EP0818661A1 - Procédé et installation perfectionnés de refroidissement, en particulier pour la liquéfaction de gaz naturel - Google Patents
Procédé et installation perfectionnés de refroidissement, en particulier pour la liquéfaction de gaz naturel Download PDFInfo
- Publication number
- EP0818661A1 EP0818661A1 EP97401367A EP97401367A EP0818661A1 EP 0818661 A1 EP0818661 A1 EP 0818661A1 EP 97401367 A EP97401367 A EP 97401367A EP 97401367 A EP97401367 A EP 97401367A EP 0818661 A1 EP0818661 A1 EP 0818661A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- heat exchange
- fraction
- exchange means
- cooled
- separator
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000001816 cooling Methods 0.000 title claims abstract description 42
- 238000000034 method Methods 0.000 title claims abstract description 30
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims description 72
- 239000003345 natural gas Substances 0.000 title claims description 35
- 239000007788 liquid Substances 0.000 claims abstract description 78
- 230000006835 compression Effects 0.000 claims abstract description 73
- 238000007906 compression Methods 0.000 claims abstract description 73
- 239000000203 mixture Substances 0.000 claims abstract description 70
- 238000000926 separation method Methods 0.000 claims abstract description 36
- 239000002826 coolant Substances 0.000 claims abstract description 11
- 238000009833 condensation Methods 0.000 claims abstract description 7
- 230000005494 condensation Effects 0.000 claims abstract description 7
- 239000003507 refrigerant Substances 0.000 claims description 53
- 238000009434 installation Methods 0.000 claims description 39
- 238000004821 distillation Methods 0.000 claims description 32
- 239000012530 fluid Substances 0.000 claims description 29
- 238000001035 drying Methods 0.000 claims description 13
- 238000005057 refrigeration Methods 0.000 claims description 9
- 238000005194 fractionation Methods 0.000 claims description 4
- FGUUSXIOTUKUDN-IBGZPJMESA-N C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 Chemical compound C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 FGUUSXIOTUKUDN-IBGZPJMESA-N 0.000 claims description 3
- 239000013529 heat transfer fluid Substances 0.000 claims description 3
- 150000001875 compounds Chemical class 0.000 claims 2
- 239000007789 gas Substances 0.000 description 15
- 239000012071 phase Substances 0.000 description 11
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 9
- 238000002347 injection Methods 0.000 description 8
- 239000007924 injection Substances 0.000 description 8
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 6
- 241000287107 Passer Species 0.000 description 5
- 239000003949 liquefied natural gas Substances 0.000 description 5
- 239000012808 vapor phase Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 239000001273 butane Substances 0.000 description 3
- 229940082150 encore Drugs 0.000 description 3
- 235000021183 entrée Nutrition 0.000 description 3
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 3
- 239000001294 propane Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- VOPWNXZWBYDODV-UHFFFAOYSA-N Chlorodifluoromethane Chemical compound FC(F)Cl VOPWNXZWBYDODV-UHFFFAOYSA-N 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- 230000004323 axial length Effects 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 239000012809 cooling fluid Substances 0.000 description 2
- 208000028659 discharge Diseases 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 240000008042 Zea mays Species 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- -1 among others Substances 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Images
Classifications
-
- 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
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0042—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by liquid expansion with extraction of work
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
- F25J1/0055—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
-
- 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
- F25J1/008—Hydrocarbons
- F25J1/0092—Mixtures of hydrocarbons comprising possibly also minor amounts of nitrogen
-
- 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
- F25J1/0211—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
-
- 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
- F25J1/0211—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
- F25J1/0214—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 dual level refrigeration cascade with at least one MCR cycle
-
- 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
- F25J1/0211—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
- F25J1/0214—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 dual level refrigeration cascade with at least one MCR cycle
- F25J1/0215—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 dual level refrigeration cascade with at least one MCR cycle with one SCR cycle
-
- 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
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0262—Details of the cold heat exchange system
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0262—Details of the cold heat exchange system
- F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
- F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
- F25J1/0268—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer using a dedicated refrigeration means
-
- 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
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
-
- 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
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0291—Refrigerant compression by combined gas compression and liquid pumping
-
- 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
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
-
- 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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S62/00—Refrigeration
- Y10S62/912—External refrigeration system
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S62/00—Refrigeration
- Y10S62/912—External refrigeration system
- Y10S62/913—Liquified gas
Definitions
- the present invention relates to cooling of fluids and applies in particular to liquefaction of natural gas.
- WO-A-94 24500 (which is included in the present description by reference), is described such process in which you compress in at least two stages, in a cascade type installation integral, a refrigerant mixture composed of constituents different volatilities, and after at least each of intermediate stages of compression (i.e.
- stages preceding the last high pressure stage on partially condenses the refrigerant mixture, some at minus the condensed fractions as well as the fraction high pressure gas being cooled, expanded (or expanded) and put into heat exchange relationship with the fluid to be cooled, then compressed again, the gas from the penultimate compression stage being by elsewhere distilled in a distillation apparatus which cools the head with a liquid having a temperature below a so-called “reference” temperature, or “ambient”, to form on the one hand the liquid condensate of this penultimate compression stage and, on the other hand, a vapor phase which is sent at the last stage of compression.
- this same publication provides to partially cool and condense the vapor of head of the distillation apparatus, by heat exchange (in a heat exchanger unit with two heat exchangers plates arranged in series) with at least said fractions relaxed, to obtain a vapor phase and a phase liquid, and cool the camera head distillation with the liquid phase thus obtained, the phase vapor constituting said phase which is sent to the last compression stage.
- the refrigerant mixture which we have already spoken, should be considered to consist of a number of fluids including, among others, nitrogen and hydrocarbons such as methane, ethylene, ethane, propane, butane, pentane, etc ...
- thermodynamic reference temperature corresponding to the coolant temperature (water or air in particular) available on the site of use of the process and used in the cycle, increased by the difference of temperature which is fixed, by construction, to the removal of refrigerating appliances from the installation (compressor, exchanger, ).
- this difference will be from about 1 ° C to 20 ° C, and preferably of the order of 3 ° C to 15 ° C.
- step d) to cool the vapor fraction resulting from the separation of the condensed refrigerant, circulating this steam fraction in exchange for heat (indirect) with a refrigerant, in a second exchange unit thermal.
- the mechanical energy required for operation of this second "refrigeration unit” should, according to calculations, be less than 10% of the energy total mechanics required for the entire installation, this for example to train this second group by an electric motor from the launch engine of the gas turbine of the mixture compression unit refrigerant, then used as a generator.
- natural gas production liquefied could be increased by more than 10% by compared to the two stage compression solution of WO-A-94 24500.
- the technology of the hot exchanger of the first refrigerant unit is also simplified.
- the invention makes it possible to partially offload their thermal work, a part of said "first heat exchange unit", this allowing to optimize other elements of the cycle.
- step b) could possibly be deleted so that there is no refrigerant between the compressor outlet from the penultimate floor and the entrance to the aircraft separation (especially still), and thus do not condense the compressed refrigerant mixture before separate in step c).
- circulation of the liquid fraction from the separation of the compressed mixture in exchange means thermal marked 4A, 10, in EP-A-117 793 separate said "first heat exchange means" (marked 11, 15 in EP'793), before traveling there itself.
- the subject of the invention is also a cooling installation, in particular of liquefaction of natural gas, which can be used for the implementation of the process presented above.
- the installation of the invention comprises, as a means of cooling of the vapor fraction obtained at the outlet of said first separation unit, before the entry of this fraction steam in the last compression stage, second heat exchange means where this vapor fraction is going to be placed in exchange for heat with the refrigerant cited before.
- FIGS 1, 2, 3, 4, 5, 6 and 7 show as many possible embodiments of the installation of the invention that there are figures.
- Natural gas liquefaction facility represented in the figures, and in particular in FIG. 1, includes in particular a cycle 1 compression unit with two compression stages 1A, 1C, each discharge stage via a line 2A, 2C in a condenser or refrigerant, respectively 3A, 3C, cooled with water or air, the available fluid used having typically a temperature of the order of + 25 ° C to + 35 ° C; separation means identified as a whole 4, interposed between the two compression stages 1A and 1C of so as to supply the high pressure stage 1C with a steam fraction from these separation means; a first heat exchange unit 5 comprising two heat exchangers in series, namely an exchanger "hot” 6 and a "cold” exchanger 7; a separator pot intermediate 8; and a storage of liquefied natural gas (LNG) 10.
- a cycle 1 compression unit with two compression stages 1A, 1C, each discharge stage via a line 2A, 2C in a condenser or refrigerant, respectively 3A, 3C,
- the separation means 4 can be consisting either of a distillation apparatus 12, the upper head 12a is cooled by a liquid from a separator 13 ( Figures 1 to 5 and 7), or by two separator pots 14, 15, the vapor fraction of the distillation apparatus 12 or the first separator 14 circulating in the associated separator (respectively 13, 15) before being admitted to the input of the compression stage high pressure 1C.
- the output of the condenser 3A communicates with the lower part of tank 12b of the column distillation 12 and the bottom of the separator 13 is connected by gravity or by pump, via a siphon 16 and an adjustment valve 17, at the head 12a of the column 12.
- the gas liquefaction installation natural further includes, on the different modes of realization of Figures 1 to 7, a second exchange unit thermal 18 constituting a second refrigerant group, independent of the first, 5.
- auxiliary circuit 19 it can go to the hottest part of the exchanger 18 which is then used to cool from + 40 ° C to + 20 ° C approximately the heat transfer fluid which circulates there, this fluid (if it does not not natural gas) that can be used to refrigerate a other part of the installation, for example natural gas crude intended to be dried before processing in the installation.
- the fluid circulating in each of the cooling circuits above is cooled by indirect heat exchange with a coolant, such as a "pure" fluid, or mixture binary or ternary, circulating in a closed circuit in the regenerating cycle 21 or 21 '.
- a coolant such as a "pure" fluid, or mixture binary or ternary
- the circuit regeneration 21 comes as a refrigeration cycle with two compression stages, including a lower stage 1D pressure (of the order of 2.5 to 3.5 bars) and a stage of 1E high pressure compression (operating at approximately 6 to 8 bars), possibly a refrigerant 22, and a condenser 23 condensing the mixture in circulation.
- This mixture can in particular comprise about 60% butane and about 40% propane.
- a "pure” fluid can however be used, as an alternative.
- the mixture leaving the high pressure stage 1E is fully condensed in condenser 23, such so it's a liquid mixture that's allowed to the hot upper end (around 40 ° C) of the exchanger 18.
- the refrigerant mixture in gaseous state, can be cooled in the refrigerant 22, before being admitted at the inlet of the high pressure stage 1E, mixed with the part of the binary mixture that we recovered in 25, relaxed to a intermediate cycle pressure (of the order of ...) in 32, reintroduced into exchanger 18 for axial circulation about half the length of the exchanger, from so as to be vaporized in the axial passages 33, the vaporized mixture emerging axially through the dome higher "hot" 28b before being mixed in 35 with the part of the mixture in the gaseous state from stage 1D.
- Exchangers 6, 7 and 18 are preferably plate exchangers, these plates preferably being equipped with fins (or waves). These exchangers which are for example metallic plates and aluminum fins.
- two exchangers 6, 7 can be brazed or welded coaxially butt end, in series, for a counter-current circulation of fluids put in heat exchange relation, and can have the same length.
- the refrigerant mixture consisting of hydrocarbons in C1 to C6 and nitrogen, leaves in the gaseous state from vertex 6a (so-called "hot” end) of the exchanger 6 (via the passages 42) and arrives via the recycling line 46, at the suction of the first compression stage 1A.
- This gas mixture is then compressed to a first intermediate pressure Pi, typically of the order from 12 to 20 bars, then cooled to + 30 ° C to + ° 40 ° C approximately in 3A, with partial condensation, and separated in a vapor fraction and a liquid fraction in the device distillation 12.
- a first intermediate pressure Pi typically of the order from 12 to 20 bars
- the tank liquid in column 12 (recovered in 12b) constitutes a first suitable coolant to provide essential refrigeration of the exchanger hot 6, after cooling in the exchanger 18.
- this tank liquid is allowed (to around 30 ° C to 40 ° C) towards the "hot" end 28b of the exchanger 18 in which it circulates, as far as its "cold” end 28a, to come out at around 47 of 8 ° C, this cooled liquid fraction then being introduced at approximately the same temperature at the location an intermediate lateral entry 48, substantially mid-length of the hot exchanger 6, to come out of again laterally towards its "cold" end 6b, at around -20 ° C to -40 ° C, be relaxed (or undergo a expansion) at low cycle pressure (2.5 to 3.5 bar) in an expansion valve 50 and be reintroduced under two-phase form, always at the cold end 6b of the same exchanger, via the inlet side box 52 and a suitable dispensing device, to be vaporized in the low pressure passages 42 of the exchanger.
- the temperature reached may even (possibly) be lower than the temperature of the "coolant" available on site.
- the liquid phase recovered at the base of the separator 13 returns, via the siphon 16 and of the adjustment valve 17, at the head of the column 12 for the cool, while the vapor phase of the separator is compressed at the high pressure of the cycle (of the order of 40 to 45 bar) at 1C and then reduced to + 30 ° C to + 40 ° C in the 3C refrigerant.
- the temperature of the head of column 12 will therefore be lower than said temperature "ambient”, or even at the temperature of the "fluid cooling "available on the site, even if we would have could imagine that this temperature is higher, in particular by removing the 3A refrigerant and operating as in EP-A-117 793, that is to say with a direct passage from the compression stage lA to the entry into the distiller 12.
- the liquid collected at the base of the separator 8 is sub-cooled in the hot part of the exchanger 7, in passages 65, partly out of the exchanger intermediate (in 67) around -120 ° C, relaxed at low cycle pressure, for example in a valve trigger 69, and reintroduced laterally in 70, still in intermediate part of the exchanger, in the passages low pressure return 41 thereof.
- the vapor fraction from separator 8 is, meanwhile, cooled, condensed and sub-cooled (up to around -160 ° C) from the hot end to the cold end of the exchanger 7 and the liquid thus obtained is expanded at the low pressure of the cycle in an expansion valve 71 and reintroduced into the exchanger 7, parallel to the axis 5a, at through the lower "cold" dome 7b, to be vaporized in the cold part of the low pressure passages 41, then combined with two-phase fluids (mainly liquids) relaxed admitted by intermediate entry 70, for a return to line 46.
- two-phase fluids mainly liquids
- Processed natural gas for example arriving at a temperature of the order of 20 ° C. after drying, via a pipe 73 is, in part, admitted directly into the apparatus 75 for removing hydrocarbons in C2 + and, for its remaining part, admitted laterally in 77, substantially mid-length of exchanger 6, to be cooled to towards the cold end 6b in passages 79, before come out laterally towards this end, at 81, this portion cooled (approximately -20 ° C to -40 ° C) then being admitted in unit 75.
- the remaining mixture leaving at 83 is then admitted in 85, near the "hot” dome 7b of the exchanger "cold” 7, to circulate near its end cold 7b, in passages 87 while being liquefied and sub-cooled to come out in 89, around -160 ° C, before being stored, in liquid form (LNG), at 10, after being relaxed.
- LNG liquid form
- the expanders provided on the circulation paths of liquids may particular be used to drive pumps (not shown), the one providing the most power being that arranged in parallel with valve 69, the valves do not preferably for fine adjustment or trigger (expansion) of the liquid in question, in the event of failure of the (turbo-) corresponding expander.
- circuit 21 ' there will preferably be a ternary mixture, for example composed of ethane, butane and propane.
- the mixture under its vapor form is (totally) condensed in the 23 'condenser to be admitted 24' towards the end hot 28b of the exchanger 18 in which it circulates longitudinally (parallel to axis 18a) up to the cold end 28a, near which it emerges laterally in 26 'around 8 ° C to 10 ° C to be slackened by valve 27 up to around 2.5 to 3.5 bar.
- the refrigerant mixture thus cooled and relaxed is then reinjected through the cold dome 28a, parallel to axis 18a, against the current of the others circulation passages, in vaporization passages 33 'to exit coaxially through the "hot" dome 28b and always be introduced in vapor form around 30 ° C to 40 ° C at the inlet of compressor 1E '.
- the 21 'circuit which we also find in Figure 6, is simpler than circuit 21 but has an energy handicap of around 15 to 20% per compared to this circuit, i.e. approximately 1.5 to 2% over the cycle complete installation.
- the gas (via 99a) and liquid (via 99b) are then injected separately into the passages return of the cycle, spraying at low pressure.
- the vapor fraction is injected laterally at the cut 40, while that the liquid fraction is injected slightly more downstream, near the cold end 6b of the exchanger 6, via the lateral injection path 101 leading to 42.
- Comparable treatment of the liquid fraction from cycle separator 8 and expanded in the valve expansion 69 after having circulated in passages 65, to be sub-cooled, is performed in the third cycle separator 103.
- the gaseous and liquid from this separator are injected separately by separate injections, 105 and 107 respectively, substantially at the same intermediate level of the passages vaporization cold 41 of the exchanger 7, that is to say therefore further upstream of the return passages of the mixture refrigerant vaporized at low pressure as arrivals injection of steam and liquid fractions arriving from 99a and 99b.
- this gas After having passed in the passages 79 ' up to the cold end 6b of the exchanger 6, this gas natural thus sub-cooled leaves 81 'from exchanger 6 to pass into the exchanger 7, via an injection 109, before exiting through an intermediate outlet 111, after have been sub-cooled in passages 113, to a temperature of about -40 ° C to -60 ° C, the gas thus sub-cooled passing through the separation installation 75, its fraction which leaves in 83 then being reinjected laterally at 115 in the intermediate part of the exchanger 7 to circulate in cold passages 117 to around -160 ° C and thus be liquefied, before exit at 89 ', substantially at the exit 89 of the previous figures, then go through the valve expansion 119 (which could also be an expander) and finally be stored in the storage unit 10, after relaxation.
- the valve expansion 119 which could also be an expander
- part of the gas can be delivered to the separation unit 75, via the line 82, without passing there through the exchanger 7.
- the 21 "circuit of the refrigerant used in the exchanger 18 includes a circuit additional 121, connected in parallel, at input, between outlet 25 and the expansion valve 32 and, at the outlet, between condenser 22 (or low pressure condenser outlet 1D) and the mixing connection 35.
- the circuit 121 thus connected comprises a additional exchanger 123 in which circulates between its cold end 123a and its warmer end 123b, the binary liquefied refrigerant mixture leaving 25 and relaxed in 125 in an expansion valve, before being sprayed in passages 127, between the cold ends and hot heat exchanger 123, against the flow of a relatively wet natural gas (before drying), allowed in 129 and therefore circulating in the opposite direction to the vaporized fluid in 127, inside passages 131, before being introduced into a desiccation unit (not shown), then possibly to be introduced at the entry "GN" 73 to leave either in line 20 or directly to the separation installation 75.
- a partition of the lengths of the passages has also used to cool, in the part the less cold from exchanger 18 (passages 137), the mixture compressed two-phase leaving the 3A condenser, before admit it as a low input 12c from the distillation 12 (around 10 ° C to 15 ° C below "ambient" temperature), the complementary part of passages 137 (marked 137 ') located in the more heat exchanger 18 used to cool the liquid tank recovered in 12b, before admitting it into the entry lateral injection 48 of the exchanger 6.
- the traffic in the passages 137 of the partially condensed two-phase mixture and tablet provides an entry temperature into the first part 12 of the separation means 4 which can therefore be different from (less than) the "temperature ambient ", or even at the temperature of the cooling available on site.
- the circulation of high pressure steam fraction in passages 135 allows to obtain in 61 an inlet temperature of this fraction steam in exchanger 6, of the order of 25 ° C to 30 ° C that we can adapt and which can in particular be lower than the inlet temperature in 61 of the installation of FIG. 1, typically of the order of 40 ° C, that is to say close to the so-called “ambient” temperature (or the temperature of the "coolant").
- figure 5 corresponds to that of the figure 1 (the forecast of an expander 91 in parallel with the expansion valve 69 being optional).
- the liquid fraction recovered around 8 ° C in the lower part of the second separator 15 is transmitted towards the intermediate input 48, and a priori directly, without going through the exchanger 18.
- this liquid fraction from separator 15 meets the duct 145 used for the liquid fraction recovered from separator 14, after circulation substantially between the "hot” ends 28b and "cold” 28a of the exchanger 18, in the passages of indirect cooling 147.
- Adjustment valves respectively 149 and 151, allow to adapt the flow rate of liquid fractions from separators 14 and 15, respectively.
- the circulation of the liquid fraction of the separator 14 in the passages 147 allows passage its temperature of around 40 ° C around 8 ° C, temperature at which the liquid fraction of the separator 15 is recovered, due to its circulation in the passages 153 of exchanger 18, substantially in the same indirect heat exchange conditions as the fraction liquid flowing through passages 147.
- figure 7 differs from that of Figure 1 only (except the prediction of expander 91 in parallel with the valve trigger 69) because of the forecast not of two but of three compression stages on the compression unit of cycle 1 '.
- this intermediate compression stage and its accessories allows to separate in 155 in a vapor fraction and a liquid fraction the refrigerant mixture compressed into 1A and partially condensed into 3A, with cooling up to a temperature of + 30 ° C to + 40 ° C.
- the vapor phase from separator 155 is compressed at a second intermediate pressure Pi typically of the order of 12 to 20 bar, in 1B, while the liquid fraction recovered from the same separator 155 is carried by pump 157 at the same pressure Pi and injected in line 2B (or possibly leaving the partial condenser 3B).
- separators 9 and 103 this could also be applied in any other case.
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Compounds Of Unknown Constitution (AREA)
Abstract
Description
- ledit fluide (liquide) destiné au refroidissement de cette tête soit lui-même refroidi à une température inférieure à ladite température "de référence" ou "ambiante" (voire même inférieure à la température du fluide de refroidissement utilisé sur le site dans les échangeurs),
- et que la différence de température entre cette température "ambiante" et la température du fluide (liquide) destiné au refroidissement de la tête du distillateur soit comprise entre environ 20°C et 55°C, et typiquement de 30°C à 45°C.
- de séparer dans ledit appareil de distillation le mélange (partiellement) condensé,
- de condenser (à nouveau en partie) dans ladite seconde unité d'échange thermique la fraction vapeur issue de cet appareil de distillation, pour obtenir une fraction vapeur condensée,
- de faire passer dans un séparateur la fraction vapeur condensée, pour obtenir une fraction vapeur et une fraction liquide,
- d'envoyer la fraction vapeur issue du séparateur dans le dernier étage de compression,
- et de renvoyer la fraction liquide issue dudit séparateur dans la tête de colonne de l'appareil de distillation, pour la refroidir.
- on fait passer dans un second séparateur ladite fraction vapeur condensée pour obtenir une fraction vapeur et une fraction liquide,
- on envoie la fraction vapeur issue du second séparateur dans le dernier étage de compression,
- et on envoie la fraction liquide issue du second séparateur vers ladite première unité d'échange thermique.
- de faire circuler la fraction liquide issue de l'étape c) dans la seconde unité d'échange thermique, sensiblement entre les extrémités chaude et froide de l'unité,
- et d'admettre la fraction liquide ainsi refroidie, en partie intermédiaire d'un premier échangeur chaud parmi deux échangeurs de chaleur disposés en série, l'un chaud, l'autre froid, appartenant à ladite première unité d'échange thermique.
- à l'extérieur de la seconde unité d'échange thermique, on fait circuler le fluide réfrigérant dans un cycle de réfrigération en circuit fermé, soit à un étage unique de compression, soit à deux étages successifs de compression, avec, en sortie du réfrigérant final (23 sur la figure 1), une condensation totale du fluide réfrigérant;
- si le fluide à refroidir est du gaz naturel, avant d'admettre ce gaz naturel dans ladite première unité d'échange thermique, on le fait circuler d'abord dans ladite "seconde unité d'échange thermique" et, avant ou après sa circulation dans cette seconde unité, on fait passer le gaz naturel dans une unité de dessiccation ;
- lors de l'étape f) précitée, on refroidit la fraction vapeur haute pression après le dernier étage de compression, et on la fait circuler dans ladite seconde unité d'échange thermique, pour la refroidir encore par échange de chaleur avec le fluide réfrigérant avant de l'envoyer dans la première unité d'échange thermique,
- en sortie du dernier étage de compression de ladite unité de compression, on refroidit la fraction vapeur haute pression et on l'envoie dans une entrée intermédiaire d'un premier échangeur chaud, parmi deux échangeurs disposés en série, l'un chaud, l'autre froid, constituant ladite première unité d'échange thermique ;
- entre les étapes b) et c) susmentionnées, on fait circuler le mélange condensé dans la seconde unité d'échange thermique ;
- on fait circuler isolément un fluide caloporteur dans la seconde unité d'échange thermique ;
- dans l'hypothèse où le gaz à refroidir est du
gaz naturel,
- avant de faire circuler ce gaz naturel dans la première unité d'échange thermique, on lui fait subir une dessiccation,
- et, après dessiccation, on fait passer le gaz naturel sec, à l'intérieur de la première unité d'échange thermique, d'abord dans une première partie d'un premier échangeur chaud parmi deux échangeurs disposés en série, l'un chaud, l'autre froid, constituant ladite première unité d'échange thermique, puis dans une partie dudit second échangeur de cette première unité d'échange thermique, avant de passer dans une unité de fractionnement extérieure à ladite première unité d'échange thermique.
- de refroidir la fraction vapeur issue des premiers moyens de séparation 12 ou 14, avant qu'elle passe dans les seconds moyens de séparation 13, 15,
- de refroidir la fraction liquide issue desdits premiers moyens de séparation 12, 14, avant de l'envoyer dans le premier 6, des deux échangeurs de la première unité d'échange thermique 5,
- d'assurer un refroidissement d'un circuit auxiliaire 19 (figures 1,2 et 4 à 7) dans lequel circule soit du pentane, soit du gaz naturel avant décarbonatation et dessiccation (c'est-à-dire relativement humide),
- ou encore, par le circuit 20 de la figure 3, de refroidir du gaz naturel déjà sec mais non encore fractionné, avant de l'envoyer dans la première unité d'échange thermique 5 pour le liquéfier, avec élimination intermédiaire d'hydrocarbures en C2+, dans l'unité de fractionnement 75.
- les produits qui risqueraient de cristalliser lors de la liquéfaction (c'est-à-dire essentiellement les C6+),
- les produits en C2 à C5 nécessaires au maintien de la composition au gaz de cycle,
- et éventuellement les quantités de produits à extraire pour que le gaz naturel liquéfié soit conforme aux spécifications requises par les utilisateurs,
- et on produit la majeure partie du "fuel gaz" nécessaire à la production d'énergie mécanique de l'installation, directement à la pression requise.
- du fait de la circulation de la fraction vapeur haute pression sortant de 3C, avant que cette fraction vapeur parvienne à l'entrée latérale d'injection 61 de l'échangeur 6,
- et dans la manière dont le mélange frigorigène comprimé sortant du condenseur 3A est admis dans le distillateur 12, du fait qu'un refroidissement du mélange sortant de 3A est prévu en dessous de la température "ambiante" (et même éventuellement en dessous de la température du fluide de refroidissement disponible sur le site) avant entrée dans la colonne 12, ceci par circulation dans l'échangeur 18.
Claims (31)
- Procédé pour refroidir un fluide, notamment pour la liquéfaction de gaz naturel, dans lequel :a) on comprime un mélange frigorigène dans un avant-dernier étage (1A, 1B) parmi plusieurs étages d'une unité de compression (1, 1'),b) on condense partiellement le mélange, par refroidissement, pour obtenir un mélange condensé,c) on sépare le mélange condensé pour obtenir une fraction vapeur et une fraction liquide,d) on refroidit et on condense partiellement ladite fraction vapeur,e) on envoie la fraction vapeur résultante vers le dernier étage de compression (1C), pour obtenir une fraction vapeur haute pression,f) on refroidit, on expand et on fait circuler dans au moins des premiers moyens (5) d'échange thermique, avec le fluide à refroidir, au moins certaines parmi lesdites fraction vapeur haute pression et fraction liquide,
- Procédé selon la revendication 1,
caractérisé en ce que, lors des étapes c), d) et e) :on sépare le mélange condensé dans un premier séparateur (14),on condense la fraction vapeur issue dudit premier séparateur dans les seconds moyens d'échange thermique, pour obtenir une fraction de vapeur condensée,on fait passer dans un second séparateur (15) ladite fraction vapeur condensée, pour obtenir une fraction vapeur et une fraction liquide,on envoie la fraction vapeur issue du second séparateur dans ledit dernier étage de compression (1C),et on envoie la fraction liquide issue du second séparateur vers lesdits premiers moyens d'échange thermique (5). - Procédé selon la revendication 2,
caractérisé en ce que :on fait passer la fraction liquide issue du premier séparateur (14) dans les seconds moyens d'échange thermique (18),et, avant d'admettre la fraction liquide issue du second séparateur (15) dans les premiers moyens d'échange thermique (5), on réunit cette fraction liquide avec la fraction liquide ayant traversé lesdits seconds moyens d'échange thermique (18). - Procédé selon la revendication 1,
caractérisé en ce que, lors des étapes c), d) et e) :on sépare le mélange condensé dans un appareil de distillation (12),on condense la fraction vapeur issue de cet appareil de distillation dans lesdits seconds moyens d'échange thermique (18), pour obtenir une fraction vapeur condensée,on fait passer dans un séparateur (13) la fraction vapeur condensée, pour obtenir une fraction vapeur et une fraction liquide,on envoie la fraction vapeur issue du séparateur (13) dans le dernier étage de compression (1C),et on renvoie la fraction liquide issue dudit séparateur dans la tête (12a) de colonne de l'appareil de distillation, pour la refroidir. - Procédé selon l'une des revendications 2 à 4, caractérisé en ce que, lors de l'étape f), on fait circuler dans lesdits seconds moyens d'échange thermique (18) la fraction liquide issue de l'appareil de distillation (12) ou dudit premier séparateur (14) avant de l'admettre dans les premiers moyens d'échange thermique (5).
- Procédé selon la revendication 5,
caractérisé en ce que :on fait circuler la fraction liquide issue de l'appareil de distillation (12) ou du premier séparateur (14) dans les seconds moyens d'échange thermique (18), sensiblement entre une extrémité chaude (28b) et une extrémité froide (28a) de ces moyens d'échange thermique,et on admet la fraction liquide ainsi refroidie, en partie intermédiaire d'un premier échangeur chaud (6) parmi deux échangeurs de chaleur disposés en série, l'un chaud, l'autre froid (7), appartenant auxdits premiers moyens d'échange thermique (5). - Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce qu'on fait circuler le fluide réfrigérant dans un cycle de réfrigération en circuit fermé (21) à deux étages successifs de compression et, en sortie de l'étage de compression le plus élevé des deux (1E), on condense totalement le fluide réfrigérant.
- Procédé selon l'une quelconque des revendications 1 à 6, caractérisé en ce qu'on fait circuler le fluide réfrigérant dans un cycle (21') de réfrigération en circuit fermé à un étage unique de compression et, en sortie de cet étage de compression (1E'), on condense totalement le fluide réfrigérant.
- Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que, lors de l'étape f) :on refroidit la fraction vapeur haute pression après le dernier étage de compression (1C) de ladite unité de compression (1, 1'),et on fait circuler cette fraction vapeur refroidie dans les seconds moyens d'échange thermique (18), pour la refroidir encore par échange de chaleur avec le fluide réfrigérant avant de l'envoyer dans les premiers moyens d'échange thermique (5).
- Procédé selon les revendications 4 et 9,
caractérisé en ce que :pour refroidir encore la fraction vapeur haute pression refroidie, on la fait circuler entre une extrémité chaude (28b) desdits seconds moyens d'échange thermique (18) et une partie intermédiaire de ceux-ci,et on fait circuler entre sensiblement cette partie intermédiaire et une extrémité froide (28a) desdits seconds moyens d'échange thermique (18), ladite fraction vapeur issue de l'appareil de distillation (12), avant de l'envoyer dans ledit séparateur (15). - Procédé selon l'une quelconque des revendications 4 à 9, caractérisé en ce que l'on fait circuler essentiellement entre une extrémité chaude et une extrémité froide des seconds moyens d'échange thermique (18), les fractions vapeur et liquide issues de l'appareil de distillation (12), avant de les admettre respectivement dans ledit séparateur (15) et dans lesdits premiers moyens d'échange thermique (5).
- Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce qu'entre les étapes b) et c) de la revendication 1, on fait circuler le mélange condensé dans les seconds moyens d'échange thermique (18).
- Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que l'on fait circuler un fluide caloporteur dans les seconds moyens d'échange thermique (18).
- Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que :le fluide à refroidir est du gaz naturel,avant de faire circuler ce gaz naturel dans les premiers moyens d'échange thermique (5), on lui fait subir une dessiccation,et, après dessiccation, le gaz naturel sec passe, à l'intérieur des premiers moyens d'échange thermique (5), d'abord dans une première partie d'un premier échangeur chaud (6) parmi deux échangeurs disposés en série, l'un chaud, l'autre froid (7), appartenant auxdits premiers moyens d'échange thermique, puis dans une partie dudit second échangeur de ces premiers moyens d'échange thermique, avant de passer dans une unité de fractionnement (75) extérieure auxdits premiers moyens d'échange thermique.
- Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que :le fluide à refroidir est du gaz naturel,avant d'admettre ce gaz naturel dans ladite première unité d'échange thermique (5), on le fait passer successivement :dans des troisièmes moyens d'échange thermique (123), pour le refroidir par échange de chaleur avec le fluide réfrigérant,puis dans une unité intermédiaire de dessiccation.
- Procédé selon la revendication 15,
caractérisé en ce que l'on fait circuler le gaz naturel sortant de l'unité intermédiaire de dessiccation dans les seconds moyens d'échange thermique (18), avant de l'admettre dans les premiers moyens d'échange thermique (5). - Procédé selon l'une quelconque des revendications 1 à 14, caractérisé en ce que :le fluide à refroidir est du gaz naturel,avant d'admettre ce gaz naturel dans les premiers moyens d'échange thermique (5), on le fait circuler d'abord dans les seconds moyens d'échange thermique (18) et, avant ou après cette circulation dans les seconds moyens d'échange thermique, on fait subir au gaz naturel une dessiccation.
- Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que :le fluide à refroidir est du gaz naturel,on fait subir une dessiccation au gaz naturel avant de l'admettre, pour le refroidir, dans un premier échangeur chaud (6) parmi deux échangeurs disposés en série, l'un chaud, l'autre froid (7), appartenant auxdits premiers moyens d'échange thermique (5),on en refroidit au moins une partie dans une première partie du second échangeur froid (7),on le fait ensuite passer dans une unité de fractionnement (75) pour obtenir un composé résultant,et on fait circuler ledit composé résultant dans une deuxième partie du second échangeur froid (7), pour le liquéfier et le sous-refroidir.
- Procédé pour refroidir un fluide,
notamment pour la liquéfaction de gaz naturel, dans lequela) on comprime un mélange frigorigène dans un avant-dernier étage (1A, 1B) parmi plusieurs étages d'une unité de compression (1, 1'), pour obtenir un mélange comprimé,b) on sépare le mélange comprimé pour obtenir une fraction vapeur et une fraction liquide,c) on refroidit et on condense partiellement ladite fraction vapeur,d) on envoie la fraction vapeur résultante vers le dernier étage de compression (1C), pour obtenir une fraction vapeur haute pression,e) on refroidit, on expand et on fait circuler dans au moins des premiers moyens (5) d'échange thermique, avec le fluide à refroidir, au moins certaines parmi lesdites fraction vapeur haute pression et fraction liquide, ladite fraction liquide de l'étape b) circulant préalablement dans des seconds moyens d'échange thermique (18), en échange de chaleur avec un fluide réfrigérant, caractérisé en ce que, lors de l'étape c), on refroidit ladite fraction vapeur issue de la séparation dudit mélange comprimé de l'étape b), en la faisant circuler en échange de chaleur avec ledit fluide réfrigérant, dans les seconds moyens d'échange thermique (18). - Installation de refroidissement pour refroidir un fluide, l'installation comprenant :une unité de compression (1, 1') comprenant plusieurs étages de compression disposés en série, incluant un dernier étage de compression (1C) et un avant-dernier étage de compression (1A, 1B), pour comprimer au moins une partie d'un mélange frigorigène,des moyens de séparation (12, 13 ; 14, 15) disposés entre l'avant-dernier étage et le dernier étage de compression, pour obtenir une séparation du mélange frigorigène issu de l'avant dernier étage de compression, en une fraction vapeur et une fraction liquide, les moyens de séparation comprenant une sortie pour ladite fraction vapeur communiquant avec une entrée du dernier étage de compression et une sortie pour ladite fraction liquide,des moyens de refroidissement et de condensation (18), pour refroidir et condenser partiellement ladite fraction vapeur avant son entrée dans le dernier étage de compression (1C),et des premiers moyens d'échange thermique (5) ayant une sortie en communication avec une entrée de l'unité de compression et des entrées respectivement en communication avec une admission pour le fluide à refroidir, avec la sortie de fraction liquide desdits moyens de séparation et avec une sortie du dernier étage de compression,
- Installation selon la revendication 20,
caractérisée en ce que :lesdits moyens de séparation sont des premiers moyens de séparation (12, 14),et l'installation comprend en outre des seconds moyens de séparation (13, 15) interposés entre les seconds moyens d'échange thermique (18) et l'entrée du dernier étage de compression (1C), sur la communication entre la sortie de la fraction vapeur desdits premiers moyens de séparation (12, 14) et le dernier étage de compression (1C). - Installation selon la revendication 21,
caractérisée en ce que les premiers moyens de séparation comprennent un séparateur (14). - Installation selon la revendication 21
caractérisée en ce que les premiers moyens de séparation comprennent un appareil de distillation (12). - Appareil selon l'une des revendications 21 à 23, caractérisé en ce que les seconds moyens de séparation comprennent un séparateur (13, 15).
- Installation selon l'une quelconque des revendications 20 à 24, caractérisée en ce que les seconds moyens de séparation (13, 15) comprennent une sortie pour une fraction liquide communiquant avec ladite entrée de fraction liquide (48) des premiers moyens d'échange thermique (5).
- Installation selon l'une quelconque des revendications 20 à 25, caractérisée en ce que :les premiers moyens de séparation comprennent une entrée communiquant avec une sortie d'un condenseur (3A),et cette communication entre la sortie du condenseur et l'entrée des premiers moyens de séparation (12, 14) passe dans la seconde unité d'échange thermique (18).
- Installation selon l'une quelconque des revendications 20 à 26 caractérisée en ce que ledit fluide réfrigérant circule dans un cycle de réfrigération (21") comprenant :lesdits seconds moyens d'échange thermique (18),et des troisièmes moyens d'échange thermique (123) où passe, en échange thermique, le fluide réfrigérant et ledit fluide à refroidir.
- Installation selon l'une quelconque des revendications 20 à 27, caractérisée en ce que la communication entre la sortie du dernier étage de compression (1C) et l'entrée de fraction vapeur des premiers moyens d'échange thermique (5) passe dans les seconds moyens d'échange thermique (18).
- Installation selon l'une quelconque des revendications 20 à 28, caractérisée en ce qu'elle comprend un circuit de fluide frigorigène (19) passant dans les seconds moyens d'échange thermique (18).
- Installation selon l'une quelconque des revendications 20 à 29, caractérisée en ce que la communication entre ladite sortie de fraction liquide des moyens de séparation et l'entrée correspondante dans les premiers moyens d'échange thermique (5) passe à travers les seconds moyens d'échange thermique (18).
- Installation selon l'une quelconque des revendications 20 à 30, caractérisée en ce qu'elle comprend en outre des moyens (3A ; 3B) d'échange thermique avec un fluide de refroidissement disposés entre la sortie dudit avant-dernier étage de compression et l'entrée des moyens de séparation (12, 14), de façon à refroidir ledit mélange frigorigène sortant de l'avant dernier étage de compression avant de l'introduire dans les moyens de séparation.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9608758 | 1996-07-12 | ||
FR9608758A FR2751059B1 (fr) | 1996-07-12 | 1996-07-12 | Procede et installation perfectionnes de refroidissement, en particulier pour la liquefaction de gaz naturel |
Publications (2)
Publication Number | Publication Date |
---|---|
EP0818661A1 true EP0818661A1 (fr) | 1998-01-14 |
EP0818661B1 EP0818661B1 (fr) | 2002-09-11 |
Family
ID=9494005
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP97401367A Expired - Lifetime EP0818661B1 (fr) | 1996-07-12 | 1997-06-16 | Procédé et installation perfectionnés de refroidissement, en particulier pour la liquéfaction de gaz naturel |
Country Status (22)
Country | Link |
---|---|
US (1) | US5943881A (fr) |
EP (1) | EP0818661B1 (fr) |
JP (1) | JP4233619B2 (fr) |
KR (1) | KR100365367B1 (fr) |
CN (1) | CN1140755C (fr) |
AR (1) | AR007816A1 (fr) |
AT (1) | ATE224036T1 (fr) |
AU (1) | AU723530B2 (fr) |
BR (1) | BR9703959A (fr) |
CA (1) | CA2209723C (fr) |
CO (1) | CO5070650A1 (fr) |
DE (1) | DE69715330T2 (fr) |
DK (1) | DK0818661T3 (fr) |
DZ (1) | DZ2265A1 (fr) |
ES (1) | ES2185883T3 (fr) |
FR (1) | FR2751059B1 (fr) |
ID (1) | ID19101A (fr) |
IL (1) | IL121092A (fr) |
MY (1) | MY119081A (fr) |
NO (1) | NO311461B1 (fr) |
PT (1) | PT818661E (fr) |
TW (1) | TW332253B (fr) |
Families Citing this family (23)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH10329015A (ja) | 1997-03-24 | 1998-12-15 | Canon Inc | 研磨装置および研磨方法 |
US6119479A (en) * | 1998-12-09 | 2000-09-19 | Air Products And Chemicals, Inc. | Dual mixed refrigerant cycle for gas liquefaction |
US6347532B1 (en) | 1999-10-12 | 2002-02-19 | Air Products And Chemicals, Inc. | Gas liquefaction process with partial condensation of mixed refrigerant at intermediate temperatures |
US6298688B1 (en) | 1999-10-12 | 2001-10-09 | Air Products And Chemicals, Inc. | Process for nitrogen liquefaction |
US6564578B1 (en) | 2002-01-18 | 2003-05-20 | Bp Corporation North America Inc. | Self-refrigerated LNG process |
US6640586B1 (en) | 2002-11-01 | 2003-11-04 | Conocophillips Company | Motor driven compressor system for natural gas liquefaction |
DE102004011483A1 (de) * | 2004-03-09 | 2005-09-29 | Linde Ag | Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes |
US7266976B2 (en) * | 2004-10-25 | 2007-09-11 | Conocophillips Company | Vertical heat exchanger configuration for LNG facility |
US8578734B2 (en) | 2006-05-15 | 2013-11-12 | Shell Oil Company | Method and apparatus for liquefying a hydrocarbon stream |
US20110036120A1 (en) * | 2007-07-19 | 2011-02-17 | Marco Dick Jager | Method and apparatus for recovering and fractionating a mixed hydrocarbon feed stream |
EP2245403A2 (fr) | 2008-02-14 | 2010-11-03 | Shell Internationale Research Maatschappij B.V. | Procédé et appareil pour refroidir un courant d'hydrocarbures |
CN101239194B (zh) * | 2008-03-17 | 2012-11-28 | 张博 | 厕所除臭杀菌泡沫液 |
US8209997B2 (en) * | 2008-05-16 | 2012-07-03 | Lummus Technology, Inc. | ISO-pressure open refrigeration NGL recovery |
CN102115683A (zh) * | 2009-12-30 | 2011-07-06 | 中国科学院理化技术研究所 | 一种生产液化天然气的方法 |
CN105247190B (zh) | 2014-04-07 | 2017-04-05 | 三菱重工压缩机有限公司 | 浮体式液化气制造设备 |
FR3043451B1 (fr) * | 2015-11-10 | 2019-12-20 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Methode pour optimiser la liquefaction de gaz naturel |
FR3043452B1 (fr) * | 2015-11-10 | 2019-12-20 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procede de liquefaction de gaz naturel a l'aide d'un circuit de refrigeration en cycle ferme |
FR3045798A1 (fr) | 2015-12-17 | 2017-06-23 | Engie | Procede hybride de liquefaction d'un gaz combustible et installation pour sa mise en œuvre |
US10323880B2 (en) * | 2016-09-27 | 2019-06-18 | Air Products And Chemicals, Inc. | Mixed refrigerant cooling process and system |
CN106831300B (zh) * | 2017-04-17 | 2023-05-23 | 中国石油集团工程股份有限公司 | 一种乙烷回收联产液化天然气的装置与方法 |
US11248840B2 (en) * | 2017-12-15 | 2022-02-15 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
CA3095583A1 (fr) * | 2018-04-20 | 2019-10-24 | Chart Energy And Chemicals, Inc. | Systeme et procede de liquefaction de refrigerant mixte avec pre-refroidissement |
FR3103543B1 (fr) * | 2019-11-21 | 2021-10-22 | Air Liquide | Echangeur de chaleur avec agencement de dispositifs mélangeurs améliorant la distribution d’un mélange diphasique |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO1994024500A1 (fr) * | 1993-04-09 | 1994-10-27 | Gaz De France | Procede et installation de refroidissement d'un fluide, notamment pour la liquefaction de gaz naturel |
Family Cites Families (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2280041A1 (fr) * | 1974-05-31 | 1976-02-20 | Teal Technip Liquefaction Gaz | Procede et installation pour le refroidissement d'un melange gazeux |
FR2292203A1 (fr) * | 1974-11-21 | 1976-06-18 | Technip Cie | Procede et installation pour la liquefaction d'un gaz a bas point d'ebullition |
US4325231A (en) * | 1976-06-23 | 1982-04-20 | Heinrich Krieger | Cascade cooling arrangement |
FR2471566B1 (fr) * | 1979-12-12 | 1986-09-05 | Technip Cie | Procede et systeme de liquefaction d'un gaz a bas point d'ebullition |
FR2540612A1 (fr) * | 1983-02-08 | 1984-08-10 | Air Liquide | Procede et installation de refroidissement d'un fluide, notamment de liquefaction de gaz naturel |
US4755200A (en) * | 1987-02-27 | 1988-07-05 | Air Products And Chemicals, Inc. | Feed gas drier precooling in mixed refrigerant natural gas liquefaction processes |
DE19722490C1 (de) * | 1997-05-28 | 1998-07-02 | Linde Ag | Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes |
-
1996
- 1996-07-12 FR FR9608758A patent/FR2751059B1/fr not_active Expired - Lifetime
-
1997
- 1997-06-11 TW TW086108000A patent/TW332253B/zh not_active IP Right Cessation
- 1997-06-16 DK DK97401367T patent/DK0818661T3/da active
- 1997-06-16 EP EP97401367A patent/EP0818661B1/fr not_active Expired - Lifetime
- 1997-06-16 PT PT97401367T patent/PT818661E/pt unknown
- 1997-06-16 ES ES97401367T patent/ES2185883T3/es not_active Expired - Lifetime
- 1997-06-16 AT AT97401367T patent/ATE224036T1/de active
- 1997-06-16 DE DE69715330T patent/DE69715330T2/de not_active Expired - Lifetime
- 1997-06-17 AU AU24966/97A patent/AU723530B2/en not_active Expired
- 1997-06-17 IL IL12109297A patent/IL121092A/xx not_active IP Right Cessation
- 1997-06-25 MY MYPI97002852A patent/MY119081A/en unknown
- 1997-06-27 CO CO97036140A patent/CO5070650A1/es unknown
- 1997-07-07 ID IDP972347A patent/ID19101A/id unknown
- 1997-07-07 AR ARP970103019A patent/AR007816A1/es active IP Right Grant
- 1997-07-07 CA CA002209723A patent/CA2209723C/fr not_active Expired - Lifetime
- 1997-07-09 DZ DZ970115A patent/DZ2265A1/fr active
- 1997-07-10 NO NO19973221A patent/NO311461B1/no not_active IP Right Cessation
- 1997-07-10 US US08/891,133 patent/US5943881A/en not_active Expired - Lifetime
- 1997-07-11 BR BR9703959A patent/BR9703959A/pt not_active IP Right Cessation
- 1997-07-12 KR KR1019970032394A patent/KR100365367B1/ko not_active IP Right Cessation
- 1997-07-14 CN CNB971145717A patent/CN1140755C/zh not_active Expired - Lifetime
- 1997-07-14 JP JP18806697A patent/JP4233619B2/ja not_active Expired - Lifetime
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO1994024500A1 (fr) * | 1993-04-09 | 1994-10-27 | Gaz De France | Procede et installation de refroidissement d'un fluide, notamment pour la liquefaction de gaz naturel |
Also Published As
Publication number | Publication date |
---|---|
EP0818661B1 (fr) | 2002-09-11 |
KR100365367B1 (ko) | 2003-02-19 |
CO5070650A1 (es) | 2001-08-28 |
DZ2265A1 (fr) | 2004-07-04 |
AU2496697A (en) | 1998-01-22 |
JP4233619B2 (ja) | 2009-03-04 |
TW332253B (en) | 1998-05-21 |
NO311461B1 (no) | 2001-11-26 |
DK0818661T3 (da) | 2003-01-20 |
CA2209723C (fr) | 2005-05-24 |
NO973221L (no) | 1998-01-13 |
CN1172243A (zh) | 1998-02-04 |
KR980010302A (ko) | 1998-04-30 |
ES2185883T3 (es) | 2003-05-01 |
FR2751059B1 (fr) | 1998-09-25 |
AU723530B2 (en) | 2000-08-31 |
ATE224036T1 (de) | 2002-09-15 |
ID19101A (id) | 1998-06-11 |
AR007816A1 (es) | 1999-11-24 |
CN1140755C (zh) | 2004-03-03 |
FR2751059A1 (fr) | 1998-01-16 |
CA2209723A1 (fr) | 1998-01-12 |
BR9703959A (pt) | 1999-03-16 |
DE69715330D1 (de) | 2002-10-17 |
NO973221D0 (no) | 1997-07-10 |
IL121092A (en) | 2000-07-16 |
DE69715330T2 (de) | 2003-01-02 |
IL121092A0 (en) | 1997-11-20 |
JPH1068586A (ja) | 1998-03-10 |
US5943881A (en) | 1999-08-31 |
PT818661E (pt) | 2003-01-31 |
MY119081A (en) | 2005-03-31 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP0818661B1 (fr) | Procédé et installation perfectionnés de refroidissement, en particulier pour la liquéfaction de gaz naturel | |
EP0644996B1 (fr) | Procede et installation de refroidissement d'un gaz, notamment pour la liquefaction de gaz naturel | |
FR3053771B1 (fr) | Procede de liquefaction de gaz naturel et de recuperation d'eventuels liquides du gaz naturel comprenant deux cycles refrigerant semi-ouverts au gaz naturel et un cycle refrigerant ferme au gaz refrigerant | |
EP1352203B1 (fr) | Procede de refrigeration de gaz liquefie et installation mettant en oeuvre celui-ci | |
CA2269147C (fr) | Procede et dispositif de liquefaction d'un gaz naturel sans separation de phases sur les melanges refrigerants | |
FR2471567A1 (fr) | Procede et systeme de refrigeration d'un fluide a refroidir a basse temperature | |
EP0125980B1 (fr) | Procédé et appareil de refroidissement et liquéfaction d'au moins un gaz à bas point d'ébullition, tel que par exemple du gaz naturel | |
CA1054922A (fr) | Procede et installation pour la liquefaction d'un gaz a bas point d'ebullition | |
CA1050413A (fr) | Procede et installation pour le refroidissement d'un melange gazeux | |
FR2611386A1 (fr) | Procede perfectionne pour liquefier un flux d'alimentation en gaz naturel, en utilisant un ou deux refrigerants en circuit ferme a plusieurs composants | |
CA2194089C (fr) | Procede et dispositif de liquefaction en deux etapes d'un melange gazeux, tel qu'un gaz naturel | |
FR2675891A1 (fr) | Procede de production d'azote liquide en utilisant un gaz naturel liquefie comme seul refrigerant. | |
FR2471566A1 (fr) | Procede et systeme de liquefaction d'un gaz a bas point d'ebullition | |
EP1118827B1 (fr) | Procédé de liquéfaction partielle d'un fluide contenant des hydrocarbures tel que du gaz naturel | |
FR2714722A1 (fr) | Procédé et appareil de liquéfaction d'un gaz naturel. | |
FR2675888A1 (fr) | Procede a l'utilisation du gaz naturel liquefie (gnl) associe a un expanseur a froid pour produire de l'azote liquide. | |
FR2764972A1 (fr) | Procede de liquefaction d'un gaz naturel a deux etages interconnectes | |
FR3053770B1 (fr) | Procede de liquefaction de gaz naturel et de recuperation d'eventuels liquides du gaz naturel comprenant un cycle refrigerant semi-ouvert au gaz naturel et deux cycles refrigerant fermes au gaz refrigerant | |
FR2723183A1 (fr) | Procede et installation de liquefaction d'hydrogene | |
EP2417411B1 (fr) | Procede et systeme frigorifique pour la recuperation de la froideur du methane par des fluides frigorigenes | |
FR2479846A1 (fr) | Procede de refrigeration, pour la recuperation ou le fractionnement d'un melange compose principalement de butane et propane, contenu dans un gaz brut, par utilisation d'un cycle mecanique exterieur | |
FR2714720A1 (fr) | Procédé et appareil de liquéfaction d'un gaz naturel. | |
OA19019A (en) | Procédé de liquéfaction de gaz naturel et de récupération d'éventuels liquides du gaz naturel comprenant deux cycles réfrigérant semi-ouverts au gaz naturel et un cycle réfrigérant fermé au gaz réfrigérant | |
MXPA97005256A (en) | Procedure and installation to cool a flu |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
|
AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): AT BE CH DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE |
|
17P | Request for examination filed |
Effective date: 19980613 |
|
AKX | Designation fees paid |
Free format text: AT BE CH DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE |
|
RBV | Designated contracting states (corrected) |
Designated state(s): AT BE CH DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE |
|
17Q | First examination report despatched |
Effective date: 20000529 |
|
GRAG | Despatch of communication of intention to grant |
Free format text: ORIGINAL CODE: EPIDOS AGRA |
|
GRAG | Despatch of communication of intention to grant |
Free format text: ORIGINAL CODE: EPIDOS AGRA |
|
GRAH | Despatch of communication of intention to grant a patent |
Free format text: ORIGINAL CODE: EPIDOS IGRA |
|
GRAH | Despatch of communication of intention to grant a patent |
Free format text: ORIGINAL CODE: EPIDOS IGRA |
|
GRAA | (expected) grant |
Free format text: ORIGINAL CODE: 0009210 |
|
AK | Designated contracting states |
Kind code of ref document: B1 Designated state(s): AT BE CH DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE |
|
REF | Corresponds to: |
Ref document number: 224036 Country of ref document: AT Date of ref document: 20020915 Kind code of ref document: T |
|
REG | Reference to a national code |
Ref country code: GB Ref legal event code: FG4D Free format text: NOT ENGLISH |
|
REG | Reference to a national code |
Ref country code: CH Ref legal event code: EP |
|
REG | Reference to a national code |
Ref country code: IE Ref legal event code: FG4D Free format text: FRENCH |
|
REF | Corresponds to: |
Ref document number: 69715330 Country of ref document: DE Date of ref document: 20021017 |
|
GBT | Gb: translation of ep patent filed (gb section 77(6)(a)/1977) |
Effective date: 20021223 |
|
REG | Reference to a national code |
Ref country code: CH Ref legal event code: NV Representative=s name: LUCHS & PARTNER PATENTANWAELTE |
|
REG | Reference to a national code |
Ref country code: DK Ref legal event code: T3 |
|
REG | Reference to a national code |
Ref country code: PT Ref legal event code: SC4A Free format text: AVAILABILITY OF NATIONAL TRANSLATION Effective date: 20021210 |
|
REG | Reference to a national code |
Ref country code: GR Ref legal event code: EP Ref document number: 20020404209 Country of ref document: GR |
|
REG | Reference to a national code |
Ref country code: ES Ref legal event code: FG2A Ref document number: 2185883 Country of ref document: ES Kind code of ref document: T3 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: LU Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20030616 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: MC Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20030630 |
|
PLBE | No opposition filed within time limit |
Free format text: ORIGINAL CODE: 0009261 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT |
|
26N | No opposition filed |
Effective date: 20030612 |
|
REG | Reference to a national code |
Ref country code: CH Ref legal event code: PFA Owner name: GDF SUEZ SOCIETE ANONYME Free format text: GAZ DE FRANCE (SERVICE NATIONAL)#23 RUE PHILIBERT-DELORME#F-75017 PARIS (FR) -TRANSFER TO- GDF SUEZ SOCIETE ANONYME#12-26 RUE DU DOCTEUR LANCEREAUX#75008 PARIS (FR) |
|
NLT1 | Nl: modifications of names registered in virtue of documents presented to the patent office pursuant to art. 16 a, paragraph 1 |
Owner name: GDF SUEZ |
|
REG | Reference to a national code |
Ref country code: FR Ref legal event code: CJ Ref country code: FR Ref legal event code: CD Ref country code: FR Ref legal event code: CA |
|
REG | Reference to a national code |
Ref country code: DE Ref legal event code: R082 Ref document number: 69715330 Country of ref document: DE Representative=s name: WSL PATENTANWAELTE PARTNERSCHAFTSGESELLSCHAFT, DE |
|
REG | Reference to a national code |
Ref country code: DE Ref legal event code: R082 Ref document number: 69715330 Country of ref document: DE Representative=s name: WSL PATENTANWAELTE PARTNERSCHAFT MBB, DE Effective date: 20111028 Ref country code: DE Ref legal event code: R081 Ref document number: 69715330 Country of ref document: DE Owner name: GDF SUEZ S.A., FR Free format text: FORMER OWNER: GAZ DE FRANCE (SERVICE NATIONAL), PARIS, FR Effective date: 20111028 |
|
REG | Reference to a national code |
Ref country code: AT Ref legal event code: PC Ref document number: 224036 Country of ref document: AT Kind code of ref document: T Owner name: GDF SUEZ, FR Effective date: 20130328 |
|
REG | Reference to a national code |
Ref country code: FR Ref legal event code: PLFP Year of fee payment: 20 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: NL Payment date: 20160525 Year of fee payment: 20 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: DE Payment date: 20160524 Year of fee payment: 20 Ref country code: ES Payment date: 20160525 Year of fee payment: 20 Ref country code: GB Payment date: 20160527 Year of fee payment: 20 Ref country code: IE Payment date: 20160524 Year of fee payment: 20 Ref country code: CH Payment date: 20160523 Year of fee payment: 20 Ref country code: FI Payment date: 20160524 Year of fee payment: 20 Ref country code: GR Payment date: 20160524 Year of fee payment: 20 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: IT Payment date: 20160525 Year of fee payment: 20 Ref country code: FR Payment date: 20160526 Year of fee payment: 20 Ref country code: SE Payment date: 20160527 Year of fee payment: 20 Ref country code: BE Payment date: 20160525 Year of fee payment: 20 Ref country code: DK Payment date: 20160524 Year of fee payment: 20 Ref country code: AT Payment date: 20160524 Year of fee payment: 20 Ref country code: PT Payment date: 20160601 Year of fee payment: 20 |
|
REG | Reference to a national code |
Ref country code: DE Ref legal event code: R071 Ref document number: 69715330 Country of ref document: DE |
|
REG | Reference to a national code |
Ref country code: DK Ref legal event code: EUP Effective date: 20170616 |
|
REG | Reference to a national code |
Ref country code: NL Ref legal event code: MK Effective date: 20170615 |
|
REG | Reference to a national code |
Ref country code: CH Ref legal event code: PL |
|
REG | Reference to a national code |
Ref country code: GB Ref legal event code: PE20 Expiry date: 20170615 |
|
REG | Reference to a national code |
Ref country code: IE Ref legal event code: MK9A |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: GB Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION Effective date: 20170615 |
|
REG | Reference to a national code |
Ref country code: SE Ref legal event code: EUG |
|
REG | Reference to a national code |
Ref country code: AT Ref legal event code: MK07 Ref document number: 224036 Country of ref document: AT Kind code of ref document: T Effective date: 20170616 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: PT Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION Effective date: 20170623 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: IE Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION Effective date: 20170616 |
|
REG | Reference to a national code |
Ref country code: ES Ref legal event code: FD2A Effective date: 20180508 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: ES Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION Effective date: 20170617 |