EP3058296B1 - Verfahren zur stickstoffentfernung aus erdgas mit oder ohne heliumgewinnung - Google Patents
Verfahren zur stickstoffentfernung aus erdgas mit oder ohne heliumgewinnung Download PDFInfo
- Publication number
- EP3058296B1 EP3058296B1 EP14799510.4A EP14799510A EP3058296B1 EP 3058296 B1 EP3058296 B1 EP 3058296B1 EP 14799510 A EP14799510 A EP 14799510A EP 3058296 B1 EP3058296 B1 EP 3058296B1
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- column
- gas
- natural gas
- turbine
- sent
- Prior art date
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims description 97
- 239000003345 natural gas Substances 0.000 title claims description 33
- 238000000034 method Methods 0.000 title claims description 21
- 239000001307 helium Substances 0.000 title description 6
- 229910052734 helium Inorganic materials 0.000 title description 6
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 title description 6
- 238000011084 recovery Methods 0.000 title description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 31
- 239000007789 gas Substances 0.000 claims description 31
- 239000007788 liquid Substances 0.000 claims description 27
- 229910052757 nitrogen Inorganic materials 0.000 claims description 15
- 238000004821 distillation Methods 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 3
- 238000009834 vaporization Methods 0.000 claims description 3
- 238000011144 upstream manufacturing Methods 0.000 claims description 2
- 230000006835 compression Effects 0.000 description 5
- 238000007906 compression Methods 0.000 description 5
- 239000012530 fluid Substances 0.000 description 5
- 239000006200 vaporizer Substances 0.000 description 3
- 238000000605 extraction Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- QGZKDVFQNNGYKY-AKLPVKDBSA-N Ammonia-N17 Chemical compound [17NH3] QGZKDVFQNNGYKY-AKLPVKDBSA-N 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
- 238000005265 energy consumption Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000004094 preconcentration Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
-
- 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
-
- 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
- F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
- F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
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- 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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
-
- 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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
Definitions
- the present invention applies to denitrogenation processes of natural gas with or without helium recovery according to the preamble of claim 1 and known from the document US-A-4,758,258 .
- the exploited natural gas fields contain more and more nitrogen. This is particularly due to the depletion and scarcity of fields rich enough that no enrichment treatment is necessary before the marketing of gas.
- Unconventional resources such as shale gas also have the same problem: to make them marketable, it may be necessary to increase their calorific value by means of a pretreatment which consists of de-nitrogenising the raw gas.
- US-A-4778498 describes a double column used for denitrogenation of natural gas.
- Natural gas denitrogen units generally treat gases that come directly from wells at high pressure. After denaturing, the treated gas must be returned to the network, often at a pressure close to its inlet pressure.
- the denitrogenation of natural gas uses cryogenic distillation techniques that take place at lower pressures than source pressures.
- the sources can be at pressures of the order of 60 to 80 bara, while the cryogenic separation is carried out at pressures ranging from 30 bara to a pressure slightly above atmospheric pressure.
- nitrogen purified natural gas is produced at low pressure and must be pumped and / or compressed to be introduced into the network.
- the nitrogen-purified natural gas can be produced at different pressure levels at the outlet of the cold box.
- the different streams are then compressed by external compression until the desired pressure is reached.
- distillation at pressures greater than 12 bara is generally not well suited to the use of structured packings because of the "washing machine” phenomena, related to the approximation of the gas and liquid densities passing through the columns, which requires the use of trays for these pressure levels.
- the invention consists in valuing the expansion of the natural gas in the different turbines of the process, using it to effect cold compression.
- it may be product compression (typically natural gas purified by nitrogen).
- it is the compression of a nitrogen enriched gas from a column of the column system. For example, the compression of the gas at the top of the high pressure column of a double column process makes it possible to reduce the pressure of this column.
- the invention will be described in more detail with reference to the Figures 1 to 3 among which only the figure 3 illustrates a process according to the invention.
- the process is carried out in an isolated cold box which contains an exchange line 1 and a double column 2,3 comprising a first column 2 operating at between 10 and 30 bara and a second column 3 operating at between 0.8 and 3 bara.
- the first column 2 is thermally connected to the second column 3 by means of a vaporizer-condenser 5.
- the exchange line comprises at least one heat exchanger, preferably brazed aluminum plates and fins.
- the natural gas 10 which is generally at a pressure greater than 35 bara, cools in the exchange line 1.
- a portion 11 of the natural gas representing between 1 and 80% of the gas to be separated, preferably between 5 and 55%, or even between 25 and 35% of the gas to be separated, is withdrawn from the exchange line 1 and is expanded in gaseous form in an expansion turbine 7 which produces a fluid that is sent to the bottom of the first column to separate.
- the remainder of the natural gas 12 continues cooling in the exchange line where it is condensed, then is expanded in a flash valve before being sent in liquid form to the first column.
- column 2 separates the gas natural in a liquid enriched methane 21 in the bottom of the column and a nitrogen-enriched gas at the top of the column.
- the gas is used to heat the vaporizer-condenser 5 where it condenses and reflux at the top of the column 2.
- the bottom liquid cools in a subcooler 4 and is expanded to be sent to an intermediate level of the second column 3.
- An intermediate liquid 23 of the first column 2 is subcooled, expanded and sent to the top of the second column 3.
- the waste nitrogen 18 is withdrawn at the top of the column and is heated in the exchangers 4.1.
- Incondensable gases enriched in helium and nitrogen 17 leave the vaporizer 5 and heat up in the exchangers 4.1.
- the methane-enriched liquid 13 of the second column 3 is withdrawn in the tank, pumped at high pressure by means of the pump 6, subcooled and then divided as flow 14 into three fractions.
- a fraction 15A vaporizes in the exchange line 1 at the outlet pressure of the pump 6.
- the fractions 15, 15B are expanded at different pressures from each other by valves and each vaporizes in the line exchange at a different vaporization pressure.
- the fraction 15 leaves the exchange line as the gas flow 16.
- the liquid 14 is divided in the same manner but the liquid 15 vaporizes in the exchange line 1, leaves it, is compressed in a cold in a CBP booster before being returned to the exchange line 1 to continue its warming.
- This booster CBP values the energy of the turbine 7.
- the liquids produced by the division of the liquid 14 vaporize in the same way as in the Figure 1 .
- the nitrogen-enriched gas from the top of the first column 2 is compressed to a pressure of 17 to 30 bara in a cold booster CB1 having an inlet temperature generally below -150 ° C.
- the compressed nitrogen serves to heat the vaporizer 5 where it condenses into a fluid 27 is expanded in a valve and returned to the top of the column 2.
- the first and second columns can be replaced by a single column.
- Natural gas to be treated 10 Natural gas to be treated, 11 Natural gas to be treated to turbine, 12 Natural gas to treat to expansion, 13 Low pressure liquid methane, 14 High pressure liquid methane, 15 Medium pressure liquid methane, 16 Medium pressure methane gas, 17 Mixture of nitrogen and helium, 18 Residual nitrogen.
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Claims (9)
- Verfahren zur Deazotierung von Erdgas durch Destillation, wobei:i. Erdgas (11, 12), das in einer Austauschleitung (1) gekühlt wird,
in einem Kolonnensystem mit mindestens zwei Kolonnen (2,3) getrennt wird,ii. ein mit Stickstoff angereichertes Gas (18) aus einer Kolonne (3) des Kolonnensystems abgezogen und in der Austauschleitung erwärmt wird,iii. eine mit Methan angereicherte Flüssigkeit (13) aus einer Kolonne (3) des Kolonnensystems abgezogen, in der Austauschleitung unter Druck gesetzt und bei mindestens einem Verdampfungsdruck verdampft wird, und mindestens ein Teil des gekühlten Erdgases in gasförmiger Form in einer Turbine (7) entspannt wird und einer Kolonne (2) des Kolonnensystems in Gasform zugeführt wird, dadurch gekennzeichnet, dass die mit Methan angereicherte Flüssigkeit in der Austauschleitung bei mindestens zwei oder sogar drei Verdampfungsdrücken verdampft wird, und dadurch gekennzeichnet, dass die Energie, die von der Turbine (7) zugeführt wird, in mindestens einem Kompressor (CBI, CBP) genutzt wird, der ein Gas des Verfahrens komprimiert, wobei der Kompressor eine Einlasstemperatur aufweist, die niedriger als die Umgebungstemperatur oder sogar niedriger als -150 °C ist, wobei der Kompressor (CBI, CBP) direkt von der Turbine (7) angetrieben wird und wobei das Gas des Verfahrens ein mit Stickstoff angereichertes Gas (25) ist, das aus einer Kolonne (2) des Kolonnensystems stammt, das in dem Kompressor (CB1) komprimiert wird und dann dazu dient, den Sumpf einer anderen Kolonne (3) des Systems zu erwärmen. - Verfahren nach Anspruch 1, wobei ein zweiter Teil (12) des Erdgases mindestens teilweise kondensiert wird und in mindestens teilweise kondensierter Form einer Kolonne (2) des Kolonnensystems zugeführt wird.
- Verfahren nach einem der vorhergehenden Ansprüche, wobei die mit Methan angereicherte Flüssigkeit (13), die aus einer Kolonne (3) des Kolonnensystems abgezogen wird, ganz oder teilweise auf ein oder verschiedene Druckniveaus gepumpt wird, bevor sie in der Austauschleitung (1) verdampft wird.
- Verfahren nach Anspruch 3, wobei die mit Methan angereicherte Flüssigkeit (13), die zuvor gepumpt wird, in mindestens zwei Fraktionen (15, 15A, 15B) aufgeteilt wird, wovon mindestens eine in einem Ventil entspannt wird, bevor sie in der Austauschleitung verdampft wird.
- Verfahren nach einem der vorhergehenden Ansprüche, wobei das System eine erste Kolonne, die bei einem ersten Druck (2) arbeitet, eine zweite Kolonne (3) aufweist, die bei einem zweiten Druck arbeitet, der niedriger als der erste Druck ist, wobei die zweite Kolonne mit der ersten Kolonne thermisch verbunden ist, wobei das Erdgas (11, 12) der ersten Kolonne zugeführt wird, um eine Sumpfflüssigkeit (13) und ein Kopfgas (18) zu erzeugen, mindestens ein Teil der angereicherten Sumpfflüssigkeit der zweiten Kolonne zugeführt wird, wobei mindestens ein Teil des Kopfgases dazu dient, den Sumpf der zweiten Kolonne zu erwärmen, das mit Stickstoff angereicherte Gas (18) vom Kopf der zweiten Kolonne abgezogen wird und die mit Methan angereicherte Flüssigkeit von dem Sumpf der zweiten Kolonne abgezogen wird und das Gas, das in der Turbine (7) entspannt wird, der ersten Kolonne in Form eines Gases zugeführt wird.
- Verfahren nach Anspruch 5, wobei eine intermediäre Flüssigkeit (23) der ersten Kolonne (2) entspannt wird und der zweiten Kolonne (3) auf einem mittleren Niveau oder am Kopf von dieser zugeführt wird.
- Verfahren nach einem der vorhergehenden Ansprüche, wobei der mindestens eine Teil des Erdgases, der in dem Wärmetauscher gekühlt und der Turbine zugeführt wird, bei seinem Abkühlen stromaufwärts von der Turbine gasförmig bleibt.
- Verfahren nach einem der vorhergehenden Ansprüche, wobei der Teil des Erdgases (11), der für die Turbine bestimmt ist, auf einem mittleren Niveau des Wärmetauschers abgezogen wird.
- Verfahren nach Anspruch 8, wobei der zweite Teil des Erdgases bis zum kalten Ende des Wärmetauschers abgekühlt wird.
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PL14799510T PL3058296T3 (pl) | 2013-10-18 | 2014-10-14 | Sposób odazotowywania gazu ziemnego z odzyskiwaniem lub bez odzyskiwania helu |
HRP20180610TT HRP20180610T1 (hr) | 2013-10-18 | 2018-04-17 | Postupak uklanjanja dušika iz zemnog plina, uz ili bez prikupljanja helija |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR1360138A FR3012211B1 (fr) | 2013-10-18 | 2013-10-18 | Procede de deazotation du gaz naturel avec ou sans recuperation d'helium |
PCT/FR2014/052606 WO2015055938A2 (fr) | 2013-10-18 | 2014-10-14 | Procede de deazotation du gaz naturel avec ou sans recuperation d'helium |
Publications (2)
Publication Number | Publication Date |
---|---|
EP3058296A2 EP3058296A2 (de) | 2016-08-24 |
EP3058296B1 true EP3058296B1 (de) | 2018-03-28 |
Family
ID=49998435
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP14799510.4A Active EP3058296B1 (de) | 2013-10-18 | 2014-10-14 | Verfahren zur stickstoffentfernung aus erdgas mit oder ohne heliumgewinnung |
Country Status (9)
Country | Link |
---|---|
US (1) | US10006699B2 (de) |
EP (1) | EP3058296B1 (de) |
EA (1) | EA034668B1 (de) |
FR (1) | FR3012211B1 (de) |
HR (1) | HRP20180610T1 (de) |
MX (1) | MX2016004800A (de) |
PL (1) | PL3058296T3 (de) |
SA (1) | SA516370968B1 (de) |
WO (1) | WO2015055938A2 (de) |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR3121743B1 (fr) * | 2021-04-09 | 2023-04-21 | Air Liquide | Procédé et appareil de séparation d’un mélange contenant au moins de l’azote et du méthane |
Family Cites Families (16)
Publication number | Priority date | Publication date | Assignee | Title |
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US2557171A (en) * | 1946-11-12 | 1951-06-19 | Pritchard & Co J F | Method of treating natural gas |
JPS5420986A (en) * | 1977-07-18 | 1979-02-16 | Kobe Steel Ltd | Method of equipment for separating air |
US4331461A (en) * | 1978-03-10 | 1982-05-25 | Phillips Petroleum Company | Cryogenic separation of lean and rich gas streams |
US4357153A (en) * | 1981-03-30 | 1982-11-02 | Erickson Donald C | Internally heat pumped single pressure distillative separations |
US4710212A (en) | 1986-09-24 | 1987-12-01 | Union Carbide Corporation | Process to produce high pressure methane gas |
US4758258A (en) * | 1987-05-06 | 1988-07-19 | Kerr-Mcgee Corporation | Process for recovering helium from a natural gas stream |
US4936888A (en) * | 1989-12-21 | 1990-06-26 | Phillips Petroleum Company | Nitrogen rejection unit |
US4948405A (en) * | 1989-12-26 | 1990-08-14 | Phillips Petroleum Company | Nitrogen rejection unit |
US5692395A (en) * | 1995-01-20 | 1997-12-02 | Agrawal; Rakesh | Separation of fluid mixtures in multiple distillation columns |
DE10215125A1 (de) | 2002-04-05 | 2003-10-16 | Linde Ag | Verfahren zum Abtrennen von Stickstoff aus einer Stickstoff-enthaltenden Kohlenwasserstoff-reichen Fraktion |
GB0220791D0 (en) * | 2002-09-06 | 2002-10-16 | Boc Group Plc | Nitrogen rejection method and apparatus |
GB0226983D0 (en) * | 2002-11-19 | 2002-12-24 | Boc Group Plc | Nitrogen rejection method and apparatus |
DE102009009477A1 (de) * | 2009-02-19 | 2010-08-26 | Linde Aktiengesellschaft | Verfahren zum Abtrennen von Stickstoff |
GB2455462B (en) * | 2009-03-25 | 2010-01-06 | Costain Oil Gas & Process Ltd | Process and apparatus for separation of hydrocarbons and nitrogen |
DE202009010874U1 (de) * | 2009-08-11 | 2009-11-19 | Linde Aktiengesellschaft | Vorrichtung zur Erzeugung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft |
US20140060114A1 (en) * | 2012-08-30 | 2014-03-06 | Fluor Technologies Corporation | Configurations and methods for offshore ngl recovery |
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2013
- 2013-10-18 FR FR1360138A patent/FR3012211B1/fr not_active Expired - Fee Related
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2014
- 2014-10-14 US US15/029,107 patent/US10006699B2/en active Active
- 2014-10-14 EA EA201690799A patent/EA034668B1/ru not_active IP Right Cessation
- 2014-10-14 WO PCT/FR2014/052606 patent/WO2015055938A2/fr active Application Filing
- 2014-10-14 MX MX2016004800A patent/MX2016004800A/es unknown
- 2014-10-14 EP EP14799510.4A patent/EP3058296B1/de active Active
- 2014-10-14 PL PL14799510T patent/PL3058296T3/pl unknown
-
2016
- 2016-04-17 SA SA516370968A patent/SA516370968B1/ar unknown
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2018
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Also Published As
Publication number | Publication date |
---|---|
EA034668B1 (ru) | 2020-03-04 |
FR3012211B1 (fr) | 2018-11-02 |
US10006699B2 (en) | 2018-06-26 |
MX2016004800A (es) | 2016-07-18 |
PL3058296T3 (pl) | 2018-09-28 |
US20160245584A1 (en) | 2016-08-25 |
WO2015055938A2 (fr) | 2015-04-23 |
FR3012211A1 (fr) | 2015-04-24 |
EP3058296A2 (de) | 2016-08-24 |
HRP20180610T1 (hr) | 2018-06-29 |
SA516370968B1 (ar) | 2020-10-20 |
WO2015055938A3 (fr) | 2015-12-03 |
EA201690799A1 (ru) | 2016-08-31 |
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