les relations :
D1 + D2 = D et de préférence D1/D2=1/3 à 1/20, de préférence de 1/4 à 1/10.In this method according to the invention, we have the relationships:
D1 + D2 = D and preferably D1 / D2 = 1/3 to 1/20, preferably 1/4 to 1/10.
Le principal avantage du dispositif selon l'invention de la
Ainsi, dans le diagramme de la
La courbe 53 correspond à la variation de l'enthalpie H du fluide réfrigérant circulant dans les circuits S1 et S3 de la
La surface 52 comprise entre les deux courbes 50 et 53 représente la perte d'énergie globale dans le processus de liquéfaction en référence à la
Lors des variations dans le temps de la qualité du gaz naturel fourni par le champ de gaz, donc de sa composition, le point bas 54 de la courbe 50 correspondant à P0 et T2 de fin de liquéfaction du GNL, peut varier de quelques %. Dans le processus conventionnel de la
Par contre, dans le dispositif selon l'invention selon la
La
Dans cette version de la
Sur les
Sur les
Sur les
D'autre part, sur le diagramme 5A relatif à un mélange azote-néon, le point de fonctionnement dans le cas du procédé conventionnel de la
Les points W0 à W4 correspondent à des puissances injectées au niveau du moteur M1 :
- W0 = puissance nulle,
- W1 = 7% de la puissance globale,
- W2 = 15% de la puissance globale,
- W3 = 24% de la puissance globale,
- W4 = 33% de la puissance globale.
- W0 = zero power,
- W1 = 7% of the overall power,
- W2 = 15% of the overall power,
- W3 = 24% of the overall power,
- W4 = 33% of the overall power.
De manière similaire sur le diagramme de la
Ainsi, sur cette même
De manière similaire sur le diagramme de la
Ainsi, une augmentation de la proportion de puissance injectée W au niveau du moteur M1 des
- n'a pas d'influence sur la pression P1,
- augmente la pression P2,
- augmente la pression maximale P3,
- diminue la consommation en énergie Ef jusqu'à une valeur minimale, pour une proportion de puissance W donnée, puis cette consommation en énergie croît à nouveau au-delà de cette dite proportion de puissance W donnée.
- has no influence on the pressure P1,
- increases the pressure P2,
- increases the maximum pressure P3,
- decreases the energy consumption Ef to a minimum value, for a given proportion of power W, then this energy consumption increases again beyond this said given proportion of power W.
De la même manière, l'utilisation d'un mélange azote-néon conduit à une amélioration des performances énergétiques telle que représenté sur les
Ainsi, en considérant un mélange comportant 20% de néon, la pression P1 est d'environ 12.5 bars et la courbe 71 de la
Pour ce même pourcentage en néon de 20%, sur la courbe 91 de la
Les mêmes effets sont observés pour l'hydrogène sur les
Sur les
Dans le diagramme de la
De manière générale, en opérant à plus forte pression, pour un débit massique donné, les débits volumiques sont réduits au prorata de l'augmentation de ladite pression : - les conduites sont de plus faible diamètre, mais leur résistance mécanique, donc leur épaisseur, leur poids et leur coût sont augmentés d'autant : - par contre, l'emprise au sol s'en trouve réduite d'autant, ce qui est très intéressant dans le cas d'installations en environnement confiné tel que sur un support flottant ancré en mer, ou encore sur un méthanier dans le cas d'unité de reliquéfaction de boil-off. De la même manière, les compresseurs et les turbines opérant à plus forte pression sont beaucoup plus compacts. En ce qui concerne les échangeurs cryogéniques, l'augmentation de la pression améliore aussi les transferts thermiques, mais les surfaces d'échange thermique ne sont pas réduites dans la même proportion que dans le cas des conduites et des compresseurs et des turbines. En revanche, leur poids augmente de manière importante car ils doivent résister à cet accroissement de pression.In general, by operating at higher pressure, for a given mass flow rate, the volume flow rates are reduced in proportion to the increase in said pressure: - the pipes are of smaller diameter, but their mechanical resistance, therefore their thickness, their weight and cost are increased by as much: - on the other hand, the footprint is reduced accordingly, which is very interesting in the case of installations in a confined environment such as on an anchored floating support at sea, or on an LNG carrier in the case of a boil-off reliquefaction unit. Likewise, compressors and turbines operating at higher pressure are much more compact. With regard to cryogenic exchangers, the increase in pressure also improves heat transfers, but the heat exchange surfaces are not reduced in the same proportion as in the case of pipes and compressors and turbines. On the other hand, their weight increases significantly because they have to resist this increase in pressure.
Ainsi, globalement, le procédé selon l'invention des
Sur la
Ainsi, pour une composition donnée de gaz, le point de fonctionnement du processus conventionnel en référence à la
En utilisant comme gaz réfrigérant un mélange de 80% d'azote et de 20% de néon, on peut augmenter la pression, comme représenté sur la courbe 70, sans que le mélange de gaz n'atteigne son point de rosée, jusqu'à une valeur optimale 70a d'environ 88 bars et pour une consommation en énergie minimale d'environ 19.4 kWxd/t, ce qui représente un gain de rendement thermodynamique de 1.77% par rapport au point de fonctionnement 62 du procédé selon l'invention avec un gaz réfrigérant composé de 100% d'azote et un gain de rendement thermodynamique de 8.92% par rapport au point de fonctionnement 60 du procédé conventionnel.By using a mixture of 80% nitrogen and 20% neon as refrigerant gas, the pressure can be increased, as shown on
En utilisant comme gaz réfrigérant un mélange de 60% d'azote et de 40% de néon, on peut augmenter la pression, comme représenté sur la courbe 71, sans que le mélange de gaz n'atteigne son point de rosée, jusqu'à une valeur optimale 71a d'environ 118 bars et pour une consommation en énergie minimale d'environ 19.15 kWxd/t, ce qui représente un gain de rendement thermodynamique de 3.04% par rapport au point de fonctionnement 62 du procédé selon l'invention avec un gaz réfrigérant composé de 100% d'azote et un gain de rendement thermodynamique de 10.09% par rapport au point de fonctionnement 60 du procédé conventionnel.By using a mixture of 60% nitrogen and 40% neon as refrigerant gas, the pressure can be increased, as shown on
En utilisant comme gaz réfrigérant un mélange de 50% d'azote et de 50% de néon, on peut augmenter la pression, comme représenté sur la courbe 72, sans que le mélange de gaz n'atteigne son point de rosée, jusqu'à une valeur optimale 72a d'environ 145 bars et pour une consommation en énergie minimale d'environ 18.8 kWxd/t, ce qui représente un gain de rendement thermodynamique de 4.81% par rapport au point de fonctionnement 62 du procédé selon l'invention avec un gaz réfrigérant composé de 100% d'azote et un gain de rendement thermodynamique de 11.74% par rapport au point de fonctionnement 60 du procédé conventionnel.By using a mixture of 50% nitrogen and 50% neon as refrigerant gas, the pressure can be increased, as shown on
De la même manière, comme représenté sur le diagramme de la
Ainsi, en utilisant comme gaz réfrigérant un mélange de 80% d'azote et de 20% d'hydrogène, on peut augmenter la pression, comme représenté sur la courbe 80, sans que le mélange de gaz n'atteigne son point de rosée, jusqu'à une valeur optimale 80a d'environ 94 bars et pour une consommation en énergie minimale d'environ 19.2 kWxd/t, ce qui représente un gain de rendement thermodynamique de 2.78% par rapport au point de fonctionnement 62 du procédé selon l'invention des
En utilisant comme gaz réfrigérant un mélange de 60% d'azote et de 40% d'hydrogène, on peut augmenter la pression, comme représenté sur la courbe 81, sans que le mélange de gaz n'atteigne son point de rosée, jusqu'à une valeur optimale 81a d'environ 140 bars et pour une consommation en énergie minimale d'environ 18.8 kWxd/t, ce qui représente un gain de rendement thermodynamique de 4.81% par rapport au point de fonctionnement 62 du procédé selon l'invention des
En utilisant comme gaz réfrigérant un mélange de 50% d'azote et de 50% d'hydrogène, on peut augmenter la pression, comme représenté sur la courbe 82, sans que le mélange de gaz n'atteigne son point de rosée, jusqu'à une valeur optimale 82a d'environ 186 bars et pour une consommation en énergie minimale d'environ 18.7 kWxd/t, ce qui représente un gain de rendement thermodynamique de 5.32% par rapport au point de fonctionnement 62 du procédé selon l'invention des
Ainsi, un pourcentage croissant de gaz complémentaire, soit de l'hydrogène, soit du néon, rajouté à de l'azote pour constituer un gaz réfrigérant, améliore de manière radicale de rendement thermodynamique du procédé, tout en autorisant un fonctionnement à plus haute pression, ce qui implique des équipements plus compacts, ce qui est très avantageux dès lors que l'on ne dispose que de surfaces très réduites, ce qui est le cas sur un support flottant ancré en mer, ou à bord d'un méthanier, dans le cas d'unités de reliquéfaction.Thus, an increasing percentage of complementary gas, either hydrogen or neon, added to nitrogen to constitute a refrigerant gas, radically improves the thermodynamic efficiency of the process, while allowing operation at higher pressure. , which implies more compact equipment, which is very advantageous when only very small surfaces are available, which is the case on a floating support anchored at sea, or on board an LNG carrier, in the case of reliquefaction units.
Avantageusement, le procédé selon l'invention utilise soit un mélange d'azote et de néon, soit d'azote et d'hydrogène, et malgré son rendement légèrement inférieur, on privilégiera l'utilisation du mélange d'azote et de néon, car le néon est un gaz inerte, alors que l'hydrogène est combustible et reste dangereux et délicat à opérer, surtout à haute pression dans des installations confinées à bord d'un support flottant. De plus l'hydrogène est un gaz qui percole très facilement à travers des joints élastomériques et même dans certains cas à travers les métaux, surtout à très haute pression, et de ce fait le procédé selon l'invention basé sur l'utilisation d'un mélange azote-hydrogène ne constitue pas la version préférée de l'invention : la version préférée de l'invention reste l'utilisation comme gaz réfrigérant d'un mélange d'azote et de néon dans les dispositifs décrits en référence aux diverses figures.Advantageously, the method according to the invention uses either a mixture of nitrogen and neon, or of nitrogen and hydrogen, and despite its slightly lower yield, the use of the mixture of nitrogen and neon will be preferred, because neon is an inert gas, while hydrogen is combustible and remains dangerous and difficult to operate, especially at high pressure in installations confined on board a floating medium. In addition, hydrogen is a gas which percolates very easily through elastomeric seals and even in certain cases through metals, especially at very high pressure, and therefore the process according to the invention based on the use of a nitrogen-hydrogen mixture does not constitute the preferred version of the invention: the preferred version of the invention remains the use as refrigerant gas of a mixture of nitrogen and neon in the devices described with reference to the various figures.
De la même manière, on améliore le rendement des procédés conventionnels utilisant comme gaz réfrigérant de l'azote, en considérant un mélange binaire azote-néon ou azote-hydrogène, ce qui, par contre, ne fait pas objet de la présente invention.In the same way, the yield of the conventional processes using nitrogen as refrigerant gas is improved, by considering a binary nitrogen-neon or nitrogen-hydrogen mixture, which, on the other hand, is not the subject of the present invention.
Ainsi, comme représenté sur le diagramme de la
Pour un pourcentage de 40% de néon, le point de fonctionnement se situe en 71b, ce qui correspond à une pression maximale P3 de 90 bars environ et une consommation en énergie d'environ 19.70 kWxd/t, ce qui représente un gain de rendement thermodynamique de 7.29% par rapport au point de fonctionnement 60 du même procédé conventionnel avec un gaz réfrigérant composé de 100% d'azote.For a percentage of 40% neon, the operating point is at 71b, which corresponds to a maximum pressure P3 of approximately 90 bars and an energy consumption of approximately 19.70 kWxd / t, which represents a gain in efficiency thermodynamic of 7.29% compared to the
Pour un pourcentage de 50% de néon, le point de fonctionnement se situe en 72b, ce qui correspond à une pression maximale P3 de 120 bars environ et une consommation en énergie d'environ 19.35 kWxd/t, ce qui représente un gain de rendement thermodynamique de 8.94% par rapport au point de fonctionnement 60 du même procédé conventionnel avec un gaz réfrigérant composé de 100% d'azote.For a percentage of 50% neon, the operating point is at 72b, which corresponds to a maximum pressure P3 of approximately 120 bars and an energy consumption of approximately 19.35 kWxd / t, which represents a gain in efficiency thermodynamic of 8.94% compared to the
De la même manière avec un mélange azote-hydrogène comportant 20% d'hydrogène, comme représenté sur la
Pour un pourcentage de 40% d'hydrogène, le point de fonctionnement se situe en 81b, ce qui correspond à une pression maximale P3 de 108 bars environ et une consommation en énergie d'environ 19.8 kWxd/t, ce qui représente un gain de rendement thermodynamique de 6.82% par rapport au point de fonctionnement 60 du même procédé conventionnel avec un gaz réfrigérant composé de 100% d'azote.For a percentage of 40% hydrogen, the operating point is at 81b, which corresponds to a maximum pressure P3 of approximately 108 bars and an energy consumption of approximately 19.8 kWxd / t, which represents a gain of thermodynamic efficiency of 6.82% compared to the
Pour un pourcentage de 50% d'hydrogène, le point de fonctionnement se situe en 82b, ce qui correspond à une pression maximale P3 de 150 bars environ et une consommation en énergie d'environ 19 kWxd/t, ce qui représente un gain de rendement thermodynamique de 10.59% par rapport au point de fonctionnement 60 du même procédé conventionnel avec un gaz réfrigérant composé de 100% d'azote.For a percentage of 50% hydrogen, the operating point is located at 82b, which corresponds to a maximum pressure P3 of approximately 150 bars and an energy consumption of approximately 19 kWxd / t, which represents a gain of thermodynamic efficiency of 10.59% compared to the
A titre d'exemple, une unité de liquéfaction conventionnelle est dimensionnée par rapport aux puissances des turbines à gaz disponibles, les turbines de forte puissance étant couramment de 25MW.For example, a conventional liquefaction unit is dimensioned in relation to the powers of the gas turbines available, high power turbines are commonly 25MW.
On cherche en général à augmenter la puissance de l'installation, et il est alors possible d'installer en parallèle deux turbines à gaz (GT1 et GT2) identiques pour obtenir 30MW (2x15MW), voire 40MW (2x20MW), mais on alors deux lignes de machines tournantes, ce qui augmente les encombrements, les quantités de conduites et bien sûr les coûts.We generally seek to increase the power of the installation, and it is then possible to install two identical gas turbines (GT1 and GT2) in parallel to obtain 30MW (2x15MW), or even 40MW (2x20MW), but we then have two lines of rotating machines, which increases the overall dimensions, the quantities of pipes and of course the costs.
En installant une seule turbine GT de 25MW en C3 comme sur la
Ainsi, en considérant une turbine à gaz GT de 25MW, l'ajout de 5MW de puissance au niveau du moteur (M2), de préférence grâce à une motorisation électrique, donne plus de souplesse au fonctionnement et permet ainsi un accroissement de puissance de 20%. Par contre, le rendement de l'ensemble reste inchangé, sensiblement à 21.25 kW x jour/t de LNG produit comme représenté sur le diagramme de la
Si par contre, on fournit la même puissance de 5MW au niveau du premier moteur M1, la puissance globale est toujours de 30MW, mais dans ce cas le rendement de l'ensemble est amélioré et atteint sensiblement la valeur de 19.8 kW x jour/t de LNG produit, ce qui représente un gain de 6.59% pour la même puissance globale de 30MW, par rapport à une injection de puissance de 5MW au niveau du deuxième moteur M2, comme détaillé précédemment. Ledit apport de puissance de 5MW au niveau du premier moteur M1 représente alors 16.6% de la puissance globale et ledit rendement (19.8 kW x jour/t) correspond sensiblement au point W2 du diagramme de la
De la même manière sur la
Ainsi, en considérant une turbine à gaz GT de 25MW, l'ajout de 5MW de puissance au niveau de la turbine GT, donne plus de souplesse au fonctionnement et permet ainsi un accroissement de puissance de 20%. Par contre, le rendement de l'ensemble reste inchangé, sensiblement à 21.25 kW x jour/t de LNG produit comme représenté sur le diagramme de la
Si par contre, on fournit la même puissance de 5MW au niveau du premier moteur M1, la puissance globale est toujours de 30MW, mais dans ce cas le rendement de l'ensemble est amélioré et atteint sensiblement la valeur de 19.8 kW x jour/t de LNG produit, ce qui représente un gain de 6.59% pour la même puissance globale de 30MW, par rapport à une injection de puissance de 5MW au niveau du deuxième moteur M2, comme détaillé précédemment. Ledit apport de puissance de 5MW au niveau du premier moteur M1 représente alors 16.6% de la puissance globale et ledit rendement (19.8 kW x jour/t) correspond sensiblement au point W2 du diagramme de la
Ainsi, en fonction de la production de gaz naturel, tant en quantité qu'en qualité, en provenance des nappes souterraines, on utilisera avantageusement une turbine à gaz GT, par exemple de 25MW, à plein régime en permanence,
- que l'on complètera par injection de puissance au niveau de la turbine GT (
fig. 3 ) ou du deuxième moteur M2 (fig.2 ) sans changer le rendement global (point WO de lafigure 7 ), et - que l'on complétera, voire le cas échéant modulera, par injection de puissance au niveau du premier moteur M1 ce qui a pour effet d'améliorer le rendement global selon la courbe 61 de la même
figure 7 , jusqu'à atteindre un optimum, c'est à dire un minimum de consommation d'énergie de 19.75 kW x jour/t correspondant sensiblement au point W3 de ladite courbe 61 : - l'énergie injectée au niveau dudit premier moteur M1 représentant alors dans ce cas sensiblement 24% de l'énergie totale.
- which will be completed by power injection at the level of the GT turbine (
fig. 3 ) or the second motor M2 (fig.2 ) without changing the overall efficiency (point WO of thefigure 7 ), and - which will be supplemented, or even if necessary modulated, by power injection at the level of the first motor M1, which has the effect of improving the overall efficiency according to
curve 61 of the samefigure 7 , until an optimum is reached, i.e. a minimum of energy consumption of 19.75 kW x day / t corresponding substantially to point W3 of said curve 61: the energy injected into said first motor M1 then representing in this case substantially 24% of the total energy.
D'une manière générale, on fonctionnera avec une turbine à gaz GT à plein régime, que l'on complètera par un apport de puissance au niveau du premier moteur M1, ledit apport étant limité à environ 24% de la puissance globale de manière à optimiser le rendement à la valeur minimale de 19.75 kW x jour/t, puis en cas de nécessité, on augmentera la puissance globale par injection de puissance au niveau du deuxième moteur M2, et concomitamment on réajustera la puissance injectée au niveau du premier moteur M1, de manière à ce que ladite puissance soit toujours sensiblement égale à environ 24% de la puissance globale de manière à conserver le rendement de l'installation à la valeur optimale de 19.75 kW x jour/t.In general, we will operate with a gas turbine GT at full speed, which will be completed by a power supply to the first engine M1, said input being limited to about 24% of the overall power so as to optimize the output to the minimum value of 19.75 kW x day / t, then if necessary, the overall power will be increased by power injection at the level of the second motor M2, and at the same time the power injected at the level of the first motor M1 will be readjusted , so that said power is always substantially equal to approximately 24% of the overall power so as to keep the efficiency of the installation at the optimum value of 19.75 kW x day / t.
Ledit rendement optimal de 19.75 kW x jour/t pour une puissance du premier moteur M1 représentant 24% de la puissance totale est valable pour un fluide réfrigérant constitué de 100% d'azote. Dans le cas de mélanges azote-néon ou azote-hydrogène, le rendement optimal ainsi que le pourcentage de puissance varient en fonction des mélanges et des pourcentages de néon ou d'hydrogène, mais les avantages détaillés précédemment restent valables et même se cumulent.Said optimum efficiency of 19.75 kW x day / t for a power of the first motor M1 representing 24% of the total power is valid for a refrigerant fluid consisting of 100% nitrogen. In the case of nitrogen-neon or nitrogen-hydrogen mixtures, the optimum efficiency as well as the power percentage vary depending on the mixtures and the percentages of neon or hydrogen, but the advantages detailed previously remain valid and even accumulate.
Claims (16)
- A method for liquefying a natural gas comprising predominantly methane, preferably at least 85% methane, the other components essentially comprising nitrogen and C2-C4 alkanes, wherein said natural gas to be liquefied is liquefied by circulating said natural gas at a pressure P0 greater than or equal to atmospheric pressure (Patm), preferably P0 being greater than atmospheric pressure, in at least one cryogenic heat exchanger (EC1, EC2, EC3) by counter-current closed circuit circulation in indirect contact with at least one coolant gas flow remaining in gaseous state compressed at a pressure P1 entering said cryogenic exchanger at a temperature T3' lower than T3, T3 being the liquefaction temperature of said liquefied natural gas at the outlet of said cryogenic exchanger, T3 being lower than or equal to the liquefaction temperature of said natural gas liquefied at atmospheric pressure, wherein said natural gas to be liquefied is liquefied by carrying out the following concomitant steps of:(a) circulating said natural gas to be liquefied circulating (Sg) at a pressure P0 greater than or equal to atmospheric pressure (Patm), preferably P0 being greater than atmospheric pressure, in at least three cryogenic heat exchangers (EC1, EC2, EC3) arranged in series including:- a first exchanger (EC1) wherein said natural gas entering at a temperature T0 is cooled and exits (BB) at a temperature T1 lower than T0, then- a second exchanger (EC2) wherein the natural gas is fully liquefied and exits (CC) at a temperature T2 lower than T1 and greater than T3, and- a third exchanger (EC3) wherein said natural gas liquefied is cooled from T2 to T3, and(b) circulating in a closed circuit at least two flows (S1, S3) of coolant gas in gaseous state named first and third flow respectively at different pressures P1 and P2, passing through at least said two exchangers in indirect contact with and against the natural gas flow (Sg), comprising:- said first flow of coolant gas (S1) at a pressure P1 lower than P3 passing through the three exchangers (EC1, EC2, EC3) entering (DD) said third exchanger (EC3) at a temperature T3' lower than T3, then entering (CC) at a temperature T2' lower than T2 said second exchanger (EC2), then entering (BB) at a temperature T1' lower than T1 said first exchanger (EC1) and exiting (AA) said first exchanger at a temperature T0' lower than or equal to T0, said first flow of coolant gas at P1 and T3' being obtained by expansion in at least a first expander (E1) of a first part (D1) of a second flow (S2) of coolant gas compressed at the pressure P3 greater than P2, said second flow (S2) circulating in indirect contact with and co-current of said natural gas flow (Sg) by entering (AA) said first exchanger (EC1) at T0 and said first part (D1) of the second flow (S2) exiting (CC) said second exchanger (EC2) substantially at T2, and- said third flow (S3) at a pressure P2 greater than P1 and lower than P3 circulating in indirect contact with and co-current of said first flow, passing only through said second and first exchangers (EC2, EC1), entering (CC) said second exchanger at a temperature T2' lower than T2 and exiting (AA) said first exchanger (EC1) at T0' lower than or equal to T0, said third flow (S3) of coolant gas at P2 and T2 being obtained by expansion in a second expander (E2) of a second part (D2) of said second flow (S2) of coolant gas exiting said first exchanger substantially at T1, the flow rate D2 of said second part of second flow being preferably greater than the flow rate D1 of the first part of second flow(c) said second flow of coolant gas (S2) compressed at the pressure P3 being obtained by compressing by at least two compressors (C1, C2, C3) and cooling (H1, H2) said first and third flows (S1, S3) of coolant gas exiting (AA) said first exchanger (EC1) at P1 and P2 respectively, a first compressor compressing from P1 to P2 all of said first coolant gas flow exiting (AA) said first exchanger (EC1), and at least the second compressor (C2), compressing from P2 to at least P'3, P'3 being a pressure lower than or equal to P3 and greater than P2, on one hand said third flow (S3) of coolant gas exiting said first exchanger (EC1) at P2, and on the other hand said first flow of coolant gas compressed at P2 exiting said first compressor, in order to obtain said second flow of coolant gas at P3 and T0 after cooling (H1, H2),
method wherein:- both first and second compressors (C1, C2) arranged in series are respectively coupled with said first and second expanders (E1, E2), consisting in energy recovery turbines, and- at least said first compressor (C1) is coupled with a first motor (M1),said method being characterized in that:- said first motor allows to modulate and control specifically the value of the pressure P2 by providing a differentiated power to said first compressor compared to the power supplied to the other compressors, and- a gas turbine (GT) is coupled with either said second compressor, this one compressing said second coolant gas flow directly at P3, or a third compressor (C3) connected in series after the second compressor (C2), said third compressor compressing from P'3 to P3 said second coolant gas flow,- said first motor (M1) providing at least 3%, preferably from 3 to 30%, of the total power supplied to all of said compressors implemented (C1, C2), said gas turbine (GT) providing 97 to 70% of the total power supplied to all of said compressors implemented (C1, C2, C3). - The method according to claim 1, characterized in that said pressure P2 is varied in a controlled manner by supplying power in a controlled manner to said first compressor with said first motor, in such a way that the energy consumed in carrying out the method (Ef) is minimal.
- The method according to claim 2, characterized in that the pressure P2 is increased by increasing the power fed to the first compressor with the first motor, the pressure P1 remaining substantially constant.
- The method according to claim 2 or 3, characterized in that said pressure P2 is varied in a controlled manner by supplying power in a controlled manner to said first compressor with said first motor when the composition of the natural gas to be liquefied varies.
- The method according to any one of claims 1 to 4, characterized in that two compressors (C1, C2) connected in series are implemented, comprising:(i) said first compressor coupled with said first expander (E1), compressing from P1 to P2 all of said first coolant gas flow exiting (AA) said first exchanger (EC1), and(ii) said second compressor (C2) coupled with said second expander (E2), compressing from P2 to P3, on one hand said third flow (S3) of coolant gas exiting said first exchanger (EC1) at P2, and on the other hand said first flow of coolant gas compressed at P2 exiting said first compressor, in order to obtain said second flow of coolant gas (S2) at P3 and T0 after cooling (H1, H2), and(iii) said first compressor (C1) is driven by said first motor (M1), said second compressor (C2) being driven by at least said gas turbine (GT).
- The method according to any one of claims 1 to 4, characterized in that three compressors (C1, C2, C3) connected in series are implemented, comprising:(i) said first compressor (C1) driven by said first motor (M1) and coupled with said first expander (E1), compressing from P1 to P2 all of said first coolant gas flow exiting (AA) said first exchanger (EC1), and(ii) said second compressor (C2) driven by one said second motor (M2) and coupled with said second expander (E2), compressing from P2 to P'3, P'3 being greater than P2 and lower than P3, on one hand said third flow (S3) of coolant gas exiting said first exchanger (EC1) at P2, and on the other hand said first flow of coolant gas compressed at P2 exiting said first compressor C1, and(iii) said third compressor (C3) driven by said gas turbine (GT) to provide most of the energy and compress at P3 all of the first and third coolant gas flows at P3 and T0 after cooling (H1, H2), and(iv) said first motor (M1) provides at least 3%, preferably from 3 to 30%, of the total power supplied to all of said compressors implemented (C1, C2, C3), said gas turbine (GT) coupled with said third compressor (C3), as well as said second motor (M2) coupled with the second compressor (C2) providing together from 97 to 70% of the total power supplied to all of said compressors implemented (C1, C2, C3).
- The method according to any one of claims 1 to 6, characterized in that said coolant gas comprises nitrogen.
- The method according to any one of claims 1 to 7, characterized in that the composition of the gas to be liquefied is within the following ranges for a total of 100%:- Methane from 80 to 100%,- nitrogen from 0 to 20%,- ethane from 0 to 20%,- propane from 0 to 20%, and- butane from 0 to 20%.
- The method according to any one of claims 1 to 8, characterized in that:- T0 and T0' are from 10 to 35°C, and- T3 and T3' are from -160 to -170°C, and- T2 and T2' are from -100 to 140°C, and- T1 and T1' are from -30 to -70°C.
- The method according to any one of claims 1 to 9, characterized in that:- P0 is from 0.5 to 5 MPa, and- P1 is from 0.5 to 5 MPa, and- P2 is from 1 to 10 MPa, and- P3 is from 5 to 20 MPa.
- The method according to any one of claims 1 to 10, characterized in that P2 is varied until the minimum total energy Ef consumed in the method is less than 21.5 kW x day/t of liquefied gas produced, preferably from 18.5 to 20.5 kW x day/t.
- The method according to claims 1 to 11, characterized in that it is carried out on board a floating support.
- The method according to any one of claims 1 to 12, characterized in that it uses a binary mixture nitrogen-neon or nitrogen-hydrogen.
- An on-board installation on a floating support for carrying out a method according to any one of claims 1 to 13, the installation comprises:- at least said three cryogenic heat exchangers (EC1, EC2, EC3) in series comprising at least:- a first counter-current circulation conduit capable of circulating a first flow (S1) of coolant gas in gaseous state compressed at P1 passing in counter-current successively through the 3 third, second and first exchangers (EC3, EC2, EC1),- a second co-current circulation conduit capable of circulating one said second flow (S2) of coolant gas in gaseous state compressed at P3 passing in co-current successively through only said first and second exchangers (EC1, EC2),- a third counter-current circulation conduit of said coolant gas capable of circulating one said third flow (S3) of coolant gas in gaseous state compressed at P2 passing in counter-current successively through only said second and first exchangers (EC2, EC1),- a fourth conduit (Sg) capable of circulating said natural gas to be liquefied passing successively through the three first, second and third exchangers (EC1, EC2, EC3),- a first expander (E1) between the outlet of the second conduit and the inlet of said first conduit,- a second expander (E2) between (i) a bypass (BB) of said second conduit located between said first and second exchangers and (ii) the inlet (CC) of said third conduit, and- a first compressor (C1) at the outlet of said first conduit, coupled with a turbine consisting said first expander,- a second compressor (C2) at the outlet of said third conduit, coupled with a turbine consisting said second expander, and said second compressor being connected in series with said first compressor, and- a conduit for circulating of all the compressed gas at P2 by the first compressor (C1) to the second compressor (C2) so connected in series with said first compressor, and- at least a first motor (M1) coupled with said first compressor (C1),
characterized in that said first motor is capable of providing at least 3%, preferably from 3 to 30%, of the total power supplied to all of said compressors implemented (C1, C2, C3), said first motor allowing to modulate and control specifically the value of the pressure P2 by providing a differentiated power to said first compressor compared to the power supplied to the other compressors, and- a gas turbine (GT) coupled with either said second compressor, this one compressing said second coolant gas flow directly at P3, or to a third compressor (C3) connected in series after the second compressor (C2), said third compressor compressing from P'3 to P3 said second coolant gas flow, said gas turbine being capable of providing from 97 to 70% of the total power supplied to all of said compressors implemented (C1, C2, C3). - The installation according to claim 14, characterized in that it only comprises two compressors (C1, C2) connected in series, comprising:(i) said first compressor (C1) coupled with said first expander (E1), capable of compressing from P1 to P2 all of said first coolant gas flow exiting (AA) said first exchanger (EC1), and(ii) said second compressor (C2) coupled with said second expander (E2), capable of compressing from P2 to at least P'3, P'3 being a pressure greater than P2 and lower than or equal to P3, on one hand said third flow (S3) of coolant gas exiting said first exchanger (EC1) at P2, and on the other hand said first flow of coolant gas compressed at P2 exiting said first compressor, in order to obtain said second flow of coolant gas at P3 and T0 after cooling (H1, H2), and(iii) said first motor (M1), coupled with said first compressor (C1), and at least said gas turbine (GT) coupled with said second compressor (C2), said first motor being capable of providing at least 3%, preferably from 3 to 30%, of the total power supplied to all of said compressors implemented (C1, C2), and(iv) said gas turbine (GT) coupled with said second compressor being capable of providing from 97 to 70% of the total power supplied.
- The installation according to claim 14, characterized in that it only comprises three compressors (C1, C2, C3) connected in series, comprising:(i) said first compressor (C1) coupled with said first expander (E1) and said first motor (M1), and(ii) said second compressor (C2) coupled with said second expander (E2) and a second motor (M2), and(iii) said third compressor (C2) coupled with said gas turbine (GT) capable of providing most of the energy and capable of compressing at P3 all of the first and third coolant gas flows compressed by the second compressor (C2), in order to obtain said second coolant gas flow at P2 and T0 after cooling (H1, H2), and(iv) said first motor (M1) being capable of providing at least 3%, even preferably from 3 to 30%, of the total power supplied to all of said compressors implemented (C1, C2, C3), and(v) the gas turbine (GT) coupled with said third compressor (C3), as well as said second motor (M2) coupled with said second compressor (C2) being capable of providing together from 97 to 70% of the total power supplied to all of said compressors implemented (C1, C2, C3).
Priority Applications (3)
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SI201231880T SI2724100T1 (en) | 2011-06-24 | 2012-06-22 | Method for liquefying natural gas with a triple closed circuit of coolant gas |
RS20210238A RS61507B1 (en) | 2011-06-24 | 2012-06-22 | Method for liquefying natural gas with a triple closed circuit of coolant gas |
HRP20210341TT HRP20210341T1 (en) | 2011-06-24 | 2021-03-01 | Method for liquefying natural gas with a triple closed circuit of coolant gas |
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FR1155595A FR2977015B1 (en) | 2011-06-24 | 2011-06-24 | METHOD FOR LIQUEFACTING NATURAL GAS WITH TRIPLE FIRM CIRCUIT OF REFRIGERATING GAS |
PCT/FR2012/051428 WO2012175889A2 (en) | 2011-06-24 | 2012-06-22 | Method for liquefying natural gas with a triple closed circuit of coolant gas |
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EP2724100A2 (en) | 2014-04-30 |
SI2724100T1 (en) | 2021-04-30 |
WO2012175889A2 (en) | 2012-12-27 |
HUE053378T2 (en) | 2021-06-28 |
BR112013033341A2 (en) | 2017-01-31 |
CY1124080T1 (en) | 2022-05-27 |
BR112013033341B1 (en) | 2021-02-09 |
FR2977015A1 (en) | 2012-12-28 |
ES2854990T3 (en) | 2021-09-23 |
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