FR2923000A1 - Raw natural gas liquefaction method for producing liquid natural gas, involves recycling portion of fraction enriched in ethane by introducing portion of fraction in disengager, and liquefying gas phase to produce liquid natural gas - Google Patents
Raw natural gas liquefaction method for producing liquid natural gas, involves recycling portion of fraction enriched in ethane by introducing portion of fraction in disengager, and liquefying gas phase to produce liquid natural gas Download PDFInfo
- Publication number
- FR2923000A1 FR2923000A1 FR0707602A FR0707602A FR2923000A1 FR 2923000 A1 FR2923000 A1 FR 2923000A1 FR 0707602 A FR0707602 A FR 0707602A FR 0707602 A FR0707602 A FR 0707602A FR 2923000 A1 FR2923000 A1 FR 2923000A1
- Authority
- FR
- France
- Prior art keywords
- fraction
- ethane
- enriched
- column
- natural gas
- 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
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 92
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 title claims abstract description 81
- 239000003345 natural gas Substances 0.000 title claims abstract description 28
- 239000007789 gas Substances 0.000 title claims abstract description 14
- 239000003949 liquefied natural gas Substances 0.000 title claims abstract description 11
- 238000004064 recycling Methods 0.000 title claims description 3
- 238000004519 manufacturing process Methods 0.000 title 1
- 239000007788 liquid Substances 0.000 claims abstract description 38
- 238000000034 method Methods 0.000 claims abstract description 33
- 239000007791 liquid phase Substances 0.000 claims abstract description 19
- 238000005194 fractionation Methods 0.000 claims description 28
- 238000010992 reflux Methods 0.000 claims description 25
- 238000001816 cooling Methods 0.000 claims description 11
- 150000001875 compounds Chemical class 0.000 claims description 7
- FGUUSXIOTUKUDN-IBGZPJMESA-N C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 Chemical compound C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 FGUUSXIOTUKUDN-IBGZPJMESA-N 0.000 claims description 6
- 239000007792 gaseous phase Substances 0.000 claims description 6
- 229910052799 carbon Inorganic materials 0.000 claims description 2
- 239000012071 phase Substances 0.000 abstract description 4
- 238000011084 recovery Methods 0.000 description 10
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 6
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 6
- 229930195733 hydrocarbon Natural products 0.000 description 6
- 150000002430 hydrocarbons Chemical class 0.000 description 6
- 239000000203 mixture Substances 0.000 description 5
- 239000003507 refrigerant Substances 0.000 description 4
- 238000005057 refrigeration Methods 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 3
- 229910052753 mercury Inorganic materials 0.000 description 3
- 239000001294 propane Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000004088 simulation Methods 0.000 description 2
- 239000012808 vapor phase Substances 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- -1 comprises methane Chemical compound 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
- F25J1/0231—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the working-up of the hydrocarbon feed, e.g. reinjection of heavier hydrocarbons into the liquefied gas
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- 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
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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
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0235—Heat exchange integration
- F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
- F25J1/0239—Purification or treatment step being integrated between two refrigeration cycles of a refrigeration cascade, i.e. first cycle providing feed gas cooling and second cycle providing overhead gas cooling
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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
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0235—Heat exchange integration
- F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
- F25J1/0239—Purification or treatment step being integrated between two refrigeration cycles of a refrigeration cascade, i.e. first cycle providing feed gas cooling and second cycle providing overhead gas cooling
- F25J1/0241—Purification or treatment step being integrated between two refrigeration cycles of a refrigeration cascade, i.e. first cycle providing feed gas cooling and second cycle providing overhead gas cooling wherein the overhead cooling comprises providing reflux for a fractionation step
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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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
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- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/50—Processes or apparatus using other separation and/or other processing means using absorption, i.e. with selective solvents or lean oil, heavier CnHm and including generally a regeneration step for the solvent or lean oil
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- F25J2215/62—Ethane or ethylene
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- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid 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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising loop
Abstract
Description
La présente invention concerne le domaine de la liquéfaction du gaz naturel. The present invention relates to the field of liquefaction of natural gas.
Un gaz naturel brut comporte principalement du méthane, ainsi que différents constituants tels que l'eau, l'hydrogène sulfureux, le dioxyde de carbone, le mercure, l'azote et des hydrocarbures légers comportant généralement entre deux et six atomes de carbones. Certains de ces constituants tels que l'eau, l'hydrogène sulfureux, le dioxyde de carbone et le mercure, sont des polluants qui sont éliminés en amont des étapes de liquéfaction du gaz naturel. Les hydrocarbures plus lourds que le méthane sont condensés et récupérés en tant que liquides de gaz naturel qui peuvent être valorisés. Les liquides de gaz naturel sont séparés du méthane au moyen d'une colonne de fractionnement et par refroidissement et liquéfaction partielle du gaz naturel. Le gaz obtenu en tête de la colonne de fractionnement est destiné à être liquéfié pour produire le gaz naturel liquide. Fonctionner à très haute pression permet de limiter l'énergie nécessaire à la liquéfaction. Cependant, la pression de fonctionnement de la colonne de fractionnement est limitée par la pression critique du mélange à séparer. A raw natural gas mainly comprises methane, as well as various constituents such as water, sulphurous hydrogen, carbon dioxide, mercury, nitrogen and light hydrocarbons generally having between two and six carbon atoms. Some of these constituents, such as water, sulphurous hydrogen, carbon dioxide and mercury, are pollutants that are removed upstream of the liquefaction stages of natural gas. Hydrocarbons heavier than methane are condensed and recovered as natural gas liquids that can be recovered. Natural gas liquids are separated from methane by means of a fractionation column and by cooling and partial liquefaction of the natural gas. The gas obtained at the top of the fractionation column is intended to be liquefied to produce the liquid natural gas. Operating at very high pressure limits the energy required for liquefaction. However, the operating pressure of the fractionation column is limited by the critical pressure of the mixture to be separated.
La présente invention a pour but d'améliorer la récupération de propane et d'augmenter la pression critique du gaz à liquéfier de manière à réaliser le fractionnement à plus haute pression, diminuant ainsi l'énergie nécessaire à la liquéfaction. L'invention consiste à recycler un flux d'éthane dans la ligne de reflux de la colonne de fractionnement ou dans le ballon de reflux du fractionnement. The present invention aims to improve the recovery of propane and increase the critical pressure of the gas to be liquefied so as to achieve the fractionation at higher pressure, thus reducing the energy required for liquefaction. The invention involves recycling a stream of ethane into the reflux line of the fractionation column or into the reflux flask of the fractionation.
De manière générale, l'invention décrit un procédé de liquéfaction d'un gaz naturel dans lequel on effectue les étapes suivantes : a) on liquéfie partiellement le gaz naturel par refroidissement, b) on introduit le gaz naturel partiellement liquéfié dans une colonne de 30 fractionnement de manière à obtenir une fraction gazeuse enrichie en méthane et une fraction liquide appauvrie en méthane, c) on refroidit la fraction gazeuse jusqu'à liquéfaction partielle, puis on introduit la fraction gazeuse refroidie dans un ballon séparateur de rnanière à séparer une phase gazeuse et une phase liquide, d) on recycle au moins une partie de la phase liquide dans la colonne de fractionnement à titre de reflux, e) on sépare la fraction liquide de manière à obtenir une fraction enrichie en éthane et au moins une fraction enrichie en composés plus lourds que l'éthane, f) on recycle au moins une partie de la fraction enrichie en éthane en effectuant au moins l'une des opérations suivantes : on introduit ladite partie de la fraction enrichie en éthane dans ledit ballon séparateur, avant l'étape d), on mélange ladite partie de la fraction enrichie en éthane avec ladite phase liquide, g) on liquéfie la phase gazeuse obtenu à l'étape c) par refroidissement puis par détente de manière à produire un gaz naturel liquide. In general, the invention describes a process for liquefying a natural gas in which the following steps are carried out: a) partially liquefying the natural gas by cooling, b) introducing the partially liquefied natural gas into a column of 30 fractionation to obtain a gaseous fraction enriched in methane and a liquid fraction depleted in methane, c) the gaseous fraction is cooled to partial liquefaction, then the cooled gaseous fraction is introduced into a separating flask to separate a gaseous phase and a liquid phase, d) at least a portion of the liquid phase is recycled to the fractionation column as reflux, e) the liquid fraction is separated so as to obtain a fraction enriched in ethane and at least one fraction enriched in heavier than ethane, f) at least part of the ethane-enriched fraction is recycled by carrying out at least one of the following steps: introducing said portion of the ethane-enriched fraction into said separator flask, before step d), mixing said portion of the ethane-enriched fraction with said liquid phase, g) liquefying the gaseous phase obtained at step c) by cooling and then expanding to produce a liquid natural gas.
Selon l'invention, la fraction enrichie en éthane obtenue à l'étape e) peut comporter au moins 90% molaire d'éthane. According to the invention, the fraction enriched in ethane obtained in step e) may comprise at least 90 mol% of ethane.
A l'étape f), ladite au moins une partie de la fraction enrichie en éthane peut être recyclée à un débit compris entre 5 % et 20 % du débit d'éthane contenu dans ledit gaz naturel. Le procédé selon l'invention peut fonctionner dans les conditions suivantes : la colonne de fractionnement peut fonctionner à une pression comprise entre 40 bars et 60 bars, à l'étape a), le gaz naturel peut être refroidi à une température comprise entre 0°C et -60°C, et à l'étape c), on peut refroidir la fraction gazeuse jusqu'à une température comprise entre -45°C et -70°C. In step f), said at least a portion of the ethane-enriched fraction can be recycled at a flow rate of between 5% and 20% of the ethane flow rate contained in said natural gas. The process according to the invention can be operated under the following conditions: the fractionation column can operate at a pressure of between 40 bars and 60 bars, in step a), the natural gas can be cooled to a temperature of between 0 ° C. C and -60 ° C, and in step c), the gaseous fraction can be cooled to a temperature between -45 ° C and -70 ° C.
Selon une première alternative, à l'étape e), on peut séparer la fraction liquide dans une colonne de dééthanisation, ladite fraction enrichie en éthane étant obtenue en tête de la colonne de dééthanisation, la fraction enrichie en composés plus lourds que l'éthane étant obtenue en fond de la colonne de dééthanisation. De plus, la fraction enrichie en éthane peut être au moins partiellement liquéfiée, une partie de la fraction liquide enrichie en éthane étant introduite en tête de la colonne de dééthanisation à titre de reflux, une autre partie de la fraction liquide enrichie en éthane étant recyclée selon l'étape f). Selon la première alternative, la colonne de dééthanisation peut fonctionner à une pression comprise entre 20 et 35 bars, et ladite fraction enrichie en éthane peut être au moins partiellement liquéfiée par refroidissement à une température comprise entre -5°C et 10°C. According to a first alternative, in step e), the liquid fraction can be separated in a deethanization column, said ethane-enriched fraction being obtained at the top of the deethanization column, the fraction enriched in heavier compounds than ethane. being obtained at the bottom of the deethanization column. In addition, the fraction enriched in ethane may be at least partially liquefied, a part of the liquid fraction enriched in ethane being introduced at the top of the deethanization column as reflux, another portion of the liquid fraction enriched in ethane being recycled. according to step f). According to the first alternative, the deethanization column may operate at a pressure of between 20 and 35 bar, and said ethane-enriched fraction may be at least partially liquefied by cooling to a temperature between -5 ° C and 10 ° C.
Selon une deuxième alternative, à l'étape e), on peut séparer la fraction liquide dans une colonne de déméthanisation de manière à obtenir un flux gazeux enrichi en méthane et un flux liquide enrichi en composés plus lourds que le méthane, puis on peut séparer le flux liquide dans une colonne de dééthanisation, ladite fraction enrichie en éthane étant obtenue en tête de la colonne de dééthanisation, la fraction enrichie en composés plus lourds que l'éthane étant obtenue en fond de la colonne de dééthanisation. De plus, la fraction enrichie en éthane peut être au moins partiellement liiquéfiée, une partie de la fraction liquide enrichie en éthane étant introduite en tête de la colonne de dééthanisation à titre de reflux, une autre partie de la fraction liquide enrichie en éthane étant recyclée selon l'étape f). Selon la deuxième alternative, on peut introduire une portion de la phase liquide obtenue à l'étape c) en tête de la colonne de déméthanisation à titre de reflux. Selon la deuxième alternative, la colonne de déméthanisation peut fonctionner à une pression comprise entre 25 et 40 bars, la colonne de dééthanisation peut fonctionner à une pression comprise entre 20 et 35 bars, et ladite fraction enrichie en éthane peut être au moins partiellement liquéfiée par refroidissement à une température comprise entre -5°C et 10°C. According to a second alternative, in step e), the liquid fraction can be separated in a demethanizer column so as to obtain a gas stream enriched in methane and a liquid stream enriched in compounds heavier than methane, and then it is possible to separate the liquid flow in a deethanization column, said fraction enriched in ethane being obtained at the top of the deethanization column, the fraction enriched in heavier compounds than ethane being obtained at the bottom of the deethanization column. In addition, the fraction enriched in ethane can be at least partially liquefied, a part of the ethane-enriched liquid fraction being introduced at the top of the deethanization column as reflux, while another part of the ethane-enriched liquid fraction is recycled. according to step f). According to the second alternative, a portion of the liquid phase obtained in step c) can be introduced at the top of the demethanizer column as reflux. According to the second alternative, the demethanizer column can operate at a pressure of between 25 and 40 bar, the deethanization column can operate at a pressure of between 20 and 35 bar, and said fraction enriched in ethane can be at least partially liquefied by cooling at a temperature between -5 ° C and 10 ° C.
D'autres caractéristiques et avantages de l'invention seront 'mieux compris et apparaîtront clairement à la lecture de la description faite ci-après en se référant aux dessins parmi lesquels : la figure 1 schématise un procédé de liquéfaction avec fractionnement, les figures 2 à 5 schématisent différents modes de réalisation de l'invention. Other features and advantages of the invention will be better understood and will be clear from reading the description given below with reference to the drawings, in which: FIG. 1 schematizes a liquefaction process with fractionation, FIGS. 5 diagrammatically show different embodiments of the invention.
Sur la figure 1, le gaz naturel arrivant par le conduit 1 peut avoir été préalablement purifié des impuretés tels que l'eau, l'hydrogène sulfureux, le dioxyde de carbone et le mercure. Le gaz naturel est introduit dans l'échangeur de chaleur El pour être refroidi jusqu'à liquéfaction partielle. Dans El, le gaz naturel peut être refroidi jusqu'à une température comprise entre 0°C et -60°C. Dans El, la réfrigération est effectuée au moyen du circuit fermé de réfrigération Cl qui fonctionne par compression et détente d'un fluide réfrigérant. In Figure 1, the natural gas arriving through line 1 may have been previously purified impurities such as water, hydrogen sulphide, carbon dioxide and mercury. The natural gas is introduced into the heat exchanger E1 to be cooled to partial liquefaction. In El, the natural gas can be cooled to a temperature between 0 ° C and -60 ° C. In El, the refrigeration is carried out by means of the refrigeration closed circuit C1 which operates by compression and expansion of a refrigerant fluid.
Le flux partiellement liquéfié issu de El est introduit dans la zone de fractionnement F. La présente invention propose différents modes de réalisation de la zone F, décrits en référence aux figures 2 à 5. Les références des figures 2 à 5 identiques à celles de la figure 1 désignent les mêmes éléments. Les liquides de gaz naturel sont évacués sous forme de un ou plusieurs flux LGN. Le méthane 5 obtenu dans la zone F est sous-refroidi dans l'échangeur E2 jusqu'à liquéfaction complète. Dans E2, la réfrigération est effectuée au moyen du circuit fermé de réfrigération C2 qui fonctionne par compression et détente d'un fluide réfrigérant. Le gaz naturel liquide sous pression est évacué de E2 pour être détendu dans l'organe de détente V jusqu'à la pression atmosphérique pour produire le gaz naturel liquide GNL. The partially liquefied flow from El is introduced into fractionation zone F. The present invention proposes different embodiments of zone F, described with reference to FIGS. 2 to 5. The references of FIGS. 2 to 5 are identical to those of FIG. Figure 1 denote the same elements. Natural gas liquids are discharged as one or more NGL streams. The methane obtained in zone F is sub-cooled in exchanger E2 until complete liquefaction. In E2, the refrigeration is carried out by means of the refrigeration closed circuit C2 which operates by compression and expansion of a refrigerant fluid. The pressurized liquid natural gas is evacuated from E2 to be expanded in the expansion device V to atmospheric pressure to produce LNG liquid natural gas.
En référence aux figures 2 et 3, le gaz naturel 1 est refroidi et partiellement condensé dans l'échangeur El puis introduit dans Ila colonne de fractionnement 2. La colonne 2 fonctionne en général à une pression comprise entre 40 et 60 bars abs. La vapeur obtenue en tête de la colonne 2 est partiellement condensée par le condenseur 3. La phase gazeuse est séparée de la phase liquide dans le ballon 4. Le condenseur 3 effectue un refroidissement à très basse température, en général entre -45°C et -70°C, à l'aide d'un fluide réfrigérant, par exemple utilisé dans l'échangeur de chaleur E2. La phase gazeuse 5 est envoyée dans l'échangeur de chaleur E2 pour être liquéfiée. La 5 phase liquide obtenue en fond du ballon 4 est renvoyée à l'aide de la pompe 6 à travers le conduit 7 en tête de la colonne de fractionnement 2 à titre de reflux. La température en fond de la colonne est contrôlée par le rebouilleur 12 de manière à vaporiser les fractions légères présentes sous forme liquide en fond de la colonne 2 et à limiter leur entraînement dans le conduit 8. With reference to FIGS. 2 and 3, the natural gas 1 is cooled and partially condensed in the exchanger E1 and then introduced into the fractionation column 2. The column 2 generally operates at a pressure of between 40 and 60 bar abs. The vapor obtained at the top of the column 2 is partially condensed by the condenser 3. The gaseous phase is separated from the liquid phase in the flask 4. The condenser 3 performs cooling at a very low temperature, generally between -45.degree. -70 ° C, using a refrigerant, for example used in the heat exchanger E2. The gas phase 5 is sent into the heat exchanger E2 to be liquefied. The liquid phase obtained at the bottom of the flask 4 is returned by means of the pump 6 through the duct 7 at the top of the fractionation column 2 as reflux. The temperature at the bottom of the column is controlled by reboiler 12 so as to vaporize the light fractions present in liquid form at the bottom of column 2 and to limit their entrainment in line 8.
La phase liquide obtenue en fond de la colonne 2 est évacuée par le conduit 8 vers la colonne de dééthanisation 14. La colonne 14 peut fonctionner entre 20 et 35 bars abs. La colonne 14 permet de séparer un flux comportant principalement de l'éthane évacué en tête et un flux comportant des hydrocarbures plus lourds que l'éthane en fond. Le flux d'éthane obtenu en tête de la colonne 14 est partiellement, voire totalement condensé par le condenseur cryogénique 15 à une température comprise entre -5°C et 10°C. Le flux obtenu en sortie du condenseur 15 est envoyé dans le ballon de reflux 16. Dans le cas où le flux d'éthane n'est que partiellement condensé, une phase vapeur d'éthane est évacuée en tête du ballon 16. L'éthane liquide obtenu en fond de 16 est pompé par la pompe 17 pour être envoyé par le conduit 18 en tête de la colonne 14 à titre de reflux. Une fraction de l'éthane liquide obtenu en fond du ballon 16 peut être expédiée vers une zone de stockage par le conduit 20. Le fond de la colonne 14 est maintenue en température par le rebouilleur 21 de manière à éliminer le maximum d'éthane de la coupe C3+ évacuée en fond de 14 par le conduit 22. La coupe C3 peut être séparée, par exemple dans une colonne de dépropanisation. En référence aux figures 2 et 3, la présente invention propose de recycler une portion du flux riche en éthane liquide obtenu en fond du ballon 16 vers la colonne de fractionnement 2. Selon l'invention, le flux riche en éthane comporte au moins 90% molaire, de préférence plus de 98 % molaire, d'éthane. Plus précisément, en référence à la figure 2, une portion du flux liquide pompée par la pompe 17 est introduite par le conduit 19 dans le ballon 4. Alternativement, en référence à la figure 3, une portion du flux liquide pompé par la pompe 17 est introduite dans la ligne de reflux 7 par le conduit 19. Ainsi la phase liquide obtenue en fond du ballon 4 est assemblée et mélangée au flux riche en éthane arrivant par le conduit 19. The liquid phase obtained at the bottom of column 2 is discharged through line 8 to the deethanization column 14. Column 14 can operate between 20 and 35 bar abs. Column 14 makes it possible to separate a stream mainly comprising ethane discharged at the top and a stream comprising hydrocarbons heavier than ethane in the bottom. The ethane stream obtained at the top of the column 14 is partially or even completely condensed by the cryogenic condenser 15 at a temperature of between -5 ° C. and 10 ° C. The stream obtained at the outlet of the condenser 15 is sent to the reflux tank 16. In the case where the ethane stream is only partially condensed, an ethane vapor phase is discharged at the top of the balloon 16. Ethane liquid obtained at the bottom of 16 is pumped by the pump 17 to be sent through the conduit 18 at the top of the column 14 as reflux. A fraction of the liquid ethane obtained at the bottom of the flask 16 can be sent to a storage zone via the duct 20. The bottom of the column 14 is kept at temperature by the reboiler 21 so as to eliminate the maximum amount of ethane from the C3 + cut discharged at the bottom of 14 through the conduit 22. The C3 cut can be separated, for example in a depropanizer column. With reference to FIGS. 2 and 3, the present invention proposes to recycle a portion of the stream rich in liquid ethane obtained at the bottom of the flask 16 to the fractionation column 2. According to the invention, the stream rich in ethane comprises at least 90% molar, preferably more than 98 mol%, of ethane. More specifically, with reference to FIG. 2, a portion of the liquid flow pumped by the pump 17 is introduced via the conduit 19 into the balloon 4. Alternatively, with reference to FIG. 3, a portion of the liquid flow pumped by the pump 17 is introduced into the reflux line 7 through the conduit 19. Thus the liquid phase obtained at the bottom of the flask 4 is assembled and mixed with the flow rich in ethane arriving via the conduit 19.
Le recycle d'éthane selon l'invention permet d'augmenter significativement la récupération du propane en fond de la colonne de fractionnement 2. Pour obtenir un bon taux de récupération de propane on recycle un flux riche en éthane ayant un débit molaire d'éthane compris entre 5 % et 20 % molaire du débit molaire d'éthane contenu dans le gaz à traiter arrivant par le conduit 1. The ethane recycle according to the invention makes it possible to significantly increase the recovery of propane at the bottom of the fractionation column 2. In order to obtain a good propane recovery rate, a stream rich in ethane having a molar flow rate of ethane is recycled. between 5% and 20 mol% of the molar flow rate of ethane contained in the gas to be treated arriving via line 1.
De plus, l'arrivée d'éthane en tête de la colonne 2 permet d'augmenter légèrement la pression critique du fluide circulant dans la colonne 2 et donc améliore le fonctionnement de la séparation. Par ailleurs, le recycle d'éthane permet également d'enrichir le gaz naturel évacué en tête de la colonne 2 en éthane et donc de valoriser l'éthane et 15 d'augmenter le pouvoir calorifique du gaz naturel. In addition, the arrival of ethane at the top of column 2 makes it possible to slightly increase the critical pressure of the fluid flowing in column 2 and thus improves the operation of the separation. Moreover, the ethane recycle also makes it possible to enrich the natural gas discharged at the top of the column 2 into ethane and thus to enhance the ethane and to increase the heating value of the natural gas.
Les exemples numériques présentés ci-après permettent d'illustrer le mode de fonctionnement des procédés décrits en référence aux figures 2 et 3. The numerical examples presented below make it possible to illustrate the mode of operation of the methods described with reference to FIGS. 2 and 3.
7 Le débit de gaz naturel arrivant par le conduit 1 est de 34000 kmol/h, avec la composition suivante : Composant Composition (% mol) N2 0.9 Cl 90 C2 8 C3 0.5 iC4 0.1 nC4 0.1 iC5 0.05 nC5 0.05 nC6 0.05 nC7 0.05 nC8 0.05 nC9 0.05 Benzène 0.05 Toluène 0.05 Les procédés fonctionnent dans les conditions suivantes : • la colonne de fractionnement 2 : Pression : 45 bars abs en fond, 44 bars abs au condenseur 3, Température du gaz naturel à l'entrée : -30°C, - Température au condenseur 3 : - 65 °C ~o le dééthaniseur 14 : Pression : 27,5 bars abs en fond, 27 bar abs au condenseur 15, Température de l'alimentation : 42 °C Température au condenseur 15 : 3°C 7 The flow of natural gas arriving via line 1 is 34000 kmol / h, with the following composition: Component Composition (% mol) N2 0.9 Cl 90 C2 8 C3 0.5 iC4 0.1 nC4 0.1 iC5 0.05 nC5 0.05 nC6 0.05 nC7 0.05 nC8 0.05 nC9 0.05 Benzene 0.05 Toluene 0.05 The processes operate under the following conditions: • fractionation column 2: pressure: 45 bar abs at the bottom, 44 bar abs at the condenser 3, natural gas temperature at the inlet: -30 ° C , - Condenser temperature 3: - 65 ° C ~ o the deethanizer 14: Pressure: 27.5 bar abs at the bottom, 27 bar abs at the condenser 15, Supply temperature: 42 ° C Temperature at the condenser 15: 3 ° VS
8 Le taux de recycle, c'est-à-dire le débit molaire d'éthane recyclé par le conduit 19 par rapport au débit molaire d'éthane contenu dans le gaz arrivant par le conduit 1, est de 5%. The recycle rate, that is to say the molar flow rate of ethane recycled via line 19 with respect to the molar flow rate of ethane contained in the gas arriving via line 1, is 5%.
Le taux de récupération des C3 est défini comme le rapport entre le débit de C3 dans le conduit 22 par rapport au débit de C3 dans le conduit 1. The recovery rate of C3 is defined as the ratio between the flow rate of C3 in line 22 relative to the flow rate of C3 in line 1.
Les simulations de fonctionnement ont été effectuées pour le procédé décrit en référence à la figure 2, pour le procédé décrit en référence à la figure 3, ainsi que pour un procédé sans recycle de C2, c'est-à-dire pour un procédé identique à ceux présentés aux figures 2 et 3 à l'exception du fait qu'il est dépourvu du recycle de C2 matérialisé par la conduite de recycle 19. Schéma Procédé sans Procédé de la Procédé de la recycle de C2 figure 2 avec figure 3 avec recycle de C2 recycle de C2 dans le ballon de dans la ligne de reflux 4 reflux 7 Débit de C2 dans le recyclage (kmol/h) 0 136.4 136.4 Taux de récupération des 71.1 79.9 84.2 C3 (%) Pression critique en tête du 56.7 56.9 56.9 fractionnement 5 (bar) On constate que l'invention permet d'améliorer la récupération des C3 et de s'éloigner légèrement des conditions critiques dans la colonne de fractionnement et d'améliorer le taux de récupération des C3. The operating simulations were carried out for the method described with reference to FIG. 2, for the method described with reference to FIG. 3, as well as for a process without recycle of C2, that is to say for an identical process to those shown in Figures 2 and 3 except that it is devoid of recycle C2 materialized by the recycle line 19. Diagram Process without process of the recycle process C2 Figure 2 with Figure 3 with recycle of C2 recycle C2 in the flask in the reflux line 4 reflux 7 Flow rate of C2 in recycle (kmol / h) 0 136.4 136.4 Recovery rate of 71.1 79.9 84.2 C3 (%) Critical pressure at the top of 56.7 56.9 56.9 fractionation (bar) It is found that the invention makes it possible to improve the recovery of C3 and to move slightly away from critical conditions in the fractionation column and to improve the recovery rate of C3.
En référence aux figures 4 et 5, le gaz naturel 1 est refroidi et 20 partiellement condensé dans l'échangeur El, à une température comprise entre -60°C et 0°C, puis introduit dans la colonne de fractionnement 2. La colonne 2 peut fonctionner à une pression comprise entre 40 bars et 60 bars. La vapeur obtenue en tête de la colonne 2 est partiellement condensée par le condenseur 3. La phase gazeuse est séparée de la phase liquide dans le ballon 4. Le condenseur 3 effectue un refroidissement à très basse température, par exemple entre -45°C et -70°C, à l'aide d'un fluide réfrigérant, par exemple utilisé dans l'échangeur de chaleur E2. La phase gazeuse 5 est envoyée dans l'échangeur de chaleur E2 pour être liquéfiée. La phase liquide obtenue en fond du ballon 4 est renvoyée à l'aide de la pompe 6 à travers le conduit 7 en tête de la colonne de fractionnement 2 à titre de reflux. La phase liquide obtenue en fond de la colonne 2 est évacuée par le conduit 8 vers une deuxième colonne de fractionnement 9 pour effectuer une deuxième séparation entre le méthane et les hydrocarbures plus lourds que le méthane, à une pression inférieure à celle de la colonne 2. La colonne 9 peut fonctionner à une pression comprise entre 25 bars et 40 bars. Une portion de la phase liquide obtenue en fond du ballon 4 est introduite en tête de la colonne 9 à titre de reflux. La température en fond de la colonne 9 est contrôlée par le rebouilleur 12 de manière à vaporiser les fractions légères présentes sous forme liquide en fond de la colonne 9 et à limiter leur entraînement dans le conduit 13. With reference to FIGS. 4 and 5, natural gas 1 is cooled and partially condensed in exchanger E1 at a temperature between -60 ° C. and 0 ° C. and then introduced into fractionation column 2. Column 2 can operate at a pressure between 40 bar and 60 bar. The vapor obtained at the top of the column 2 is partially condensed by the condenser 3. The gaseous phase is separated from the liquid phase in the flask 4. The condenser 3 performs cooling at a very low temperature, for example between -45 ° C. and -70 ° C, using a refrigerant, for example used in the heat exchanger E2. The gas phase 5 is sent into the heat exchanger E2 to be liquefied. The liquid phase obtained at the bottom of the flask 4 is returned using the pump 6 through the conduit 7 at the top of the fractionation column 2 as reflux. The liquid phase obtained at the bottom of column 2 is discharged through line 8 to a second fractionation column 9 to effect a second separation between methane and hydrocarbons heavier than methane, at a pressure lower than that of column 2 The column 9 can operate at a pressure of between 25 bars and 40 bars. A portion of the liquid phase obtained at the bottom of the flask 4 is introduced at the top of the column 9 as reflux. The temperature at the bottom of the column 9 is controlled by the reboiler 12 so as to vaporize the light fractions present in liquid form at the bottom of the column 9 and to limit their entrainment in the conduit 13.
La colonne 9 permet d'obtenir, en tête, un flux enrichi en méthane évacué par le conduit 11 et, en fond, un flux enrichi en hydrocarbures plus lourds que le méthane. Le flux liquide obtenu en fond de la colonne 9 est introduit par le conduit 13 dans la colonne de dééthanisation 14. La colonne 14 fonctionne à une pression plus faible que dans la colonne 9, par exemple à une pression comprise entre 20 bars et 35 bars. La colonne 14 permet de séparer un flux comportant principalement de l'éthane évacué en tête et un flux comportant des hydrocarbures plus lourds que l'éthane en fond. Le flux d'éthane obtenu en tête de la colonne 14 est partiellement, voire totalement, condensé par le condenseur cryogénique 15 à une température comprise entre -5°C et 10°C. Le flux obtenu en sortie du condenseur 15 est envoyé dans le ballon de reflux 16. Dans le cas où le flux d'éthane n'est que partiellement condensé, une phase vapeur d'éthane est évacuée en tête du ballon 16. L'éthane liquide obtenu en fond de 16 est pompé par la pompe 17 pour être envoyé par le conduit 18, en tête, de la colonne 14 à titre de reflux. Une fraction de l'éthane liquide obtenu en fond du ballon 16 peut être expédiée vers une zone de stockage par le conduit 20. Le fond de la colonne 14 est maintenu en température par le rebouilleur 21 de manière à éliminer le maximum d'éthane de la coupe C3+ évacuée en fond de 14 par le conduit 22. La coupe C3+ peut être séparée, par exemple dans une colonne de dépropanisation. Column 9 makes it possible to obtain, at the top, a stream enriched in methane discharged through line 11 and, in bottom, a stream enriched in hydrocarbons heavier than methane. The liquid stream obtained at the bottom of the column 9 is introduced via the pipe 13 into the deethanization column 14. The column 14 operates at a lower pressure than in the column 9, for example at a pressure of between 20 bar and 35 bar . Column 14 makes it possible to separate a stream mainly comprising ethane discharged at the top and a stream comprising hydrocarbons heavier than ethane in the bottom. The ethane stream obtained at the top of the column 14 is partially or completely condensed by the cryogenic condenser 15 at a temperature of between -5 ° C. and 10 ° C. The stream obtained at the outlet of the condenser 15 is sent to the reflux tank 16. In the case where the ethane stream is only partially condensed, an ethane vapor phase is discharged at the top of the balloon 16. Ethane liquid obtained at the bottom of 16 is pumped by the pump 17 to be sent through the conduit 18 at the head of the column 14 as reflux. A fraction of the liquid ethane obtained at the bottom of the flask 16 can be sent to a storage zone via the conduit 20. The bottom of the column 14 is kept at temperature by the reboiler 21 so as to eliminate the maximum amount of ethane from the C3 + cut discharged at the bottom of 14 through line 22. The C3 + cut can be separated, for example in a depropanizer column.
En référence aux figures 4 et 5, la présente invention propose de recycler une portion du flux riche en éthane liquide obtenu en fond du ballon 16 vers la colonne de fractionnement 2. Plus précisément, en référence à la figure 4, une portion du flux liquide pompé par la pompe 17 est introduit par le conduit 19 dans le ballon 4. Alternativement, en référence à la figure 5, une portion du flux liquide pompé par la pompe 17 est introduite dans la ligne de reflux 7 par le conduit 19. Ainsi la phase liquide obtenue en fond du ballon 4 est assemblée et mélangée au flux riche en éthane arrivant par le conduit 19. With reference to FIGS. 4 and 5, the present invention proposes to recycle a portion of the stream rich in liquid ethane obtained at the bottom of the flask 16 to the fractionation column 2. More specifically, with reference to FIG. 4, a portion of the liquid flow pumped by the pump 17 is introduced through the conduit 19 into the balloon 4. Alternatively, with reference to FIG. 5, a portion of the liquid flow pumped by the pump 17 is introduced into the reflux line 7 via the conduit 19. liquid phase obtained at the bottom of the flask 4 is assembled and mixed with the stream rich in ethane arriving via the conduit 19.
Les exemples numériques présentés ci-après permettent d'illustrer le 20 mode de fonctionnement des procédés décrits en référence aux figures 4 et 5. The numerical examples presented below serve to illustrate the mode of operation of the methods described with reference to FIGS. 4 and 5.
11 Le débit de gaz naturel arrivant par le conduit 1 est de 34000 kmol/h, avec la composition suivante : Composant Composition (% mol) N2 0.9 Cl 90 C2 8 C3 0.5 iC4 0.1 nC4 0.1 iC5 0.05 nC5 0.05 nC6 0.05 nC7 0.05 nC8 0.05 nC9 0.05 Benzène 0.05 Toluène 0.05 Les procédés fonctionnent dans les conditions suivantes : 11 The flow of natural gas arriving via line 1 is 34000 kmol / h, with the following composition: Component Composition (% mol) N2 0.9 Cl 90 C2 8 C3 0.5 iC4 0.1 nC4 0.1 iC5 0.05 nC5 0.05 nC6 0.05 nC7 0.05 nC8 0.05 nC9 0.05 Benzene 0.05 Toluene 0.05 The processes operate under the following conditions:
• la colonne de fractionnement 2 : Pression : 45 bars abs en fond, 44 bars abs au condenseur 3, Température du gaz naturel à l'entrée : -30°C, Température au condenseur 15 : - 65 °C - Débit 10 de soutirage pour reflux du déméthaniseur 9 : 350 kmol/h • le déméthaniseur 9 : Pression : 30 bars abs en fond, 29,5 bar abs en tête, - Température de l'alimentation : - 41 °C • le dééthaniseur 14 : Pression : 27,5 bars abs en fond, 27 bars abs au condenseur 15, - Température de l'alimentation : 42 °C - Température au condenseur 15 : 3°C Le taux de recycle, c'est-à-dire le débit molaire d'éthane recyclé par le 5 conduit 19 par rapport au débit molaire d'éthane contenu dans le gaz arrivant par le conduit 1, est de 10%. Fractionation column 2: pressure: 45 bar abs at bottom, 44 bar abs at condenser 3, inlet natural gas temperature: -30 ° C., condenser temperature 15: 65 ° C. draw-off flow rate for the reflux of the demethanizer 9: 350 kmol / h • the demethanizer 9: Pressure: 30 bar abs at the bottom, 29.5 bar abs at the top, - Supply temperature: - 41 ° C • the deethanizer 14: Pressure: 27 , 5 bars abs at the bottom, 27 bars abs at the condenser 15, - Supply temperature: 42 ° C - Condenser temperature 15: 3 ° C The recycle rate, that is the molar flow rate The ethane recycled via line 19 with respect to the molar flow rate of ethane contained in the gas arriving via line 1 is 10%.
Le taux de récupération des C3 est défini comme le rapport entre le débit de C3 dans le conduit 22 par rapport au débit de C3 dans le conduit 1.The recovery rate of C3 is defined as the ratio between the flow rate of C3 in line 22 relative to the flow rate of C3 in line 1.
10 Les simulations de fonctionnement ont été effectuées pour le procédé décrit en référence à la figure 4, pour le procédé décrit en référence à la figure 5, ainsi que pour un procédé sans recycle de C2, c'est-à-dire pour un procédé identique à ceux présentés aux figures 4 et 5 à l'exception du fait qu'il est 15 dépourvu du recycle de C2 matérialisé par la conduite de recycle 19. Schéma Procédé sans Procédé selon la Procédé de la recycle de C2 figure 4 avec Figure 5 avec recycle de C2 recycle de C2 dans le ballon de dans la ligne de reflux 4 reflux 7 Débit de C2 dans le recyclage (kmol/h) 0 273 273 Taux de récupération des 62.4 76.6 82.6 C3 (%) Pression critique en tête du 56.7 56.9 56.9 fractionnement 5 (bar) On constate que l'invention permet d'améliorer la récupération des C3 et de s'éloigner des conditions critiques dans la colonne de fractionnement 20 spécialement lorsque le retour de recycle est effectué dans la ligne de reflux. The operating simulations were carried out for the method described with reference to FIG. 4, for the method described with reference to FIG. 5, as well as for a process without recycle of C2, that is to say for a process identical to those shown in FIGS. 4 and 5, except that it is devoid of the recycle of C2 materialized by the recycle line 19. Scheme Process without Process according to the Recycle Process of C2 FIG. 4 with FIG. with recycle of C2 recycle of C2 into the flask in the reflux line 4 reflux 7 Flow rate of C2 in recycle (kmol / h) 0 273 273 Recovery rate of 62.4 76.6 82.6 C3 (%) Critical pressure at the top of 56.7 56.9 56.9 fractionation (bar) It is found that the invention makes it possible to improve the recovery of C3 and to move away from the critical conditions in the fractionation column 20 especially when the recycle return is made in the reflux line.
Claims (11)
Priority Applications (6)
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FR0707602A FR2923000B1 (en) | 2007-10-26 | 2007-10-26 | METHOD FOR LIQUEFACTING NATURAL GAS WITH IMPROVED RECOVERY OF PROPANE |
US12/739,048 US20110265511A1 (en) | 2007-10-26 | 2008-10-17 | Natural gas liquefaction method with enhanced propane recovery |
PCT/FR2008/001461 WO2009087307A2 (en) | 2007-10-26 | 2008-10-17 | Method for liquefying natural gas with enhanced propane recovery |
EP08870226A EP2205921A2 (en) | 2007-10-26 | 2008-10-17 | Method for liquefying natural gas with enhanced propane recovery |
RU2010121164/06A RU2491487C2 (en) | 2007-10-26 | 2008-10-17 | Method of natural gas liquefaction with better propane extraction |
BRPI0818019 BRPI0818019A2 (en) | 2007-10-26 | 2008-10-17 | Liquefaction process of a natural gas with improved propane recovery |
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FR0707602A FR2923000B1 (en) | 2007-10-26 | 2007-10-26 | METHOD FOR LIQUEFACTING NATURAL GAS WITH IMPROVED RECOVERY OF PROPANE |
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FR2923000B1 FR2923000B1 (en) | 2015-12-11 |
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WO2017013329A1 (en) * | 2015-07-23 | 2017-01-26 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method for purifying a gas rich in hydrocarbons |
WO2022028729A1 (en) * | 2020-08-07 | 2022-02-10 | Linde Gmbh | Method and system for producing a liquefied natural gas product |
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US20130047632A1 (en) * | 2010-05-03 | 2013-02-28 | Consejo Superior De Investigaciones Cientificas (Csic) | Gas liquefaction system and method |
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US20160216030A1 (en) * | 2015-01-23 | 2016-07-28 | Air Products And Chemicals, Inc. | Separation of Heavy Hydrocarbons and NGLs from Natural Gas in Integration with Liquefaction of Natural Gas |
US10006701B2 (en) | 2016-01-05 | 2018-06-26 | Fluor Technologies Corporation | Ethane recovery or ethane rejection operation |
US10330382B2 (en) * | 2016-05-18 | 2019-06-25 | Fluor Technologies Corporation | Systems and methods for LNG production with propane and ethane recovery |
US11725879B2 (en) | 2016-09-09 | 2023-08-15 | Fluor Technologies Corporation | Methods and configuration for retrofitting NGL plant for high ethane recovery |
WO2019078892A1 (en) | 2017-10-20 | 2019-04-25 | Fluor Technologies Corporation | Phase implementation of natural gas liquid recovery plants |
JP7051372B2 (en) * | 2017-11-01 | 2022-04-11 | 東洋エンジニアリング株式会社 | Hydrocarbon separation method and equipment |
JP7043126B6 (en) * | 2017-11-06 | 2022-04-18 | 東洋エンジニアリング株式会社 | A device for separating and recovering multiple types of hydrocarbons from LNG |
CN109028758A (en) * | 2018-08-07 | 2018-12-18 | 中国石油工程建设有限公司 | A kind of natural gas ethane recovery device and method to be freezed using azeotrope |
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Also Published As
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US20110265511A1 (en) | 2011-11-03 |
RU2010121164A (en) | 2011-12-10 |
EP2205921A2 (en) | 2010-07-14 |
WO2009087307A2 (en) | 2009-07-16 |
BRPI0818019A2 (en) | 2015-04-14 |
FR2923000B1 (en) | 2015-12-11 |
WO2009087307A3 (en) | 2011-12-08 |
RU2491487C2 (en) | 2013-08-27 |
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