DE10121339A1 - Process for separating nitrogen from a nitrogen-containing hydrocarbon fraction - Google Patents
Process for separating nitrogen from a nitrogen-containing hydrocarbon fractionInfo
- Publication number
- DE10121339A1 DE10121339A1 DE2001121339 DE10121339A DE10121339A1 DE 10121339 A1 DE10121339 A1 DE 10121339A1 DE 2001121339 DE2001121339 DE 2001121339 DE 10121339 A DE10121339 A DE 10121339A DE 10121339 A1 DE10121339 A1 DE 10121339A1
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- nitrogen
- hydrocarbon
- rich
- circuit
- fraction
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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
- F25J3/0257—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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/04—Mixing or blending of fluids with the feed 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/90—Boil-off gas from storage
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
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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
- F25J2230/30—Compression of the feed 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
- 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
- F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
- 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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- 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
- F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
- F25J2260/20—Integration in an installation for liquefying or solidifying a fluid 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising loop
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-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
- F25J2270/00—Refrigeration techniques used
- F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. 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
- F25J2280/00—Control of the process or apparatus
- F25J2280/02—Control in general, load changes, different modes ("runs"), measurements
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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)
Abstract
Description
Die Erfindung betrifft die Kombination eines
The invention relates to the combination of a
- a) Verfahrens zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes, insbesondere eines Erdgas-Stromes, durch indirekten Wärmetausch mit wenigstens einem Kältemittelkreislauf und/oder durch indirekten Wärmetausch mit wenigstens einem Kältemittelgemischkreislauf, und einesa) process for liquefying a hydrocarbon-rich stream, in particular a natural gas stream, by indirect heat exchange with at least a refrigerant circuit and / or by indirect heat exchange with at least a mixed refrigerant circuit, and one
- b) Verfahrens zum Abtrennen von Stickstoff aus einer Stickstoff-enthaltenden, Kohlenwasserstoff-reichen Fraktion, die im Rahmen des Verflüssigungsverfahrens anfällt, wobei die Kohlenwasserstoff-reiche Fraktion ein- oder mehrstufig verdichtet, abgekühlt, dabei partiell kondensiert und einem Doppelkolonnen-Stickstoff- Abtrennprozess zugeführt wird.b) Process for separating nitrogen from a nitrogen-containing Hydrocarbon-rich fraction used in the liquefaction process is obtained, the hydrocarbon-rich fraction compressing in one or more stages, cooled, partially condensed and a double column nitrogen Separation process is fed.
Unter dem Begriff "Doppelkolonnen-Stickstoff-Abtrennprozess" seien die unterschiedlichsten Stickstoff-Abtrennprozesse zu verstehen, also unabhängig davon, ob es sich um einen reinen Doppelkolonnenprozess, einen Doppelkolonnenprozess mit Abscheidung der schweren Kohlenwasserstoffe, einen Doppelkolonnenprozess mit einer Stickstoff-Anreicherungskolonne mit oder ohne Abscheidung der schweren Kohlenwasserstoffe, einen Einfachkolonnenprozess mit oder ohne Vorabscheidung der schweren Kohlenwasserstoffe, etc. handelt.Under the term "double column nitrogen separation process" understand a wide variety of nitrogen separation processes, i.e. regardless of whether it is a pure double column process, a double column process with Separation of heavy hydrocarbons using a double column process a nitrogen enrichment column with or without separation of the heavy ones Hydrocarbons, a single column process with or without pre-separation of the heavy hydrocarbons, etc.
Gattungsgemäße Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes sind hinlänglich bekannt; siehe beispielsweise die DE-B 197 16 415. Diese beschreibt die Verflüssigung eines Kohlenwasserstoff-reichen Stromes gegen eine Kältemittelgemischkreislaufkaskade. Neben dem in der oben genannten DE-B 197 16 415 beschriebenen Verfahren zum Verflüssigen eines Kohlenwasserstoff reichen Stromes sind dem Fachmann eine Vielzahl weiterer Verflüssigungsverfahren bekannt. Beispielhaft genannt seien Prozesse, bei denen der zu verflüssigende Kohlenwasserstoff-reiche Strom gegen eine Kältemittelkreislaufkaskade oder mittels eines sog. Dual-Flow-Verflüssigungsprozesses verflüssigt wird.Generic process for liquefying a hydrocarbon-rich Stromes are well known; see for example DE-B 197 16 415. This describes the liquefaction of a hydrocarbon-rich stream against one Refrigerant mixture cycle cascade. In addition to that in DE-B 197 16 415 mentioned above described method for liquefying a hydrocarbon A large number of other liquefaction processes are known to those skilled in the art of rich electricity known. Examples include processes in which the liquefied Hydrocarbon-rich electricity against a refrigerant circuit cascade or by a so-called dual flow liquefaction process.
Die Verdichtung des oder der in den Kältemittelkreisläufen und/oder Kältemittel(gemisch)kreisläufen zirkulierenden Kältemittel bzw. Kältemittelgemische erfolgt mittels energieintensiver Verdichter. Zur Gewinnung der für diese Verdichter benötigten elektrischen Energie werden Gasturbinen vorgesehen, die bisher im Regelfall von einem Teilstrom des zu verflüssigenden Kohlenwasserstoff-reichen Stromes gespeist werden. Zwar können die Verbrennungssysteme und damit das Brenngas derartiger Gasturbinen vergleichsweise hohe Stickstoffkonzentrationen tolerieren, sie haben jedoch den Nachteil, dass der NOX-Gehalt ihres Abgases vergleichsweise hoch ist, d. h. bspw. < 25 Mol-ppm NOX.The compression of the refrigerant or refrigerant or refrigerant mixture circulating in the refrigerant circuits and / or refrigerant (mixture) circuits is carried out by means of energy-intensive compressors. To obtain the electrical energy required for these compressors, gas turbines are provided which, as a rule, have previously been fed by a partial stream of the hydrocarbon-rich stream to be liquefied. Although the combustion systems and thus the fuel gas of such gas turbines can tolerate comparatively high nitrogen concentrations, they have the disadvantage that the NO x content of their exhaust gas is comparatively high, ie for example <25 mol-ppm NO x .
Es existieren bereits sog. Low-NOX-Gasturbinen (dies sind Gasturbinen, die mit einem sog. "Dry-Low-NOX-Emission-Combustion-System" ausgerüstet sind), die jedoch mit einem vergleichsweise Stickstoffarmen Gasgemisch betrieben werden müssen. Der maximale Stickstoffgehalt des den Turbinen zugeführten Brenngases sollte je nach Turbinentyp 10-30 Mol-% nicht übersteigen, um den gewünschten NOX-Grenzwert von max. 25 Mol-ppm für das Gasturbinenabgas nicht zu überschreiten.There are already so-called low-NO x gas turbines (these are gas turbines which are equipped with a so-called "dry-low-NO x emission combustion system") which, however, have to be operated with a comparatively low-nitrogen gas mixture. The maximum nitrogen content of the fuel gas supplied to the turbines should not exceed 10-30 mol%, depending on the turbine type, in order to achieve the desired NO x limit value of max. Not to exceed 25 mole ppm for the gas turbine exhaust gas.
Darüber hinaus muss darauf geachtet werden, dass Veränderungen betreffend den sog. Low-Heating-Value (LHV), die sog. Specific Gravity und den Wobbe-Index des Kohlenwasserstoff-reichen Brennstoffgases auf bspw. ± 1% innerhalb von bspw. 30 Sekunden limitiert sind, da nur dadurch ein stabiler Betrieb der Gasturbine garantiert werden kann, ohne dass es z. B. zu Instabilitäten hinsichtlich der Flamme kommt.In addition, care must be taken to ensure that changes regarding the So-called Low Heating Value (LHV), the so-called Specific Gravity and the Wobbe Index of the Hydrocarbon-rich fuel gas to, for example, ± 1% within, for example, 30 Seconds are limited, as this is the only way to guarantee stable operation of the gas turbine can be without z. B. instabilities with regard to the flame.
Aufgabe der vorliegenden Erfindung ist es, eine gattungsgemäße Verfahrenskombination anzugeben, die eine Verringerung des Energieverbrauches des Stickstoff-Abtrennverfahrens bei gleichzeitiger Verringerung von dessen Investitionskosten ermöglicht.The object of the present invention is a generic Specify combination of processes that reduce energy consumption of the Nitrogen separation process while reducing it Investment costs enabled.
Dies wird dadurch erreicht, dass die Abkühlung und partielle Kondensation der Stickstoff-enthaltenden, Kohlenwasserstoff-reichen Fraktion gegen den oder wenigstens einen der Kältemittelkreisläufe und/oder Kältemittelgemischkreisläufe des Verfahrens zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes erfolgt. This is achieved in that the cooling and partial condensation of the Nitrogen-containing, hydrocarbon-rich fraction against the or at least one of the refrigerant circuits and / or mixed refrigerant circuits of the Process for liquefying a hydrocarbon-rich stream is carried out.
Sofern die Verflüssigung des Kohlenwasserstoff-reichen Stromes durch indirekten Wärmetausch mit den Kältemitteln einer Kältemittelgemischkreislaufkaskade erfolgt, wobei die Kältemittelgemischkreislaufkaskade aus wenigstens 3 unterschiedliche Kältemittelzusammensetzungen aufweisenden Kältemittelgemischkreisläufen besteht, und der erste der drei Kältemittelgemischkreisläufe der Vorkühlung (Vorkühlungskreislauf), der zweite Kältemittelgemischkreislauf der Verflüssigung (Verflüssigungskreislauf) und der dritte Kältemittelgemischkreislauf der Unterkühlung (Unterkühlungskreislauf) des zu verflüssigenden Kohlenwasserstoff-reichen Stromes dient, so erfolgt - entsprechend einer vorteilhaften Ausgestaltung der erfindungsgemäßen Verfahrenskombination - die Abkühlung und partielle Kondensation der Stickstoff-enthaltenden, Kohlenwasserstoff-reichen Fraktion gegen den Vorkühlungskreislauf und den Unterkühlungskreislauf des Verfahrens zum Verflüssigen des Kohlenwasserstoff-reichen Stromes.If the liquefaction of the hydrocarbon-rich stream by indirect Heat exchange takes place with the refrigerants of a refrigerant mixture circuit cascade, wherein the refrigerant mixture circuit cascade consists of at least 3 different ones Refrigerant mixture circuits having refrigerant compositions, and the first of the three pre-cooling mixed refrigerant circuits (Pre-cooling circuit), the second refrigerant mixture circuit of the liquefaction (Liquefaction circuit) and the third refrigerant mixture circuit of the supercooling (Subcooling circuit) of the hydrocarbon-rich stream to be liquefied serves, so takes place - according to an advantageous embodiment of the Process combination according to the invention - the cooling and partial Condensation of the nitrogen-containing, hydrocarbon-rich fraction against the pre-cooling circuit and the sub-cooling circuit of the process for Liquefying the hydrocarbon-rich stream.
Die Erfindung sowie weitere Ausgestaltungen derselben seien anhand des in den Fig. 1 und 2 dargestellten Ausführungsbeispieles näher erläutert.The invention and further refinements of the same will be explained in more detail with reference to the embodiment shown in FIGS. 1 and 2.
Hierbei zeigen:Here show:
Fig. 1 eine dreistufige Verdichtereinheit, die der Verdichtung des Stickstoff enthaltenden, Kohlenwasserstoff-reichen Stromes dient Fig. 1 shows a three-stage compressor unit, which serves the compression of the nitrogen-containing, hydrocarbon-rich stream
Fig. 2 eine mögliche Ausführungsform eines Doppelkolonnen-Stickstoff- Abtrennpozesses. Fig. 2 shows a possible embodiment of a double column nitrogen separation process.
Wie in der Fig. 1 dargestellt, wird über Leitung 1 einer dreistufigen Verdichtereinheit - die drei Stufen der Verdichtereinheit sind mit V1, V2 sowie V3 bezeichnet - eine Stickstoff-enthaltende, Kohlenwasserstoff-reiche Fraktion zugeführt. Diese kann sich aus beliebigen, innerhalb des jeweiligen Verflüssigungsverfahrens anfallenden Stickstoff-enthaltenden, Kohlenwasserstoff-reichen Strömen, beispielsweise aus einem Stickstoff-Stripper, Boil-off-Gas, etc., zusammensetzen. Der Stickstoff-enthaltenden, Kohlenwasserstoff-reichen Fraktion kann über Leitung 2 zumindest zeitweilig ein Stickstoffreicher Strom - auf den im Folgenden noch näher eingegangen werden wird - zugemischt werden. As shown in FIG. 1, a nitrogen-containing, hydrocarbon-rich fraction is fed via line 1 to a three-stage compressor unit - the three stages of the compressor unit are designated V1, V2 and V3. This can be composed of any nitrogen-containing, hydrocarbon-rich streams occurring within the respective liquefaction process, for example a nitrogen stripper, boil-off gas, etc. The nitrogen-containing, hydrocarbon-rich fraction can at least temporarily be mixed with a nitrogen-rich stream via line 2 - which will be discussed in more detail below.
Die Stickstoff-enthaltende, Kohlenwasserstoff-reiche Fraktion, der gegebenenfalls der über Leitung 2 herbeigeführte Stickstoff-reiche Strom zugemischt wurde, wird bei geringfügig überatmosphärischem Druck über Leitung 3 der ersten Verdichterstufe V1 zugeführt. Nach erfolgter Verdichtung wird diese Fraktion über Leitung 4 einem Nachkühler 1 zugeführt und in diesem abgekühlt. Diese Prozedur wiederholt sich nach der 2. und 3. Verdichterstufe V2 bzw. V3 in den entsprechenden Nachkühlern E2 bzw. E3. Die über Leitung 6 aus der Verdichtereinheit abgezogene Stickstoff-enthaltende, Kohlenwasserstoff-reiche Fraktion weist bei einer Temperatur von 5 bis 40°C einen Druck zwischen 35 und 65 bar auf.The nitrogen-containing, hydrocarbon-rich fraction, to which the nitrogen-rich stream brought in via line 2 was optionally added, is fed via line 3 to the first compressor stage V1 at a slightly above atmospheric pressure. After compression, this fraction is fed via line 4 to an aftercooler 1 and cooled there. This procedure is repeated after the 2nd and 3rd compressor stages V2 and V3 in the corresponding aftercoolers E2 and E3. The nitrogen-containing, hydrocarbon-rich fraction drawn off from the compressor unit via line 6 has a pressure between 35 and 65 bar at a temperature of 5 to 40 ° C.
Die aus der Verdichtereinheit abgezogene Stickstoff-enthaltende, Kohlenwasserstoff reiche Fraktion wird nunmehr - wie im Folgenden in der Fig. 2 dargestellt - im Wärmetauscher E4 gegen den hochreinen Stickstoff-Strom, der dem Wärmetauscher E4 über Leitung 16 zugeführt wird und auf den im Folgenden noch näher eingegangen werden wird, sowie erfindungsgemäß gegen einen Kältemittel(gemisch)strom x auf eine Temperatur zwischen -20 und -60°C abgekühlt. Die in der Fig. 2 dargestellten Wärmetauscher E4 bis E7 sind hierbei vorzugsweise als sog. Plattenwärmetauscher ausgebildet.The nitrogen-containing, hydrocarbon-rich fraction drawn off from the compressor unit is now - as shown in FIG. 2 below - in the heat exchanger E4 against the high-purity nitrogen stream which is fed to the heat exchanger E4 via line 16 and in the following will be discussed in more detail, and according to the invention cooled against a refrigerant (mixture) stream x to a temperature between -20 and -60 ° C. The heat exchangers E4 to E7 shown in FIG. 2 are preferably designed as so-called plate heat exchangers.
Die Stickstoff-enthaltende, Kohlenwasserstoff-reiche Fraktion wird anschließend über Leitung 8 einem weiteren Wärmetauscher E5 zugeführt und in diesem wiederum gegen den bereits erwähnten hochreinen Stickstoff-Strom in der Leitung 15 sowie einen weiteren Kältemittel(gemisch)strom y auf eine Temperatur zwischen -80 und -120°C abgekühlt.The nitrogen-containing, hydrocarbon-rich fraction is then fed via line 8 to a further heat exchanger E5 and in this again against the already mentioned high-purity nitrogen stream in line 15 and another refrigerant (mixture) stream y to a temperature between -80 and cooled to -120 ° C.
Sofern es sich bei dem Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes um ein Kältemittelgemischkreislaufkaskadenverfahren handelt, ist es zweckmäßig, für die Abkühlung der Stickstoff-enthaltenden, Kohlenwasserstoff-reichen Fraktion diese im Wärmetauscher E4 gegen den Vorkühlungskreislauf x der Kältemittelgemischkreislaufkaskade und im Wärmetauscher E5 gegen den Unterkühlungskreislauf y der Kältemittelgemischkreislaufkaskade abzukühlen und partiell zu kondensieren. If it is in the process of liquefying a hydrocarbon-rich Stromes is a mixed refrigerant cycle cascade process, it is useful for cooling the nitrogen-containing, hydrocarbon-rich Fraction this in the heat exchanger E4 against the pre-cooling circuit x Refrigerant mixture circuit cascade and in the heat exchanger E5 against the Cool the supercooling circuit y of the refrigerant mixture circuit cascade and to partially condense.
Anschließend wird die Stickstoff-enthaltende, Kohlenwasserstoff-reiche Fraktion über Leitung 9 dem Wärmetauscher E6 zugeführt, in diesem gegen einen Aufkocher, der aus der unteren Kolonne a der Doppelkolonne K über Leitung 11 abgezogen und dieser anschließend wieder aufgegeben wird, auf eine Temperatur von -120 bis -140 °C abgekühlt, bevor die Stickstoff-enthaltende, Kohlenwasserstoff-reiche Fraktion über Leitung 10 der unteren Kolonne a der Doppelkolonne K zugeführt wird. Die untere Kolonne a weist einen Arbeitsdruck von ca. 30 bar auf.The nitrogen-containing, hydrocarbon-rich fraction is then fed via line 9 to the heat exchanger E6, in which it is heated to a temperature of - against a reboiler which is drawn off from the lower column a of the double column K via line 11 and which is subsequently fed back in again. Cooled to 120 to -140 ° C. before the nitrogen-containing, hydrocarbon-rich fraction is fed via line 10 to the lower column a of the double column K. The lower column a has a working pressure of approximately 30 bar.
Aus dem Sumpf der unteren Kolonne a wird über Leitung 12 eine an Stickstoff abgereicherte, Kohlenwasserstoff-reiche Fraktion abgezogen und in dem bereits beschriebenen Wärmetauscher E5 auf eine Temperatur zwischen -155 und -160°C abgekühlt, bevor diese Fraktion über Leitung 13 und Entspannungsventil 13' der oberen Kolonne b der Doppelkolonne K aufgegeben wird. Die obere Kolonne b weist einen Arbeitsdruck von ca. 2 bar auf.From the sump of lower column a, a-depleted nitrogen via line 12, withdrawn hydrocarbon-rich fraction and cooled in the already described heat exchanger E5 to a temperature of -155 to -160 ° C before this fraction via line 13 and expansion valve 13 'the upper column b of the double column K is abandoned. The upper column b has a working pressure of approximately 2 bar.
Aus dem Kopfbereich der unteren Kolonne a der Doppelkolonne K wird über Leitung 14 eine an Stickstoff angereicherte, Kohlenwasserstoff-reiche Flüssig- oder ggf. Gasfraktion abgezogen, im Wärmetauscher E7 abgekühlt, dabei ggf. partiell kondensiert und als Rücklauf auf den Kopf der oberen Kolonne b der Doppelkolonne K gegeben.From the top area of the lower column a of the double column K, a nitrogen-enriched, hydrocarbon-rich liquid or, if appropriate, gas fraction is drawn off via line 14 , cooled in the heat exchanger E7, where appropriate partially condensed and returned to the top of the upper column b given the double column K.
Am Kopf der oberen Kolonne b der Doppelkolonne K wird über Leitung 15 die bereits erwähnte hochreine Stickstoff-Gasfraktion, die einen Kohlenwasserstoffrestgehalt von z. B. < 100 ppm und eine Temperatur von -190°C aufweist, abgezogen. Diese Gasfraktion wird zunächst im Wärmetauscher E7 angewärmt und anschließend den bereits beschriebenen Wärmetauschern E4 und E5 zugeführt und in diesen gegen die Stickstoff-enthaltende, Kohlenwasserstoff-reiche Fraktion, die der Doppelkolonne K zur Auftrennung zugeführt wird, angewärmt.At the top of the upper column of the double column K b is fed via line 15 the above-mentioned high-purity nitrogen gas fraction containing a hydrocarbon residual content of z. B. <100 ppm and a temperature of -190 ° C, deducted. This gas fraction is first heated in the heat exchanger E7 and then fed to the already described heat exchangers E4 and E5 and heated therein to the nitrogen-containing, hydrocarbon-rich fraction which is fed to the double column K for separation.
Die angewärmte hochreine Stickstoff-Gasfraktion kann über Leitung 17 an die Atmosphäre abgegeben werden. Auch kann - wie bereits beschrieben - über Leitung 2 ein Teilstrom dieser Gasfraktion vor die Verdichterstation V1 bis V3 zurückgeführt werden. The heated, highly pure nitrogen gas fraction can be released into the atmosphere via line 17 . As already described, a partial stream of this gas fraction can also be returned to the compressor station V1 to V3 via line 2 .
Diese Verfahrensführung dient dazu, den Stickstoffgehalt der der Verdichterstation V1 bis V3 zugeführten Gasfraktion über einer gewünschten oder benötigten Mindestkonzentration von bspw. 15% zu halten. Würde diese Mindestkonzentration unterschritten, könnte die gewünschte Stickstoff-Reinheit in dem an die Atmosphäre abgegebenen Stromes ohne einen zusätzlichen Vortrennschritt nicht erreicht werden. Zudem wird der Betrieb des erfindungsgemäßen Verfahrens vereinfacht und stabilisiert, da die Schwankungen in der der Verdichterstation V1 bis V3 zugeführten Gasfraktion hinsichtlich des Stickstoffgehaltes minimiert werden können. Dies ist jedoch nur zu Lasten eines höheren Energieverbrauches möglich.This procedure is used to determine the nitrogen content of the compressor station V1 up to V3 supplied gas fraction over a desired or required To maintain a minimum concentration of 15%, for example. Would this minimum concentration could fall below the desired nitrogen purity in the atmosphere emitted current can not be achieved without an additional pre-separation step. In addition, the operation of the method according to the invention is simplified and stabilized because the fluctuations in the compressor station V1 to V3 fed Gas fraction can be minimized with regard to the nitrogen content. This is however only possible at the expense of higher energy consumption.
Über einen Seitenabzug (Leitung 18) wird aus dem unteren Bereich der oberen Kolonne b der Doppelkolonne K eine Methan-reiche Flüssigfraktion abgezogen, die beispielsweise einer Stickstoff-Stripp-Kolonne - die bspw. in einem LNG-Prozess integriert ist - zugeführt werden kann. Dies kann entweder mittels Gravitation oder durch Pumpen der Flüssigkeit erfolgen. Die Methan-reiche Flüssigfraktion weist - entsprechend einer Ausgestaltung der Erfindung - vorzugsweise einen Stickstoffgehalt von maximal 5 Vol.-% auf.Via a side draw (line 18 ), a methane-rich liquid fraction is drawn off from the lower region of the upper column b of the double column K and can be fed, for example, to a nitrogen stripping column - which is integrated, for example, in an LNG process. This can be done either by gravity or by pumping the liquid. According to one embodiment of the invention, the methane-rich liquid fraction preferably has a nitrogen content of at most 5% by volume.
Wurde bisher für die Abkühlung des zu zerlegenden Stickstoff-enthaltenden, Kohlenwasserstoff-reichen Stromes im Regelfall der abgetrennte Kohlenwasserstoff reiche Strom (bspw. der Methan-Strom) angewärmt und dabei wieder verdampft, so erfolgt die Kältebereitstellung nunmehr erfindungsgemäß durch die beiden Kältemittelkreisläufe bzw. Kältemittelgemischkreisläufe x und y. Abhängig von dem jeweils realisierten Verflüssigungsverfahren des Kohlenwasserstoff-reichen Stromes kann die Abkühlung und partielle Kondensation des aufzutrennenden Stickstoff enthaltenden, Kohlenwasserstoff-reichen Stromes selbstverständlich auch gegen lediglich einen Kältemittelstrom oder Kältemittelgemischstrom erfolgen. Dadurch kann der Kohlenwasserstoff-reiche Strom in flüssiger Form (siehe Seitenabzug über Leitung 18) aus dem Prozess bzw. der Anlage abgezogen werden.While the separated hydrocarbon-rich stream (e.g. the methane stream) has been previously warmed up and then evaporated again to cool the nitrogen-containing, hydrocarbon-rich stream to be decomposed, the refrigeration is now provided according to the invention by the two refrigerant circuits or refrigerant mixture cycles x and y. Depending on the particular liquefaction process of the hydrocarbon-rich stream, the cooling and partial condensation of the nitrogen-containing, hydrocarbon-rich stream to be separated can of course also be carried out against only one refrigerant stream or refrigerant mixture stream. This allows the hydrocarbon-rich electricity to be withdrawn from the process or the system in liquid form (see side draw via line 18 ).
Claims (7)
- a) Verfahrens zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes, insbesondere eines Erdgas-Stromes, durch indirekten Wärmetausch mit wenigstens einem Kältemittelkreislauf und/oder durch indirekten Wärmetausch mit wenigstens einem Kältemittelgemischkreislauf, und eines
- b) Verfahrens zum Abtrennen von Stickstoff aus einer Stickstoff-enthaltenden, Kohlenwasserstoff-reichen Fraktion, die im Rahmen des Verflüssigungsverfahrens anfällt, wobei die Kohlenwasserstoff-reiche Fraktion ein- oder mehrstufig verdichtet, abgekühlt, dabei partiell kondensiert und einem Doppelkolonnen- Stickstoff-Abtrennprozess zugeführt wird,
- a) Process for liquefying a hydrocarbon-rich stream, in particular a natural gas stream, by indirect heat exchange with at least one refrigerant circuit and / or by indirect heat exchange with at least one refrigerant mixture circuit, and one
- b) Process for separating nitrogen from a nitrogen-containing, hydrocarbon-rich fraction which is obtained as part of the liquefaction process, the hydrocarbon-rich fraction being compressed in one or more stages, cooled, partially condensed and fed to a double-column nitrogen separation process becomes,
Priority Applications (4)
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DE2001121339 DE10121339A1 (en) | 2001-05-02 | 2001-05-02 | Process for separating nitrogen from a nitrogen-containing hydrocarbon fraction |
PCT/EP2002/004721 WO2002088612A1 (en) | 2001-05-02 | 2002-04-29 | Method for separating nitrogen out of a hydrocarbon-rich fraction that contains nitrogen |
AU2002319155A AU2002319155B2 (en) | 2001-05-02 | 2002-04-29 | Method for separating nitrogen out of a hydrocarbon-rich fraction that contains nitrogen |
NO20034865A NO20034865D0 (en) | 2001-05-02 | 2003-10-31 | Process for separating nitrogen from a nitrogen-containing hydrocarbon-rich fraction |
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DE (1) | DE10121339A1 (en) |
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WO2008098704A2 (en) * | 2007-02-13 | 2008-08-21 | Linde Aktiengesellschaft | Method for liquefying a stream rich in hydrocarbons |
FR2991442A1 (en) * | 2012-05-31 | 2013-12-06 | Air Liquide | APPARATUS AND METHOD FOR CRYOGENIC SEPARATION OF A MIXTURE OF CARBON MONOXIDE AND METHANE AND HYDROGEN AND / OR NITROGEN |
Families Citing this family (4)
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EP1715267A1 (en) | 2005-04-22 | 2006-10-25 | Air Products And Chemicals, Inc. | Dual stage nitrogen rejection from liquefied natural gas |
DE102009009477A1 (en) * | 2009-02-19 | 2010-08-26 | Linde Aktiengesellschaft | Process for separating nitrogen |
DE102009038458A1 (en) * | 2009-08-21 | 2011-02-24 | Linde Ag | Process for separating nitrogen from natural gas |
WO2014173598A2 (en) * | 2013-04-22 | 2014-10-30 | Shell Internationale Research Maatschappij B.V. | Method and apparatus for producing a liquefied hydrocarbon stream |
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DE19716415C1 (en) * | 1997-04-18 | 1998-10-22 | Linde Ag | Process for liquefying a hydrocarbon-rich stream |
DE69602771T2 (en) * | 1995-02-03 | 1999-10-21 | Air Products And Chemicals, Inc. | Process for removing nitrogen from natural gas |
DE19920312A1 (en) * | 1999-05-03 | 2000-11-09 | Linde Ag | Process for liquefying a hydrocarbon-rich stream comprises liquefying a partial stream against a stream from a cryogenic air decomposition plant on a corresponding temperature level |
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GB1181049A (en) * | 1967-12-20 | 1970-02-11 | Messer Griesheim Gmbh | Process for the Liquifaction of Natural Gas |
DE1915218B2 (en) * | 1969-03-25 | 1973-03-29 | Linde Ag, 6200 Wiesbaden | METHOD AND DEVICE FOR LIQUIFYING NATURAL GAS |
DE2438443C2 (en) * | 1974-08-09 | 1984-01-26 | Linde Ag, 6200 Wiesbaden | Process for liquefying natural gas |
DE2502959A1 (en) * | 1975-01-24 | 1976-07-29 | Linde Ag | Natural gas liquefaction process - with circulating medium leakage compensated by higher boiling liquid fraction from feed stock |
IT1176290B (en) * | 1984-06-12 | 1987-08-18 | Snam Progetti | LOW-BOILING GAS COOLING AND LIQUEFATION PROCESS |
US4680041A (en) * | 1985-12-30 | 1987-07-14 | Phillips Petroleum Company | Method for cooling normally gaseous material |
-
2001
- 2001-05-02 DE DE2001121339 patent/DE10121339A1/en not_active Withdrawn
-
2002
- 2002-04-29 WO PCT/EP2002/004721 patent/WO2002088612A1/en active IP Right Grant
- 2002-04-29 AU AU2002319155A patent/AU2002319155B2/en not_active Ceased
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Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
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DE69602771T2 (en) * | 1995-02-03 | 1999-10-21 | Air Products And Chemicals, Inc. | Process for removing nitrogen from natural gas |
DE19716415C1 (en) * | 1997-04-18 | 1998-10-22 | Linde Ag | Process for liquefying a hydrocarbon-rich stream |
DE19920312A1 (en) * | 1999-05-03 | 2000-11-09 | Linde Ag | Process for liquefying a hydrocarbon-rich stream comprises liquefying a partial stream against a stream from a cryogenic air decomposition plant on a corresponding temperature level |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
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WO2008098704A2 (en) * | 2007-02-13 | 2008-08-21 | Linde Aktiengesellschaft | Method for liquefying a stream rich in hydrocarbons |
WO2008098704A3 (en) * | 2007-02-13 | 2012-03-01 | Linde Aktiengesellschaft | Method for liquefying a stream rich in hydrocarbons |
FR2991442A1 (en) * | 2012-05-31 | 2013-12-06 | Air Liquide | APPARATUS AND METHOD FOR CRYOGENIC SEPARATION OF A MIXTURE OF CARBON MONOXIDE AND METHANE AND HYDROGEN AND / OR NITROGEN |
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NO20034865L (en) | 2003-10-31 |
NO20034865D0 (en) | 2003-10-31 |
WO2002088612A1 (en) | 2002-11-07 |
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