EP0711969A2 - Process for liquefying natural gas - Google Patents
Process for liquefying natural gas Download PDFInfo
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- EP0711969A2 EP0711969A2 EP95117286A EP95117286A EP0711969A2 EP 0711969 A2 EP0711969 A2 EP 0711969A2 EP 95117286 A EP95117286 A EP 95117286A EP 95117286 A EP95117286 A EP 95117286A EP 0711969 A2 EP0711969 A2 EP 0711969A2
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- Prior art keywords
- natural gas
- gas stream
- regeneration
- stream
- cleaned
- Prior art date
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 114
- 239000003345 natural gas Substances 0.000 title claims abstract description 51
- 238000000034 method Methods 0.000 title claims abstract description 20
- 239000007789 gas Substances 0.000 claims abstract description 29
- 230000008929 regeneration Effects 0.000 claims abstract description 23
- 238000011069 regeneration method Methods 0.000 claims abstract description 23
- 238000001816 cooling Methods 0.000 claims abstract description 11
- 230000000274 adsorptive effect Effects 0.000 claims description 9
- 239000003507 refrigerant Substances 0.000 claims description 6
- 238000005057 refrigeration Methods 0.000 claims description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 12
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 6
- 239000002826 coolant Substances 0.000 abstract description 6
- 229910001868 water Inorganic materials 0.000 abstract description 6
- 239000001569 carbon dioxide Substances 0.000 abstract description 4
- 238000010521 absorption reaction Methods 0.000 abstract 1
- 239000008239 natural water Substances 0.000 abstract 1
- 229930195733 hydrocarbon Natural products 0.000 description 14
- 150000002430 hydrocarbons Chemical class 0.000 description 14
- 238000001179 sorption measurement Methods 0.000 description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 238000000926 separation method Methods 0.000 description 7
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 4
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000003949 liquefied natural gas Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 125000003118 aryl group Chemical group 0.000 description 2
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
- F25J1/0055—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
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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
- F25J1/0212—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
- F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation 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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
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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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
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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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
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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
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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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S62/00—Refrigeration
- Y10S62/912—External refrigeration system
Definitions
- the invention relates to a method for liquefying a pressurized natural gas stream, in which the natural gas stream is first cleaned by means of an adsorptive separation device of CO2 and H2O and the pre-cleaned natural gas stream is then brought into heat exchange with at least one refrigerant conducted in a refrigeration cycle and liquefied and in which adsorptive separation device by means of a regeneration gas, consisting of a partial stream of the pre-cleaned natural gas stream and optionally further residual gas streams, such as a flash gas stream, is regenerated.
- a regeneration gas consisting of a partial stream of the pre-cleaned natural gas stream and optionally further residual gas streams, such as a flash gas stream
- a method for liquefying a pressurized natural gas stream is known for example from DE-OS 28 20 212.
- the pressurized natural gas stream is brought into heat exchange with two refrigerants which are conducted in a closed circuit and are each compressed, at least partially liquefied and expanded, the coolant of the first circuit for precooling the natural gas and the coolant of the second circuit and the coolant of the second circuit is used to liquefy the pre-cooled natural gas.
- the liquefied natural gas is then expanded and, after precooling, divided into two partial streams, one of which is liquefied by heat exchange with the coolant of the second circuit and the other by heat exchange with the flash gas formed during the expansion of the liquefied natural gas.
- Natural gas generally consists essentially of methane, small amounts of ethane, propane and higher-boiling hydrocarbons as well as small amounts of nitrogen, carbon dioxide and water.
- Natural gas Before cooling and liquefaction, all those components that freeze out during the cooling or liquefaction process and could therefore lead to laying in pipes and valves must be separated from the natural gas. It makes sense to do this by means of an adsorptive separation device. In this, carbon dioxide and water can be separated apart from very small residual contents, so that there is no longer any danger of these components freezing out in the low-temperature section.
- the adsorbent used preferably a molecular sieve
- the adsorbent used must be regenerated cyclically.
- a partial stream of the flash gas can be used for this purpose, which makes the provision of a special regeneration gas unnecessary.
- the regeneration gas drawn off from a regenerated adsorber can then be burned due to its composition, for example to drive a gas turbine.
- Part of the natural gas stream emerging from the adsorptive separation device is also frequently used as the regeneration gas.
- the aim and object of the present invention is to provide a method for liquefying a pressurized natural gas stream which has an improved energy balance compared to the known methods.
- the natural gas stream consisting of 1.0 mol% N2, 94.0 mol% methane, 2.0 mol% ethane, 1.22 mol% C3+ hydrocarbons, 1.75 mol% is Carbon dioxide and 0.03 mol% of water at a temperature of 18 ° C and a pressure of 42 bar fed to the adsorption device A.
- This consists of at least two adsorbers arranged parallel to one another, which cyclically run through adsorption and regeneration phases.
- the pre-cleaned natural gas stream with 50 ppm CO2 and ⁇ 1 ppm H2O leaves the adsorption device A at a temperature of 38 ° C and a pressure of 40 bar and is passed through line 2 through the heat exchangers E1 and E2.
- the natural gas stream now cooled to -73 ° C. is fed to the separator D.
- aromatics and heavy hydrocarbons preferably C3+ hydrocarbons
- This separation of aromatics and heavy hydrocarbons is necessary, since they would otherwise freeze out during expansion or during further cooling.
- the aromatic and heavy hydrocarbon fraction is withdrawn from the separator D via line 4, expanded to provide cold in valve V2 and then passed through the heat exchangers E2 and E1 in indirect heat exchange with the natural gas stream to be cooled in line 2 by means of line 4 '.
- This fraction led in line 4 ' consists essentially of 61.0 mol% methane, 12.0 mol% ethane, 10.0 mol% propane and 17.0 mol% C4+ hydrocarbons and has at the outlet of the Heat exchanger E1 a temperature of 36 ° C and a pressure of 9 bar. It is now added to line 7 ', which will be discussed later.
- the natural gas fraction freed from aromatics and heavy hydrocarbons consisting essentially of 1.0 mol% nitrogen, 97.0 mol% methane, 1.8 mol% ethane and 0.2 mol% C3+ hydrocarbons, is piped 3 withdrawn from the head of the separator D and further cooled, liquefied and supercooled in the heat exchangers E2 and E3.
- this fraction has a temperature of -133 ° C at a pressure of 39.6 bar.
- the valve V1 is now depressurized before the natural gas fraction is fed to the storage tank T at line pressure 3 'at atmospheric pressure and a temperature of -161 ° C. Liquefied natural gas can be withdrawn from this via line 6.
- the flash gas generated within the storage tank T is discharged from this via line 7 and passed through the heat exchangers E3, E2 and E1 in counterflow to the natural gas stream to be cooled.
- the compressor V increases the pressure to the necessary regeneration gas pressure.
- the flash gas compressed in this way is then fed via line 7 'to the adsorber (s) to be regenerated in the adsorption device A.
- this compressed flash gas is admixed with the aromatic and / or heavy hydrocarbon fraction guided through line 4 'through the heat exchangers E2 and E1.
- the two fractions introduced via line 4 'and 7' cannot fully meet the regeneration gas requirement. For this reason it is necessary to use part of the pre-cleaned natural gas flow for regeneration gas purposes.
- the partial flow of the natural gas flow required for this is drawn off between the two heat exchangers E2 and E3.
- the extraction point should be chosen with regard to the temperature so that the efficiency of the cold use is maximized by the expansion of the natural gas partial flow to the necessary regeneration gas pressure.
- This amount is removed via line 5, relaxed in the valve V3 using the Joule-Thompson effect, and then led by line 5 'in counterflow to the natural gas stream to be cooled through the heat exchangers E2 and E1.
- the partial natural gas stream branched off via line 5 upstream of the expansion valve V3 has a temperature of -126 ° C. at a pressure of 39.7 bar
- the expansion valve V3 is expanded to 9.3 bar.
- this partial flow in line 5 ' has a temperature of 36 ° C.
- the separator D is usually designed for a temperature level which also allows the separation of a larger amount of aromatics and higher hydrocarbons.
- the pressure drop between natural gas pressure and regeneration gas pressure can now be used as a cold source.
- the energy required for the refrigeration cycle can be reduced, so that the specific energy consumption in the liquefaction of natural gas is reduced.
- the specific energy requirement is the determining factor for such processes. Since the Joule-Thompson effect causes a greater temperature difference than in the case of known methods which already use part of the natural gas flow for regeneration purposes directly behind the pressure swing adsorption device A subtract, the case is, the required heat exchange surface becomes smaller despite a slightly increased heat conversion. This also reduces the costs for the heat exchangers in the cold part of the process.
- the method according to the invention leads to a reduction in specific energy consumption without additional investment.
- the energy consumption is directly proportional to the amount of partial electricity that is relaxed using the Joule-Thompson effect.
Abstract
Description
Die Erfindung betrifft ein Verfahren zum Verflüssigen eines unter Druck stehenden Erdgasstromes, bei dem der Erdgasstrom zunächst mittels einer adsorptiven Abtrennvorrichtung von CO₂ und H₂O gereinigt und der vorgereinigte Erdgasstrom anschließend in Wärmetausch mit wenigstens einem in einem Kältekreislauf geführten Kältemittel gebracht und verflüssigt wird und bei dem die adsorptive Abtrennvorrichtung mittels eines Regeneriergases, bestehend aus einem Teilstrom des vorgereinigten Erdgasstromes und gegebenenfalls weiterer Restgasströme, wie z.B. einem Flashgasstrom, regeneriert wird.The invention relates to a method for liquefying a pressurized natural gas stream, in which the natural gas stream is first cleaned by means of an adsorptive separation device of CO₂ and H₂O and the pre-cleaned natural gas stream is then brought into heat exchange with at least one refrigerant conducted in a refrigeration cycle and liquefied and in which adsorptive separation device by means of a regeneration gas, consisting of a partial stream of the pre-cleaned natural gas stream and optionally further residual gas streams, such as a flash gas stream, is regenerated.
Ein Verfahren zum Verflüssigen eines unter Druck stehenden Erdgasstromes ist z.B. aus der DE-OS 28 20 212 bekannt. Bei diesem bekannten Verfahren wird der unter Druck stehende Erdgasstrom in Wärmetausch mit zwei im geschlossenen Kreisläufen geführten Kältemitteln, die jeweils verdichtet, mindestens teilweise verflüssigt und entspannt werden, gebracht, wobei das Kühlmittel des ersten Kreislaufes zur Vorkühlung des Erdgases sowie des Kühlmittels des zweiten Kreislaufs und das Kühlmittel des zweiten Kreislaufs zur Verflüssigung des vorgekühlten Erdgases verwendet wird. Das verflüssigte Erdgas wird anschließend entspannt und nach der Vorkühlung in zwei Teilströme aufgeteilt, von denen der eine durch Wärmetausch mit dem Kühlmittel des zweiten Kreislaufs und der andere durch Wärmetausch mit dem bei der Entspannung des verflüssigten Erdgases gebildeten Flashgases verflüssigt wird. Das Flashgas wird nach dem Wärmetausch mit dem vorgekühlten Erdgas verdichtet, mindestens teilweise in Wärmetausch mit den Kühlmitteln des ersten und des zweiten Kreislaufs verflüssigt und anschließend wieder entspannt. Erdgas besteht in der Regel im wesentlichen aus Methan, geringen Anteilen an Ethan, Propan und höhersiedenden Kohlenwasserstoffen sowie geringe Mengen Stickstoff, Kohlendioxid und Wasser. Vor der Abkühlung und Verflüssigung sind all diejenigen Komponenten, die während des Abkühl- bzw. Verflüssigungsprozesses ausfrieren und damit zu Verlegungen in Leitungen und Ventilen führen könnten, aus dem Erdgas abzutrennen. Dies geschieht sinnvollerweise mittels einer adsorptiven Abtrennvorrichtung. In dieser können Kohlendioxid und Wasser bis auf sehr kleine Restgehalte abgetrennt werden, so daß die Gefahr des Ausfrierens dieser Komponenten im Tieftemperaturteil nicht mehr besteht. Das verwendete Adsorptionsmittel, vorzugsweise ein Molsieb, ist jedoch zyklisch zu regenerieren. Dazu kann, wie in der DE-OS 28 20 212 vorgeschlagen, ein Teilstrom des Flashgases verwendet werden, wodurch sich die Bereitstellung eines besonderen Regeneriergases erübrigt. Das aus einem regenerierten Adsorber abgezogene Regeneriergas kann aufgrund seiner Zusammensetzung anschließend z.B. zum Antreiben einer Gasturbine verbrannt werden. Häufig wird als Regeneriergas auch ein Teil des aus der adsorptiven Abtrennvorrichtung austretenden Erdgasstromes verwendet.A method for liquefying a pressurized natural gas stream is known for example from DE-OS 28 20 212. In this known method, the pressurized natural gas stream is brought into heat exchange with two refrigerants which are conducted in a closed circuit and are each compressed, at least partially liquefied and expanded, the coolant of the first circuit for precooling the natural gas and the coolant of the second circuit and the coolant of the second circuit is used to liquefy the pre-cooled natural gas. The liquefied natural gas is then expanded and, after precooling, divided into two partial streams, one of which is liquefied by heat exchange with the coolant of the second circuit and the other by heat exchange with the flash gas formed during the expansion of the liquefied natural gas. After the heat exchange, the flash gas is compressed with the pre-cooled natural gas, at least partially liquefied in heat exchange with the coolants of the first and second circuits and then expanded again. Natural gas generally consists essentially of methane, small amounts of ethane, propane and higher-boiling hydrocarbons as well as small amounts of nitrogen, carbon dioxide and water. Before cooling and liquefaction, all those components that freeze out during the cooling or liquefaction process and could therefore lead to laying in pipes and valves must be separated from the natural gas. It makes sense to do this by means of an adsorptive separation device. In this, carbon dioxide and water can be separated apart from very small residual contents, so that there is no longer any danger of these components freezing out in the low-temperature section. However, the adsorbent used, preferably a molecular sieve, must be regenerated cyclically. As suggested in DE-OS 28 20 212, a partial stream of the flash gas can be used for this purpose, which makes the provision of a special regeneration gas unnecessary. The regeneration gas drawn off from a regenerated adsorber can then be burned due to its composition, for example to drive a gas turbine. Part of the natural gas stream emerging from the adsorptive separation device is also frequently used as the regeneration gas.
Ziel und Aufgabe der vorliegenden Erfindung ist es, ein Verfahren zum Verflüssigen eines unter Druck stehenden Erdgasstromes anzugeben, das gegenüber den bekannten Verfahren eine verbesserte Energiebilanz aufweist.The aim and object of the present invention is to provide a method for liquefying a pressurized natural gas stream which has an improved energy balance compared to the known methods.
Dies wird erfindungsgemäß dadurch erreicht, daß während des Abkühl- und Verflüssigungsprozesses des Erdgasstromes wenigstens der zur Regenerierung der adsorptiven Abtrennvorrichtung benötigte Erdgasteilstrom bei Erreichen derjenigen Temperatur abgetrennt wird, bei der der Wirkungsgrad der Kältenutzung durch die Drosselung auf den Regeneriergasdruck maximal ist.This is achieved according to the invention in that during the cooling and liquefaction process of the natural gas flow, at least the natural gas partial flow required for regeneration of the adsorptive separation device is separated off when the temperature is reached at which the efficiency of the cold use by throttling to the regeneration gas pressure is at a maximum.
Die Erfindung sowie weitere Ausgestaltungen davon seien anhand der Figur erläutert.The invention and further embodiments thereof are explained with the aid of the figure.
Über Leitung 1 wird der Erdgasstrom, bestehend aus 1,0 Mol-% N₂, 94,0 Mol-% Methan, 2,0 Mol-% Ethan, 1,22 Mol-% C₃₊-Kohlenwasserstoffen, 1,75 Mol-% Kohlendioxid und 0,03 Mol-% Wasser bei einer Temperatur von 18°C und einem Druck von 42 bar der Adsorptionsvorrichtung A zugeführt. Diese besteht aus wenigstens zwei, parallel zueinander angeordneten Adsorbern, die zyklisch Adsorptions- und Regenerierphasen durchlaufen. Der vorgereinigte Erdgasstrom mit 50 ppm CO₂ und < 1 ppm H₂O verläßt mit einer Temperatur von 38°C und einem Druck von 40 bar die Adsorptionsvorrichtung A und wird über Leitung 2 durch die Wärmetauscher E1 und E2 geführt. Der nunmehr auf -73°C abgekühlte Erdgasstrom wird dem Abscheider D zugeführt. In diesem Abscheider D erfolgt eine Abtrennung von Aromaten und schweren Kohlenwasserstoffen, vorzugsweise C₃₊-Kohlenwasserstoffen, aus dem vorgereinigten Erdgasstrom. Diese Abtrennung von Aromaten und schweren Kohlenwasserstoffen ist notwendig, da diese ansonsten bei der Entspannung bzw. bei der weiteren Abkühlung ausfrieren würden. Die Aromaten- und schwere Kohlenwasserstoff-Fraktion wird über Leitung 4 aus dem Abscheider D abgezogen, im Ventil V2 kälteleistend entspannt und anschließend im indirekten Wärmetausch mit dem abzukühlenden Erdgasstrom in Leitung 2 mittels Leitung 4' durch die Wärmetauscher E2 und E1 geführt. Diese in Leitung 4' geführte Fraktion besteht im wesentlichen aus 61,0 Mol-% Methan, 12,0 Mol-% Ethan, 10,0 Mol-% Propan und 17,0 Mol-% C₄₊-Kohlenwasserstoffe und weist am Austritt des Wärmetauschers E1 eine Temperatur von 36°C und einen Druck von 9 bar auf. Sie wird nun der Leitung 7', auf die später noch eingegangen wird, beigemischt. Die von Aromaten und schweren Kohlenwasserstoffen befreite Erdgasfraktion, bestehend im wesentlichen aus 1,0 Mol-% Stickstoff, 97,0 Mol-% Methan, 1,8 Mol-% Ethan und 0,2 Mol-% C₃₊-Kohlenwasserstoffen wird über Leitung 3 vom Kopf des Abscheiders D abgezogen und in den Wärmetauschern E2 und E3 weiter abgekühlt, verflüssigt und unterkühlt. Am Ausgang des Wärmetauschers E3 weist diese Fraktion bei einem Druck von 39,6 bar eine Temperatur von -133°C auf. Es erfolgt nun eine Entspannung im Ventil V1, bevor die Erdgasfraktion bei Atmosphärendruck und einer Temperatur von -161°C mittels Leitung 3' dem Speichertank T zugeführt wird. Aus diesem kann über Leitung 6 verflüssigtes Erdgas abgezogen werden. Das innerhalb des Speichertanks T anfallende Flashgas wird über Leitung 7 aus diesem abgeführt und im Gegenstrom zu dem abzukühlenden Erdgasstrom durch die Wärmetauscher E3, E2 und E1 geführt. Am Austritt des Wärmetauschers E1 erfolgt mittels des Verdichters V eine Druckerhöhung auf den notwendigen Regeneriergasdruck. Das so verdichtete Flashgas wird nun über Leitung 7' dem bzw. den zu regenerierenden Adsorbern der Adsorptionsvorrichtung A zugeführt. Diesem verdichteten Flashgas wird, wie bereits beschrieben, die mittels Leitung 4' durch die Wärmetauscher E2 und E1 geführte Aromaten- und/oder schwere Kohlenwasserstoff-Fraktion beigemischt. Die beiden, über Leitung 4' und 7' herangeführten Fraktionen können den Regeneriergasbedarf jedoch nicht vollständig decken. Aus diesem Grund ist es notwendig, einen Teil des vorgereinigten Erdgasstromes zu Regeneriergaszwecken zu verwenden. Beim erfindungsgemäßen Verfahren wird der dafür benötigte Teilstrom des Erdgasstromes zwischen den beiden Wärmetauschern E2 und E3 abgezogen. Die Abzugsstelle ist bezüglich der Temperatur so zu wählen, daß der Wirkungsgrad der Kältenutzung durch die Entspannung des Erdgasteilstromes auf den notwendigen Regeneriergasdruck maximal ist. Diese Menge wird über Leitung 5 abgeführt, im Ventil V3 unter Ausnutzung des Joule-Thompson-Effekts kälteleistend entspannt und anschließend mittels Leitung 5' im Gegenstrom zu dem abzukühlenden Erdgasstrom durch die Wärmetauscher E2 und E1 geführt. Während der über Leitung 5 abgezweigte Erdgasteilstrom vor dem Entspannungsventil V3 eine Temperatur von -126°C bei einem Druck von 39,7 bar aufweist, erfolgt im Entspannungsventil V3 eine Entspannung auf 9,3 bar. Am Ausgang des Wärmetauschers E1 schließlich weist dieser Teilstrom in Leitung 5' eine Temperatur von 36°C auf und wird über Leitung 7' der Adsorptionsvorrichtung A als Regeneriergas zugeführt. Nach erfolgter Regenerierung wird das Regeneriergas über Leitung 8 aus der Adsorptionsvorrichtung A abgezogen. Die Deckung des für die Abkühlung und Verflüssigung des Erdgasstromes benötigten Kältebedarfs erfolgt mittels eines zusätzlichen Kältekreislaufes. Dieser Kältekreislauf sei hier nur schematisch dargestellt, wobei über Leitung 9 und 10 das Kältemittel bzw. Kältemittelgemisch zur Abkühlung und teilweisen Verflüssigung durch die Wärmetauscher E1, E2 und E3 bzw. durch den Wärmetauscher E1 geführt wird, in den Entspannungsventilen V4 und V5 kälteleistend entspannt und anschließend mittels Leitung 9' im Gegenstrom zu dem abzukühlenden Erdgasstrom durch die Wärmetauscher E3, E2 und E1 geleitet wird. Als Kältemittel haben sich Gemische aus Stickstoff und Methan oder Gemische aus Stickstoff, Methan sowie C₂- bis C₅-Kohlenwasserstoffen bewährt. Derartige Kältekreisläufe gehören jedoch zum Stand der Technik, so daß auf sie nicht näher eingegangen werden muß.The natural gas stream consisting of 1.0 mol% N₂, 94.0 mol% methane, 2.0 mol% ethane, 1.22 mol% C₃₊ hydrocarbons, 1.75 mol% is Carbon dioxide and 0.03 mol% of water at a temperature of 18 ° C and a pressure of 42 bar fed to the adsorption device A. This consists of at least two adsorbers arranged parallel to one another, which cyclically run through adsorption and regeneration phases. The pre-cleaned natural gas stream with 50 ppm CO₂ and <1 ppm H₂O leaves the adsorption device A at a temperature of 38 ° C and a pressure of 40 bar and is passed through line 2 through the heat exchangers E1 and E2. The natural gas stream now cooled to -73 ° C. is fed to the separator D. In this separator D, aromatics and heavy hydrocarbons, preferably C₃₊ hydrocarbons, are separated from the pre-cleaned natural gas stream. This separation of aromatics and heavy hydrocarbons is necessary, since they would otherwise freeze out during expansion or during further cooling. The aromatic and heavy hydrocarbon fraction is withdrawn from the separator D via line 4, expanded to provide cold in valve V2 and then passed through the heat exchangers E2 and E1 in indirect heat exchange with the natural gas stream to be cooled in line 2 by means of line 4 '. This fraction led in line 4 'consists essentially of 61.0 mol% methane, 12.0 mol% ethane, 10.0 mol% propane and 17.0 mol% C₄₊ hydrocarbons and has at the outlet of the Heat exchanger E1 a temperature of 36 ° C and a pressure of 9 bar. It is now added to line 7 ', which will be discussed later. The natural gas fraction freed from aromatics and heavy hydrocarbons, consisting essentially of 1.0 mol% nitrogen, 97.0 mol% methane, 1.8 mol% ethane and 0.2 mol% C₃₊ hydrocarbons, is piped 3 withdrawn from the head of the separator D and further cooled, liquefied and supercooled in the heat exchangers E2 and E3. At the outlet of the heat exchanger E3, this fraction has a temperature of -133 ° C at a pressure of 39.6 bar. The valve V1 is now depressurized before the natural gas fraction is fed to the storage tank T at line pressure 3 'at atmospheric pressure and a temperature of -161 ° C. Liquefied natural gas can be withdrawn from this via line 6. The flash gas generated within the storage tank T is discharged from this via
Es wäre auch denkbar, als den für die Regenerierung der Adsorptionsvorrichtung A benötigten Erdgasteilstrom, den am Sumpf des Abscheiders D abgezogenen Aromaten- und höhere Kohlenwasserstoff-reichen Strom zu verwenden. Dies ist jedoch nur dann möglich, wenn der Gehalt an Aromaten und höheren Kohlenwasserstoffen des die Adsorptionsvorrichtung A verlassenden Erdgasstromes so niedrig ist, daß auch bei einer Abkühlung auf diejenige Temperatur, die eine Entspannung auf den Regeneriergasdruck sinnvoll macht, diese Komponenten nicht bereits vor dem Abscheider D oder nach dem Entspannungsventil V2 ausfrieren und zu Verlegungen in den Leitungen führen. In der Regel wird schon aus Sicherheitsgründen der Abscheider D auf ein Temperaturniveau ausgelegt, das auch die Abtrennung einer größeren Menge an Aromaten und höheren Kohlenwasserstoffen ermöglicht.It would also be conceivable to use, as the natural gas partial stream required for the regeneration of the adsorption device A, the aromatics-rich stream drawn off at the bottom of the separator D and higher hydrocarbon-rich stream. However, this is only possible if the content of aromatics and higher hydrocarbons in the natural gas stream leaving the adsorption device A is so low that even when it is cooled to the temperature that makes relaxation to the regeneration gas pressure useful, these components are not already in front of the separator D or freeze after the expansion valve V2 and lead to routing in the lines. For safety reasons, the separator D is usually designed for a temperature level which also allows the separation of a larger amount of aromatics and higher hydrocarbons.
Selbstverständlich ist es auch denkbar, nicht nur die zur Regenerierung der adsorptiven Abtrennvorrichtung benötigte Erdgasteilstrommenge aus dem Erdgasstrom abzutrennen, sondern die maximal an ein gegebenenfalls vorhandenes Niederdrucknetz abführbare Menge. Wie groß die aus dem Erdgasstrom abgetrennte Erdgasteilstrommenge sein wird, wird sich also immer nach den Randbedingungen, wie z.B. vorhandenes Niederdrucknetz, etc., orientieren.Of course, it is also conceivable not only to separate the partial natural gas flow required for regeneration of the adsorptive separating device from the natural gas flow, but rather the maximum amount that can be discharged to a low-pressure network which may be present. The size of the natural gas stream separated from the natural gas stream will always depend on the boundary conditions, e.g. Orient existing low pressure network, etc.
Mittels des erfindungsgemäßen Verfahrens kann nun das Druckgefälle zwischen Erdgasdruck und Regeneriergasdruck als Kältequelle ausgenutzt werden. Dies führt dazu, daß die für den Kältekreislauf benötigte Energie verringert werden kann, so daß sich der spezifische Energieverbrauch bei der Erdgasverflüssigung erniedrigt. Gerade der spezifische Energiebedarf ist neben den Investitionskosten der bestimmende Faktor für derartige Verfahren. Da der Joule-Thompson-Effekt eine größere Temperaturdifferenz bewirkt als dies bei bekannten Verfahren, die einen Teil des Erdgasstromes zu Regenerierzwecken bereits unmittelbar hinter der Druckwechseladsorptionsvorrichtung A abziehen, der Fall ist, wird die benötigte Wärmeaustauschfläche trotz leicht erhöhtem Wärmeumsatz geringer. Dadurch erniedrigen sich zusätzlich die Kosten für die Wärmetauscher im kalten Teil des Verfahrens. Zusammenfassend läßt sich feststellen, daß das erfindungsgemäße Verfahren ohne einen Mehraufwand an Investitionen zu einer Erniedrigung des spezifischen Energieverbrauchs führt. Der Energieverbrauch ist hierbei direkt proportional zu der Teilstrommenge, die unter Ausnutzung des Joule-Thompson-Effekts entspannt wird.By means of the method according to the invention, the pressure drop between natural gas pressure and regeneration gas pressure can now be used as a cold source. This means that the energy required for the refrigeration cycle can be reduced, so that the specific energy consumption in the liquefaction of natural gas is reduced. In addition to the investment costs, the specific energy requirement is the determining factor for such processes. Since the Joule-Thompson effect causes a greater temperature difference than in the case of known methods which already use part of the natural gas flow for regeneration purposes directly behind the pressure swing adsorption device A subtract, the case is, the required heat exchange surface becomes smaller despite a slightly increased heat conversion. This also reduces the costs for the heat exchangers in the cold part of the process. In summary, it can be stated that the method according to the invention leads to a reduction in specific energy consumption without additional investment. The energy consumption is directly proportional to the amount of partial electricity that is relaxed using the Joule-Thompson effect.
Claims (1)
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE4440401 | 1994-11-11 | ||
| DE4440401A DE4440401A1 (en) | 1994-11-11 | 1994-11-11 | Process for liquefying natural gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| EP0711969A2 true EP0711969A2 (en) | 1996-05-15 |
| EP0711969A3 EP0711969A3 (en) | 1997-02-05 |
Family
ID=6533117
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP95117286A Withdrawn EP0711969A3 (en) | 1994-11-11 | 1995-11-02 | Process for liquefying natural gas |
Country Status (4)
| Country | Link |
|---|---|
| US (1) | US5551256A (en) |
| EP (1) | EP0711969A3 (en) |
| AR (1) | AR000098A1 (en) |
| DE (1) | DE4440401A1 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102410702A (en) * | 2010-09-09 | 2012-04-11 | 林德股份公司 | Natural gas liquefaction |
| FR3063540A1 (en) * | 2017-03-01 | 2018-09-07 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | METHOD FOR LIQUEFACTING NATURAL GAS USING A REFRIGERATION CIRCUIT COMPRISING ONLY ONE TURBINE |
| CN108709367A (en) * | 2018-05-22 | 2018-10-26 | 中石化宁波工程有限公司 | A kind of liquefying plant and application method of carbon dioxide |
Families Citing this family (23)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19707476C2 (en) * | 1997-02-25 | 1999-08-05 | Linde Ag | Method and device for liquefying a hydrocarbon-rich stream |
| DE19821242A1 (en) * | 1998-05-12 | 1999-11-18 | Linde Ag | Liquefaction of pressurized hydrocarbon-enriched stream |
| US20070137246A1 (en) * | 2001-05-04 | 2007-06-21 | Battelle Energy Alliance, Llc | Systems and methods for delivering hydrogen and separation of hydrogen from a carrier medium |
| US7637122B2 (en) | 2001-05-04 | 2009-12-29 | Battelle Energy Alliance, Llc | Apparatus for the liquefaction of a gas and methods relating to same |
| US7594414B2 (en) * | 2001-05-04 | 2009-09-29 | Battelle Energy Alliance, Llc | Apparatus for the liquefaction of natural gas and methods relating to same |
| US7219512B1 (en) | 2001-05-04 | 2007-05-22 | Battelle Energy Alliance, Llc | Apparatus for the liquefaction of natural gas and methods relating to same |
| US7591150B2 (en) * | 2001-05-04 | 2009-09-22 | Battelle Energy Alliance, Llc | Apparatus for the liquefaction of natural gas and methods relating to same |
| US6581409B2 (en) | 2001-05-04 | 2003-06-24 | Bechtel Bwxt Idaho, Llc | Apparatus for the liquefaction of natural gas and methods related to same |
| DE102006013686B3 (en) * | 2006-03-22 | 2007-10-11 | Technikum Corporation | Process for the liquefaction of natural gas |
| TW200914115A (en) * | 2007-05-14 | 2009-04-01 | Shell Int Research | Process for producing purified natural gas from natural gas comprising water and carbon dioxide |
| US9254448B2 (en) | 2007-09-13 | 2016-02-09 | Battelle Energy Alliance, Llc | Sublimation systems and associated methods |
| US9217603B2 (en) | 2007-09-13 | 2015-12-22 | Battelle Energy Alliance, Llc | Heat exchanger and related methods |
| US8899074B2 (en) | 2009-10-22 | 2014-12-02 | Battelle Energy Alliance, Llc | Methods of natural gas liquefaction and natural gas liquefaction plants utilizing multiple and varying gas streams |
| US9574713B2 (en) | 2007-09-13 | 2017-02-21 | Battelle Energy Alliance, Llc | Vaporization chambers and associated methods |
| US8555672B2 (en) | 2009-10-22 | 2013-10-15 | Battelle Energy Alliance, Llc | Complete liquefaction methods and apparatus |
| US8061413B2 (en) | 2007-09-13 | 2011-11-22 | Battelle Energy Alliance, Llc | Heat exchangers comprising at least one porous member positioned within a casing |
| GB2462125B (en) * | 2008-07-25 | 2012-04-04 | Dps Bristol Holdings Ltd | Production of liquefied natural gas |
| GB2469077A (en) | 2009-03-31 | 2010-10-06 | Dps Bristol | Process for the offshore liquefaction of a natural gas feed |
| US20120180901A1 (en) * | 2009-09-28 | 2012-07-19 | Koninklijke Philips Electronics N.V. | Sytem and method for liquefying and storing a fluid |
| DE102010030485A1 (en) | 2010-06-24 | 2011-12-29 | Dbi - Gastechnologisches Institut Ggmbh Freiberg | Process for the separation of C2 + hydrocarbons from natural gas or associated petroleum gas using membranes |
| US8337593B2 (en) | 2010-08-18 | 2012-12-25 | Uop Llc | Process for purifying natural gas and regenerating one or more adsorbers |
| US10655911B2 (en) | 2012-06-20 | 2020-05-19 | Battelle Energy Alliance, Llc | Natural gas liquefaction employing independent refrigerant path |
| US9273639B2 (en) | 2012-09-24 | 2016-03-01 | Elwha Llc | System and method for storing and dispensing fuel and ballast fluid |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2820212A1 (en) | 1978-05-09 | 1979-11-22 | Linde Ag | METHOD FOR LIQUIDATING NATURAL GAS |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3878689A (en) * | 1970-07-27 | 1975-04-22 | Carl A Grenci | Liquefaction of natural gas by liquid nitrogen in a dual-compartmented dewar |
| US3792590A (en) * | 1970-12-21 | 1974-02-19 | Airco Inc | Liquefaction of natural gas |
| US4133663A (en) * | 1976-03-29 | 1979-01-09 | Air Products And Chemicals, Inc. | Removing vinyl chloride from a vent gas stream |
| US5006138A (en) * | 1990-05-09 | 1991-04-09 | Hewitt J Paul | Vapor recovery system |
-
1994
- 1994-11-11 DE DE4440401A patent/DE4440401A1/en not_active Withdrawn
-
1995
- 1995-11-02 EP EP95117286A patent/EP0711969A3/en not_active Withdrawn
- 1995-11-09 US US08/556,195 patent/US5551256A/en not_active Expired - Fee Related
- 1995-11-09 AR AR33417395A patent/AR000098A1/en unknown
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2820212A1 (en) | 1978-05-09 | 1979-11-22 | Linde Ag | METHOD FOR LIQUIDATING NATURAL GAS |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102410702A (en) * | 2010-09-09 | 2012-04-11 | 林德股份公司 | Natural gas liquefaction |
| CN102410702B (en) * | 2010-09-09 | 2016-01-20 | 林德股份公司 | The liquefaction of natural gas |
| FR3063540A1 (en) * | 2017-03-01 | 2018-09-07 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | METHOD FOR LIQUEFACTING NATURAL GAS USING A REFRIGERATION CIRCUIT COMPRISING ONLY ONE TURBINE |
| CN108709367A (en) * | 2018-05-22 | 2018-10-26 | 中石化宁波工程有限公司 | A kind of liquefying plant and application method of carbon dioxide |
Also Published As
| Publication number | Publication date |
|---|---|
| DE4440401A1 (en) | 1996-05-15 |
| AR000098A1 (en) | 1997-05-21 |
| US5551256A (en) | 1996-09-03 |
| EP0711969A3 (en) | 1997-02-05 |
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