DE102005000634A1 - Process for separating a C2 + -rich fraction from LNG - Google Patents
Process for separating a C2 + -rich fraction from LNG Download PDFInfo
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- DE102005000634A1 DE102005000634A1 DE102005000634A DE102005000634A DE102005000634A1 DE 102005000634 A1 DE102005000634 A1 DE 102005000634A1 DE 102005000634 A DE102005000634 A DE 102005000634A DE 102005000634 A DE102005000634 A DE 102005000634A DE 102005000634 A1 DE102005000634 A1 DE 102005000634A1
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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
-
- 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
- F25J3/0214—Liquefied 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
- F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
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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
- F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
- F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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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
- F25J2215/62—Ethane or ethylene
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
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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
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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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)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
Es wird ein Verfahren zum Abtrennen einer C¶2+¶-reichen Fraktion aus verflüssigtem Erdgas (LNG) beschrieben, das folgende Verfahrensschritte aufweist: DOLLAR A a) teilweises Verdampfen (E1, E2) des verflüssigten Erdgases (1, 1'), DOLLAR A b) Auftrennen (D1) des teilweise verdampften Erdgases (2) in eine erste C¶1¶-reiche Gasfraktion (4) und eine erste C¶2+¶-reiche Flüssigfraktion (3), DOLLAR A c) rektifikatorische Auftrennung (T) der ersten C¶2+¶-reichen Flüssigfraktion (3) in eine zweite C¶1¶-reiche Gasfraktion (8) und eine zweite C¶2+¶-reiche Flüssigfraktion (10), DOLLAR A d) Rückverflüssigen (E1) der ersten C¶1¶-reichen Gasfraktion (4) und DOLLAR A e) Zuführen wenigstens eines Teilstromes (6) der rückverflüssigten C¶1¶-reichen Gasfraktion (5) als Rücklauf zu der rektifikatorischen Auftrennung (T).The invention relates to a method for separating a C¶2 + ¶-rich fraction of liquefied natural gas (LNG), comprising the following method steps: DOLLAR A a) partial evaporation (E1, E2) of the liquefied natural gas (1, 1 '), DOLLAR A b) separating (D1) the partially vaporized natural gas (2) into a first C¶1¶-rich gas fraction (4) and a first C¶2 + ¶ -rich liquid fraction (3), DOLLAR A c) rectificatory separation (T ) of the first C¶2 + ¶-rich liquid fraction (3) into a second C¶1¶-rich gas fraction (8) and a second C¶2 + ¶ -rich liquid fraction (10), DOLLAR A d) reliquefying (E1) the first C¶1¶-rich gas fraction (4) and DOLLAR A e) supplying at least a partial stream (6) of the reliquefied C¶1¶-rich gas fraction (5) as reflux to the rectificatory separation (T).
Description
Die Erfindung betrifft ein Verfahren zum Abtrennen einer C2+-reichen Fraktion aus verflüssigtem Erdgas (LNG).The invention relates to a method for separating a C 2+ -rich fraction from liquefied natural gas (LNG).
Gattungsgemäße Verfahren sind bspw. dann vorzusehen, wenn der Heizwert von verflüssigtem Erdgas nicht den gewünschten Spezifikationen desjenigen Pipeline-Netzes, in das das Erdgas eingespeist werden soll, entspricht. In einem derartigen Fall wird dem verflüssigten Erdgas entweder eine Heizwert-erniedrigende Komponente, beispielsweise Stickstoff, zugesetzt oder es werden Komponenten, die eine Erhöhung des Heizwertes bewirken, aus dem verflüssigten Erdgas entfernt. Nachfolgend sei die vorgenannte zweite Alternative näher erläutert.Generic method are to be provided, for example, when the calorific value of liquefied natural gas not the desired one Specifications of the pipeline network into which natural gas is fed is to be, corresponds. In such a case, the liquefied Natural gas either a calorific value-lowering component, such as nitrogen, added or there are components that increase the Heating effect, removed from the liquefied natural gas. following Let me explain the aforementioned second alternative in more detail.
Aus der US-A 5,114,451 ist ein gattungsgemäßes Verfahren zum Abtrennen einer C2+- bzw. C3+-reichen Fraktion aus LNG bekannt, bei dem – im Gegensatz zu den bis dato realisierten Verfahren – ein Teilstrom der in der rektifikatorischen Auftrennung des (verflüssigten) Erdgases gewonnenen C1-reichen Gasfraktion rückverflüssigt und der rektifikatorischen Auftrennung als Rücklauf aufgegeben wird. Der Reststrom der C1-reichen Gasfraktion wird erst nach der Abtrennung des Teilstromes, der den vorbeschriebenen Rücklaufstrom bildet, auf den gewünschten Abgabe- bzw. Pipelinedruck verdichtet. Das in der US-A 5,114,451 beschriebene Verfahren ermöglicht zwar die Steigerung der Ethanausbeute auf wirtschaftlich interessante Werte, erkauft wird dies jedoch durch den Einsatz wenigstens eines kostenintensiven Verdichters.From US-A 5,114,451 a generic method for separating a C 2+ - or C 3+ -rich fraction from LNG is known, in which - in contrast to the hitherto realized method - a partial flow in the rectification separation of the ( liquefied) natural gas obtained C 1 -rich gas fraction is liquefied and the rectification separation is given up as reflux. The residual flow of the C 1 -rich gas fraction is compressed to the desired discharge or pipeline pressure only after the separation of the partial stream, which forms the above-described return flow. Although the process described in US Pat. No. 5,114,451 makes it possible to increase the ethane yield to economically interesting values, this is paid for by the use of at least one cost-intensive compressor.
Auch aus der US-A 3,420,068 ist ein gattungsgemäßes Verfahren zum Abtrennen einer C2+-reichen Fraktion aus LNG bekannt. Bei diesem wird auf eine Rückverdichtung der in der rektifikatorischen Auftrennung des teilweise verdampften Erdgases gewonnenen methanreichen Gasfraktion verzichtet, was zur Folge hat, dass lediglich durchschnittliche Ethanausbeuten erzielt werden können.Also from US-A 3,420,068 a generic method for separating a C 2+ -rich fraction of LNG is known. In this case, a recompression of the methane-rich gas fraction obtained in the rectification separation of the partially vaporized natural gas is dispensed with, with the result that only average ethane yields can be achieved.
Aufgabe der vorliegenden Erfindung ist es, ein gattungsgemäßes Verfahren zum Abtrennen einer C2+-reichen Fraktion aus verflüssigtem Erdgas (LNG) anzugeben, das eine Steigerung der Ausbeute der C2+-reichen Fraktion bei gleichzeitiger Reduzierung der Investitions- sowie Betriebskosten des Prozesses, insbesondere den Verzicht auf eine Verdichtung der methanreichen Gasfraktion ermöglicht.The object of the present invention is to provide a generic method for separating a C 2+ -rich fraction from liquefied natural gas (LNG), which increases the yield of the C 2+ -rich fraction while reducing the investment and operating costs of the process, in particular the waiver of a compression of the methane-rich gas fraction allows.
Zur Lösung der vorgenannten Aufgabe wird ein gattungsgemäßes Verfahren zum Abtrennen einer C2+-reichen Fraktion aus verflüssigtem Erdgas (LNG) vorgeschlagen, das folgende Verfahrensschritte aufweist:
- a) teilweises Verdampfen des verflüssigten Erdgases,
- b) Auftrennen des teilweise verdampften Erdgases in eine erste C1-reiche Gasfraktion und eine erste C2+-reiche Flüssigfraktion,
- c) rektifikatorische Auftrennung der ersten C2+-reichen Flüssigfraktion in eine zweite C1-reiche Gasfraktion und eine zweite C2+-reiche Flüssigfraktion,
- d) Rückverflüssigen der ersten C1-reichen Gasfraktion und
- e) Zuführen wenigstens eines Teilstromes der rückverflüssigten C1-reichen Gasfraktion als Rücklauf zu der rektifikatorischen Auftrennung.
- a) partial evaporation of the liquefied natural gas,
- b) separating the partially vaporized natural gas into a first C 1 -rich gas fraction and a first C 2+ -rich liquid fraction,
- c) rectification separation of the first C 2+ -rich liquid fraction in a second calcareous C 1 gas fraction and a second liquid fraction rich in C 2+,
- d) re-liquefying the first C 1 -rich gas fraction and
- e) supplying at least a partial stream of the reliquefied C 1 -rich gas fraction as reflux to the rectification separation.
Im Gegensatz zu den eingangs erwähnten Verfahrensweisen wird nunmehr die in der Auftrennung des teilweise verdampften Erdgases gewonnene erste C1-reiche Gasfraktion rückverflüssigt und zumindest teilweise der rektifikatorischen Auftrennung als Rücklauf zu geführt. Die für die Rückverflüssigung der ersten C1-reichen Gasfraktion erforderliche Kälte kann hierbei ausschließlich von dem flüssigen Erdgasstrom, der einer Anwärmung bis höchstens zum Siedepunkt unterworfen wird, bereitgestellt werden. Da die der rektifikatorischen Auftrennung als Rücklauf aufgegebene C1-reiche Gasfraktion einen vergleichsweise geringen Ethangehalt aufweist, wird durch sie eine Rückwaschung von Ethan und schwereren Komponenten aus dem Kopfprodukt der rektifikatorischen Auftrennungen und damit die gewünschte Erhöhung der C2+-Ausbeute bewirkt.In contrast to the methods mentioned above, the first C 1 -rich gas fraction obtained in the separation of the partially vaporized natural gas is now reliquefied and at least partially fed to the rectification separation as reflux. The cold required for the re-liquefaction of the first C 1 -rich gas fraction can be provided exclusively by the liquid natural gas stream, which is subjected to heating up to at most the boiling point. Since the rectification separation discontinued as reflux C 1 -rich gas fraction has a relatively low ethane content, a back washing of ethane and heavier components from the overhead product of the rectification separations and thus the desired increase in C is effected 2+ yield through it.
Das erfindungsgemäße Verfahren ermöglicht es daher, bei einer wirtschaftlich sinnvollen Verfahrensweise Ethan-Ausbeuten von mehr als 90 % zu realisieren. Dieser Wert liegt im Bereich der Ethan-Ausbeute, wie sie mit dem aufwendigen Verfahren gemäß US-A 5,114,451 erreicht werden kann, aber deutlich über dem Wert bei einer Verfahrensführung gemäß US-A 3,420,068.The inventive method allows it therefore, in an economically reasonable procedure ethane yields of more than 90%. This value is in the range of ethane yield, as achieved by the complex process according to US-A 5,114,451 can, but clearly over the value in a procedure according to US-A 3,420,068.
Das
erfindungsgemäße Verfahren
sowie weitere Ausgestaltungen desselben, die Gegenstände der
abhängigen
Patentansprüche
darstellen, seien im Folgenden anhand des in den
Wie
in der
Anschließend wird
das angewärmte
Erdgas über
Leitung
Der
teilverdampfte Erdgasstrom wird über Leitung
In
der Trennkolonne T erfolgt eine rektifikatorische Auftrennung der
vorbeschriebenen C2+-reichen Flüssigfraktion
Die
vorgenannte zweite C2+-reiche Flüssigfraktion
wird über
die Leitung
In
vorteilhafter Weise erfolgt die rektifikatorische Auftrennung T
auf einem höheren
Druck als die Auftrennung D1 des teilweise verdampften Erdgases
Die
bei der Auftrennung des teilweise verdampften Erdgasstromes
Die
in der rektifikatorischen Auftrennung T gewonnene zweite C1-reiche Gasfraktion wird am Kopf der Trennkolonne
T über
Leitung
Aus
dem Pumpenvorlagebehälter
D2 wird die C2+-abgereicherte LNG-Produktfraktion
mittels der Pumpe P4 auf den gewünschten
Abgabe- bzw. Pipelinedruck – dieser
liegt in der Regel zwischen 50 und 150 bar – gepumpt und über Leitung
Sofern
die in der rektifikatorischen Auftrennung T gewonnene zweite C2+-reiche Flüssigfraktion, die aus dem Sumpf
der Trennkolonne T über
Leitung
Hierbei
wird die zweite C2+-reiche Flüssigfraktion
einer (zweiten) rektifikatorischen C2/C3-Trennung in der Trennkolonne T' unterworfen. Aus
dem Sumpf der Trennkolonne T' wird über Leitung
Am
Kopf der Trennkolonne T' wird über Leitung
Aus
dem Pumpenvorlagebehälter
D3 wird die kondensierte C2/C3-reiche
Fraktion über
Leitung
Alternativ
zu der anhand der
Das erfindungsgemäße Verfahren zum Abtrennen einer C2+-reichen Fraktion aus verflüssigtem Erdgas weiterbildend wird vorgeschlagen, dass die Abkühlung von Verfahrensströmen, die aus der Auftrennung T' der zweiten C2+-reichen Flüssigfraktion resultieren, gegen die erste C2+-reiche Flüssigfraktion und/oder gegen wenigstens eine Flüssigfraktion, die aus der rektifikatorischen Auftrennung unterhalb der Zuspeisung der ersten C2+-reichen Flüssigfraktion abgezogen wird, erfolgt.The inventive method for separating a fraction rich in C 2+ of liquefied natural gas, it is proposed that the cooling of process streams, that of the second C resulting from the separation of T '2+ -rich liquid fraction against the first calcareous C 2+ liquid fraction and / or against at least one liquid fraction which is withdrawn from the rectification separation below the feed of the first C 2+ -rich liquid fraction.
Insbesondere
dann, wenn die zweite C2+-reiche Flüssigfraktion
Der hierfür erforderliche Wärmetauscher kann beispielsweise zwischen der Pumpe P3 und der Trennkolonne T vorgesehen werden. Damit eine drucklose Lagerung realisiert werden kann, ist im Falle einer überwiegend aus Ethan bestehenden Gasfraktion, die am Kopf der rektifikatorischen C2/C3-Trennung T' gewonnen wird, eine Temperatur von etwa –100 °C erforderlich. Von Vorteil bei dieser Verfahrensführung ist, dass im gesamten Prozess auf Fremdkälte – also Kühlung unterhalb der Umgebungstemperatur – oder – thermodynamisch gleichwertig – Verdichtung verzichtet werden kann.The heat exchanger required for this purpose can be provided for example between the pump P3 and the separation column T. For a non-pressurized storage can be realized, in the case of a predominantly consisting of ethane gas fraction, which is recovered at the top of the rectifying C 2 / C 3 separation T ', a temperature of about -100 ° C is required. An advantage of this procedure is that in the entire process on external cold - ie cooling below the ambient temperature - or - thermodynamically equivalent - can be dispensed compression.
Wenn,
wie anhand der in den
Das erfindungsgemäße Verfahren zum Abtrennen einer C2+-reichen Fraktion aus verflüssigtem Erdgas (LNG) ermöglicht die Realisierung hoher Ethanausbeuten bei einem gleichzeitigen Verzicht auf kostenintensive Verdichter.The inventive method for separating a C 2+ -rich fraction from liquefied natural gas (LNG) allows the realization of high Ethanausbeuten while dispensing with expensive compressors.
Claims (9)
Priority Applications (10)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102005000634A DE102005000634A1 (en) | 2005-01-03 | 2005-01-03 | Process for separating a C2 + -rich fraction from LNG |
EP05823015.2A EP1834144B1 (en) | 2005-01-03 | 2005-12-21 | Method for separating a fraction rich in c2+ from liquefied natural gas |
PCT/EP2005/013748 WO2006072390A1 (en) | 2005-01-03 | 2005-12-21 | Method for separating a fraction rich in c2+ from liquefied natural gas |
US11/813,278 US20090211296A1 (en) | 2005-01-03 | 2005-12-21 | Method and apparatus for separating a fraction rich in c2+ from liquefied natural gas |
ES05823015.2T ES2665688T3 (en) | 2005-01-03 | 2005-12-21 | Procedure for the separation of a fraction rich in C2 + from LNG |
MX2007006584A MX2007006584A (en) | 2005-01-03 | 2005-12-21 | Method for separating a fraction rich in c2+ from liquefied natural gas. |
BRPI0518529-7A BRPI0518529B1 (en) | 2005-01-03 | 2005-12-21 | Process for Separation of a Rich C2 + LNG Fraction |
CN2005800458589A CN101095023B (en) | 2005-01-03 | 2005-12-21 | Method for separating a fraction rich in C2+ from liquefied natural gas |
JP2007548724A JP2008527287A (en) | 2005-01-03 | 2005-12-21 | Method for separating C2 + enriched fractions from liquefied natural gas |
KR1020077017075A KR101236863B1 (en) | 2005-01-03 | 2005-12-21 | Method for separating a fraction rich in c2+ from liquefied natural gas |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102005000634A DE102005000634A1 (en) | 2005-01-03 | 2005-01-03 | Process for separating a C2 + -rich fraction from LNG |
Publications (1)
Publication Number | Publication Date |
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DE102005000634A1 true DE102005000634A1 (en) | 2006-07-13 |
Family
ID=35911263
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
DE102005000634A Withdrawn DE102005000634A1 (en) | 2005-01-03 | 2005-01-03 | Process for separating a C2 + -rich fraction from LNG |
Country Status (10)
Country | Link |
---|---|
US (1) | US20090211296A1 (en) |
EP (1) | EP1834144B1 (en) |
JP (1) | JP2008527287A (en) |
KR (1) | KR101236863B1 (en) |
CN (1) | CN101095023B (en) |
BR (1) | BRPI0518529B1 (en) |
DE (1) | DE102005000634A1 (en) |
ES (1) | ES2665688T3 (en) |
MX (1) | MX2007006584A (en) |
WO (1) | WO2006072390A1 (en) |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
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US7603867B2 (en) * | 2006-09-11 | 2009-10-20 | Cryogenic Group, Inc. | Process and system to produce multiple distributable products from source, or imported LNG |
US20080190352A1 (en) | 2007-02-12 | 2008-08-14 | Daewoo Shipbuilding & Marine Engineering Co., Ltd. | Lng tank ship and operation thereof |
US7644676B2 (en) | 2008-02-11 | 2010-01-12 | Daewoo Shipbuilding & Marine Engineering Co., Ltd. | Storage tank containing liquefied natural gas with butane |
KR20090107805A (en) | 2008-04-10 | 2009-10-14 | 대우조선해양 주식회사 | Method and system for reducing heating value of natural gas |
JP5686989B2 (en) * | 2010-05-13 | 2015-03-18 | エア・ウォーター株式会社 | Production of liquefied natural gas for automobiles |
DE102012021637A1 (en) * | 2012-11-02 | 2014-05-08 | Linde Aktiengesellschaft | Process for cooling a hydrocarbon-rich fraction |
Family Cites Families (15)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR1501013A (en) | 1966-09-13 | 1967-11-10 | Air Liquide | Process for the production of a gas rich in methane under high pressure from liquid natural gas under low pressure |
US5114451A (en) * | 1990-03-12 | 1992-05-19 | Elcor Corporation | Liquefied natural gas processing |
US6116050A (en) * | 1998-12-04 | 2000-09-12 | Ipsi Llc | Propane recovery methods |
US6742358B2 (en) * | 2001-06-08 | 2004-06-01 | Elkcorp | Natural gas liquefaction |
FR2831656B1 (en) * | 2001-10-31 | 2004-04-30 | Technip Cie | METHOD AND PLANT FOR SEPARATING A GAS CONTAINING METHANE AND ETHANE WITH TWO COLUMNS OPERATING UNDER TWO DIFFERENT PRESSURES |
US6941771B2 (en) | 2002-04-03 | 2005-09-13 | Howe-Baker Engineers, Ltd. | Liquid natural gas processing |
US6564579B1 (en) * | 2002-05-13 | 2003-05-20 | Black & Veatch Pritchard Inc. | Method for vaporizing and recovery of natural gas liquids from liquefied natural gas |
US7051553B2 (en) * | 2002-05-20 | 2006-05-30 | Floor Technologies Corporation | Twin reflux process and configurations for improved natural gas liquids recovery |
US6907752B2 (en) * | 2003-07-07 | 2005-06-21 | Howe-Baker Engineers, Ltd. | Cryogenic liquid natural gas recovery process |
US7155931B2 (en) * | 2003-09-30 | 2007-01-02 | Ortloff Engineers, Ltd. | Liquefied natural gas processing |
US7278281B2 (en) * | 2003-11-13 | 2007-10-09 | Foster Wheeler Usa Corporation | Method and apparatus for reducing C2 and C3 at LNG receiving terminals |
KR101200611B1 (en) * | 2004-07-01 | 2012-11-12 | 오르트로프 엔지니어스, 리미티드 | Liquefied natural gas processing |
CN101027528B (en) * | 2004-09-14 | 2011-06-15 | 埃克森美孚上游研究公司 | Method of extracting ethane from liquefied natural gas |
WO2006066015A2 (en) * | 2004-12-16 | 2006-06-22 | Fluor Technologies Corporation | Configurations and methods for lng regasification and btu control |
CN101460800B (en) * | 2006-06-02 | 2012-07-18 | 奥特洛夫工程有限公司 | Liquefied natural gas processing |
-
2005
- 2005-01-03 DE DE102005000634A patent/DE102005000634A1/en not_active Withdrawn
- 2005-12-21 CN CN2005800458589A patent/CN101095023B/en active Active
- 2005-12-21 ES ES05823015.2T patent/ES2665688T3/en active Active
- 2005-12-21 BR BRPI0518529-7A patent/BRPI0518529B1/en not_active IP Right Cessation
- 2005-12-21 MX MX2007006584A patent/MX2007006584A/en active IP Right Grant
- 2005-12-21 WO PCT/EP2005/013748 patent/WO2006072390A1/en active Application Filing
- 2005-12-21 US US11/813,278 patent/US20090211296A1/en not_active Abandoned
- 2005-12-21 JP JP2007548724A patent/JP2008527287A/en active Pending
- 2005-12-21 KR KR1020077017075A patent/KR101236863B1/en active IP Right Grant
- 2005-12-21 EP EP05823015.2A patent/EP1834144B1/en active Active
Also Published As
Publication number | Publication date |
---|---|
ES2665688T3 (en) | 2018-04-26 |
BRPI0518529B1 (en) | 2018-06-26 |
JP2008527287A (en) | 2008-07-24 |
CN101095023A (en) | 2007-12-26 |
KR20070100760A (en) | 2007-10-11 |
BRPI0518529A2 (en) | 2008-11-25 |
WO2006072390A1 (en) | 2006-07-13 |
EP1834144B1 (en) | 2018-02-28 |
CN101095023B (en) | 2010-12-22 |
EP1834144A1 (en) | 2007-09-19 |
KR101236863B1 (en) | 2013-02-26 |
US20090211296A1 (en) | 2009-08-27 |
MX2007006584A (en) | 2007-07-13 |
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