DE102015009254A1 - Process for separating ethane from a hydrocarbon-rich gas fraction - Google Patents
Process for separating ethane from a hydrocarbon-rich gas fraction Download PDFInfo
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- DE102015009254A1 DE102015009254A1 DE102015009254.5A DE102015009254A DE102015009254A1 DE 102015009254 A1 DE102015009254 A1 DE 102015009254A1 DE 102015009254 A DE102015009254 A DE 102015009254A DE 102015009254 A1 DE102015009254 A1 DE 102015009254A1
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic 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
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead 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
- 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
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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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
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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
- F25J2270/02—Internal refrigeration with liquid vaporising loop
Abstract
Es wird ein Verfahren zum Abtrennen einer gasförmigen Ethan-reichen Produktfraktion (11') aus einer gasförmigen Kohlenwasserstoff-reichen Einsatzfraktion (1), vorzugsweise aus Erdgas, beschrieben, wobei
– die Einsatzfraktion (1) partiell kondensiert und in eine gasförmige (2, 3) und eine flüssige Fraktion (4) aufgetrennt wird (D1), und
– diese Fraktionen in einem Demethanizer (T1) und einem nachgeschalteten Deethanizer (T2) in eine Methan-reiche Gasfraktion (5) und eine gasförmige Ethan-reichen Produktfraktion (9, 11) aufgetrennt werden.
Erfindungsgemäß
– wird die Ethan-reiche Gasfraktion (9) gegen die Methan-reiche Gasfraktion (5') und wenigstens einen anzuwärmenden Seitenstrom (6) des Demethanizers (T1) partiell kondensiert (E1), der dabei anfallende Flüssiganteil wird dem Deethanizer (T2) als Rücklauf zugeführt (10) und der dabei anfallende Gasanteil (11) stellt die Ethan-reiche Produktfraktion dar, und
– die Einsatzfraktion (1) wird ausschließlich gegen die Ethan-reiche Produktfraktion (11), die Methan-reiche Gasfraktion (5') und wenigstens einen anzuwärmenden Seitenstrom (6) des Demethanizers (T1) partiell kondensiert (E1).A method is described for separating a gaseous ethane-rich product fraction (11 ') from a gaseous hydrocarbon-rich feed fraction (1), preferably from natural gas, wherein
- The feed fraction (1) is partially condensed and separated into a gaseous (2, 3) and a liquid fraction (4) (D1), and
- These fractions in a demethanizer (T1) and a downstream deethanizer (T2) in a methane-rich gas fraction (5) and a gaseous ethane-rich product fraction (9, 11) are separated.
According to the invention
- The ethane-rich gas fraction (9) against the methane-rich gas fraction (5 ') and at least one side stream to be heated (6) of the demethanizer (T1) is partially condensed (E1), the resulting liquid content is the deethanizer (T2) as Return fed (10) and the resulting gas fraction (11) represents the ethane-rich product fraction, and
- The feed fraction (1) is only against the ethane-rich product fraction (11), the methane-rich gas fraction (5 ') and at least one side stream to be heated (6) of the demethanizer (T1) partially condensed (E1).
Description
Die Erfindung betrifft ein Verfahren zum Abtrennen einer gasförmigen Ethan-reichen Produktfraktion aus einer gasförmigen Kohlenwasserstoff-reichen Einsatzfraktion, vorzugsweise aus Erdgas, wobei
- a) die Einsatzfraktion partiell kondensiert und in eine gasförmige und eine flüssige Fraktion aufgetrennt wird,
- b) die gasförmige und die flüssige Fraktion rektifikatorisch in eine Methan-reiche Gasfraktion und eine C2+-reiche Flüssigfraktion aufgetrennt werden (1. Abtrennstufe),
- c) wobei wenigstens 60 bis 90% der gasförmigen Fraktion auf den Druck der 1. Abtrennstufe entspanntund der restliche Anteil der gasförmigen Fraktion gegen die am Kopf der 1. Abtrennstufe abgezogene Methan-reiche Fraktion verflüssigt wird und wobei aus der 1. Abtrennstufe wenigstens ein Seitenstrom abgezogen, partiell verdampft und erneut der 1. Abtrennstufe zugeführt wird, und
- d) die C2+-reiche Flüssigfraktion rektifikatorisch in eine Ethan-reiche Gasfraktion und eine C3+-reiche Flüssigfraktion aufgetrennt wird (2. Abtrennstufe).
- a) the feed fraction is partially condensed and separated into a gaseous and a liquid fraction,
- b) the gaseous and liquid fractions are rectificatively separated into a methane-rich gas fraction and a C 2+ -rich liquid fraction (first separation stage),
- c) wherein at least 60 to 90% of the gaseous fraction is depressurized to the pressure of the first separation stage and the remaining portion of the gaseous fraction is liquefied against the withdrawn at the top of the 1st separation stage methane-rich fraction and wherein the 1st separation stage at least one side stream withdrawn, partially evaporated and again the 1st separation stage is supplied, and
- d) the C 2+ -rich liquid fraction is rectificially separated into an ethane-rich gas fraction and a C 3+ -rich liquid fraction (second separation step).
Konventionelles Erdgas besteht überwiegend aus Kohlenwasserstoffen. Nach Methan weist Ethan in der Regel die zweithöchste molare Konzentration auf. Die Gewinnung von technisch reinem Ethan aus Erdgas ist eine wichtige Technologie, um sog. Gascracker mit dem Einsatzstoff für die Ethylenproduktion zu versorgen. Unter dem Begriff ”technisch reines Ethan” sei eine Ethan-reiche Fraktion mit einer Ethan-Konzentration von > 95 Mol-%, vorzugsweise > 98 Mol-% zu verstehen. Die Gewinnung einer C2+Fraktion aus Erdgas erfolgt üblicherweise durch eine Kombination von partieller Kondensation und Rektifikation unter Einsatz von Wärmetauschernetzwerken. Da aus dem gasförmigen Erdgas ein flüssiges C2+-Produkt abgetrennt werden soll, muss die hierfür erforderliche Kälteleistung durch arbeitsleistende Entspannung und ggf. eine Kälteanlage bereitgestellt werden. Beispielhaft hierfür sei der sog. Gas-Subcooled-Prozess (GSP) angeführt, der in den
Derartige Trennverfahren führen den Schnitt zwischen Methan und leichteren Komponenten wie Stickstoff sowie Ethan und schwereren Komponenten wie Propan und höheren Kohlenwasserstoffen durch. Anders ausgedrückt wird das Einsatzgas durch einen Demethanizer in ein leichtes, Methan-reiches Verkaufsgas und eine flüssige C2+-Fraktion zerlegt. Die weitere Auftrennung der C2+-Fraktion in Fraktionen gewünschter Zusammensetzung erfolgt in einer Kette von dem Demethanizer nachgeschalteten Destillationskolonnen. Der erste Schritt ist in den meisten Fällen die Zerlegung des C2+-Zwischenproduktes in eine Ethan-reiche Fraktion und eine C3+-Fraktion mittels eines Deethanizers. Aufgrund der niedrigen kritischen Temperatur von Ethan – diese beträgt 32°C –, wird für den Kopfkondensator des Deethanizers in der Praxis eine Temperatur um den Gefrierpunkt gewählt, die im Allgemeinen nicht durch Kühlwasser oder Luft eingestellt werden kann. Daher ist hierfür eine Kälteversorgung, bspw. durch eine Propankälteanlage, erforderlich.Such separation processes perform the intersection between methane and lighter components such as nitrogen as well as ethane and heavier components such as propane and higher hydrocarbons. In other words, the feed gas is decomposed by a demethanizer into a light, methane-rich sales gas and a liquid C 2+ fraction. The further separation of the C 2+ fraction into fractions of desired composition takes place in a chain of distillation columns connected downstream of the demethanizer. The first step is in most cases the decomposition of the C 2+ intermediate into an ethane-rich fraction and a C 3+ fraction by means of a deethanizer. Due to the low critical temperature of ethane - this is 32 ° C -, the deethanizer top condenser is in practice chosen to have a freezing point temperature which generally can not be adjusted by cooling water or air. Therefore, this is a refrigeration, eg. By a propane refrigeration system required.
Aufgabe der vorliegenden Erfindung ist es, ein Verfahren zum Abtrennen einer gasförmigen Ethan-reichen Produktfraktion aus einer gasförmigen Kohlenwasserstoffreichen Einsatzfraktion mittels der beiden Kolonnen Demethanizer und Deethanizer anzugeben, das vollständig ohne geschlossene Kälteanlagen ausgeführt werden kann. Insbesondere sollen im Vergleich zu bekannten Verfahren die Invest- und Betriebskosten reduziert werden.The object of the present invention is to provide a process for separating a gaseous ethane-rich product fraction from a gaseous hydrocarbon-rich feed fraction by means of the two columns demethanizer and deethanizer, which can be carried out completely without closed refrigeration systems. In particular, the investment and operating costs should be reduced in comparison to known methods.
Zur Lösung dieser Aufgabe wird ein Verfahren zum Abtrennen einer gasförmigen Ethan-reichen Produktfraktion aus einer gasförmigen Kohlenwasserstoff-reichen Einsatzfraktion vorgeschlagen, das dadurch gekennzeichnet ist, dass
- e) die Ethan-reiche Gasfraktion gegen die Methan-reiche Gasfraktion und wenigstens einen anzuwärmenden Seitenstrom der 1. Abtrennstufe partiell kondensiert, der dabei anfallende Flüssiganteil der 2. Abtrennstufe als Rücklauf zugeführt wird und der dabei anfallende Gasanteil die Ethan-reiche Produktfraktion darstellt, und
- f) die Einsatzfraktion ausschließlich gegen die Ethan-reiche Produktfraktion, die Methan-reiche Gasfraktion und wenigstens einen anzuwärmenden Seitenstrom der 1. Abtrennstufe partiell kondensiert wird.
- e) partially condensing the ethane-rich gas fraction against the methane-rich gas fraction and at least one sidestream to be heated in the 1st separation stage, the resulting liquid fraction from the second separation stage being recycled as reflux and the resulting gas fraction representing the ethane-rich product fraction, and
- f) the feed fraction is only partially condensed against the ethane-rich product fraction, the methane-rich gas fraction and at least one Seitenstrom to be heated side of the 1st separation stage.
Hierbei werden die Verfahrensschritte e) und f) in vorteilhafter Weise in einem einzigen Mehrstromwärmetauscher realisiert.Here, the method steps e) and f) are realized in an advantageous manner in a single multi-flow heat exchanger.
Nachfolgend wird die 1. Abtrennstufe auch als Demethanizer und die 2. Abtrennstufe als Deethanizer bezeichnet.Hereinafter, the 1st separation stage is also referred to as a demethanizer and the 2nd separation stage as a deethanizer.
Gemäß der erfindungsgemäßen Verfahrensweise wird die aus der 2. Abtrennstufe abgezogene Ethan-reiche Gasfraktion im Gegensatz zum Stand der Technik nicht in einem Zweistromwärmetauscher gegen einen Seitenstrom der 1. Abtrennstufe vollständig kondensiert. Vielmehr wird erfindungsgemäß auf die Gewinnung eines flüssigen Ethanprodukts verzichtet und stattdessen ein gasförmiges Ethanprodukt abgezogen. Diese Verfahrensführung verringert die benötigte Kälteleistung erheblich. Die gemäß Verfahrensschritt e) (wahrscheinlich wollen Sie die Verwendung von a), b), usw. beibehalten, daher ändere ich jetzt nichts mehr) realisierte Teilkondensation der in der 2. Abtrennstufe gewonnenen Ethan-reichen Gasfraktion ist zudem in vorteilhafter Weise in einem Mehrstromwärmetauscher integriert, der zudem die partiell zu kondensierende Einsatzfraktion, die in der 1. Abtrennstufe gewonnene Methan-reiche Gasfraktion und wenigstens einen anzuwärmenden Seitenstrom der 1. Abtrennstufe in indirekten Wärmeaustausch bringt.According to the procedure of the invention, the ethane-rich gas fraction withdrawn from the second separation stage is not completely condensed in a two-flow heat exchanger against a side stream of the first separation stage, in contrast to the prior art. Rather, the invention dispenses with the recovery of a liquid ethane product and instead withdrawn a gaseous ethane product. This procedure significantly reduces the required cooling capacity. Which according to process step e) (you probably want the use of a), b), etc. maintained, so I do not change anymore) realized partial condensation of the ethane won in the 2nd separation step rich gas fraction is also advantageously integrated in a multi-flow heat exchanger, which also brings the partially to be condensed feed fraction, obtained in the 1st separation stage methane-rich gas fraction and at least one side stream to be heated of the 1st separation stage in indirect heat exchange.
Die Kombination der Verfahrensschritte a) bis d) – die den aus dem Stand der Technik bekannten Gas-Subcooled-Process widerspiegeln – mit den erfindungsgemäß vorzusehenden Verfahrensschritten e) und f) führt zu einem Verfahren zum Abtrennen einer gasförmigen Ethan-reichen Produktfraktion, das auf eine externe Kälteanlage verzichten kann. Hierdurch werden sowohl der Investitionsaufwand als auch die Komplexität des Verfahrens bzw. Anlagenbetriebs erheblich reduziert.The combination of process steps a) to d) -which reflect the gas-subcooled process known from the prior art-with the process steps e) and f) to be provided according to the invention leads to a process for separating a gaseous ethane-rich product fraction which has an external refrigeration system can do without. As a result, both the investment and the complexity of the process or plant operation are significantly reduced.
Weitere vorteilhafte Ausgestaltungen des erfindungsgemäßen Verfahrens zum Abtrennen einer gasförmigen Ethan-reichen Produktfraktion aus einer gasförmigen Kohlenwasserstoff-reichen Einsatzfraktion, die Gegenstände der abhängigen Patentansprüche darstellen, sind dadurch gekennzeichnet, dass
- – die partiell zu kondensierende Einsatzfraktion einen Druck zwischen 40 und 100 bar aufweist,
- – die 1. Abtrennstufe bei einem Druck zwischen 15 und 35 bar betrieben wird,
- – die 2. Abtrennstufe bei einem um 4 bis 12 bar, vorzugsweise um 6 bis 10 bar geringeren Druck als die 1. Abtrennstufe betrieben wird, und
- – die Entspannung der gasförmigen Fraktion arbeitsleistend erfolgt und zur Stromerzeugung in einem Generator und/oder zur Verdichtung der Methan-reichen Gasfraktion herangezogen wird.
- The feed fraction to be partially condensed has a pressure between 40 and 100 bar,
- The first separation stage is operated at a pressure between 15 and 35 bar,
- - The second separation stage is operated at a 4 to 12 bar, preferably 6 to 10 bar lower pressure than the first separation stage, and
- - The relaxation of the gaseous fraction is carried out to perform work and is used to generate electricity in a generator and / or for compression of the methane-rich gas fraction.
Das erfindungsgemäße Verfahren zum Abtrennen einer gasförmigen Ethan-reichen Produktfraktion aus einer gasförmigen Kohlenwasserstoff-reichen Einsatzfraktion sowie weitere vorteilhafte Ausgestaltungen desselben seien nachfolgend anhand des in der
Die Kohlenwasserstoff-reiche Einsatzfraktion
Der restliche Anteil
An geeigneter Stelle wird zudem aus dem Demethanizer T1 wenigstens ein Seitenstrom
Üblicherweise wird die 1. Abtrennstufe bzw. der Demethanizer T1 bei einem Druck zwischen 15 und 35 bar betrieben. In vorteilhafter Weise wird die noch zu erläuternde 2. Abtrennstufe bzw. der Deethanizer T2 bei einem um 4 bis 12 bar, vorzugsweise einem um 6 bis 10 bar geringeren Druck als der Demethanizer T1 betrieben.Usually, the first separation stage or the demethanizer T1 is operated at a pressure between 15 and 35 bar. Advantageously, the second separation stage or the deethanizer T2, which is still to be explained, is operated at a pressure lower by 4 to 12 bar, preferably by 6 to 10 bar, than the demethanizer T1.
Aus dem Sumpf des Demethanizers T1 wird eine C2+-reiche Flüssigfraktion
Die am Kopf des Deethanizers T2 abgezogene Ethan-reiche Gasfraktion
ZITATE ENTHALTEN IN DER BESCHREIBUNG QUOTES INCLUDE IN THE DESCRIPTION
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Zitierte PatentliteraturCited patent literature
- US 4157904 [0002] US 4157904 [0002]
- US 4278457 [0002] US 4278457 [0002]
Claims (6)
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
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DE102015009254.5A DE102015009254A1 (en) | 2015-07-16 | 2015-07-16 | Process for separating ethane from a hydrocarbon-rich gas fraction |
RU2015136852A RU2689866C2 (en) | 2015-07-16 | 2015-08-28 | Method of extracting ethane from a gas fraction with high content of hydrocarbons |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
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DE102015009254.5A DE102015009254A1 (en) | 2015-07-16 | 2015-07-16 | Process for separating ethane from a hydrocarbon-rich gas fraction |
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DE102015009254A1 true DE102015009254A1 (en) | 2017-01-19 |
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DE102015009254.5A Withdrawn DE102015009254A1 (en) | 2015-07-16 | 2015-07-16 | Process for separating ethane from a hydrocarbon-rich gas fraction |
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DE (1) | DE102015009254A1 (en) |
RU (1) | RU2689866C2 (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102016003305A1 (en) | 2016-03-17 | 2017-09-21 | Linde Aktiengesellschaft | Process for separating an ethane-rich fraction from natural gas |
Citations (9)
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US4157904A (en) | 1976-08-09 | 1979-06-12 | The Ortloff Corporation | Hydrocarbon gas processing |
US4278457A (en) | 1977-07-14 | 1981-07-14 | Ortloff Corporation | Hydrocarbon gas processing |
US6116050A (en) * | 1998-12-04 | 2000-09-12 | Ipsi Llc | Propane recovery methods |
DE10140584A1 (en) * | 2001-08-18 | 2003-02-27 | Linde Ag | Separation of lower hydrocarbons comprises use of de-methanizer and de-ethanizer, employing one or more defined strategies |
DE10140585A1 (en) * | 2001-08-18 | 2003-02-27 | Linde Ag | Separation of lower hydrocarbons comprises operating de-ethanizer at no less than de-methanizer pressure and combines head fractions for at least an interval |
WO2006066015A2 (en) * | 2004-12-16 | 2006-06-22 | Fluor Technologies Corporation | Configurations and methods for lng regasification and btu control |
US20100011810A1 (en) * | 2005-07-07 | 2010-01-21 | Fluor Technologies Corporation | NGL Recovery Methods and Configurations |
WO2012087740A1 (en) * | 2010-12-23 | 2012-06-28 | Fluor Technologies Corporation | Ethane recovery and ethane rejection methods and configurations |
US20130061633A1 (en) * | 2005-07-07 | 2013-03-14 | Fluor Technologies Corporation | Configurations and methods of integrated ngl recovery and lng liquefaction |
Family Cites Families (4)
Publication number | Priority date | Publication date | Assignee | Title |
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US6743829B2 (en) * | 2002-01-18 | 2004-06-01 | Bp Corporation North America Inc. | Integrated processing of natural gas into liquid products |
US7475566B2 (en) * | 2002-04-03 | 2009-01-13 | Howe-Barker Engineers, Ltd. | Liquid natural gas processing |
AU2007235921B2 (en) * | 2006-04-12 | 2010-05-27 | Shell Internationale Research Maatschappij B.V. | Method and apparatus for liquefying a natural gas stream |
DE102007010874A1 (en) * | 2007-03-06 | 2008-09-11 | Linde Ag | separation |
-
2015
- 2015-07-16 DE DE102015009254.5A patent/DE102015009254A1/en not_active Withdrawn
- 2015-08-28 RU RU2015136852A patent/RU2689866C2/en active
Patent Citations (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4157904A (en) | 1976-08-09 | 1979-06-12 | The Ortloff Corporation | Hydrocarbon gas processing |
US4278457A (en) | 1977-07-14 | 1981-07-14 | Ortloff Corporation | Hydrocarbon gas processing |
US6116050A (en) * | 1998-12-04 | 2000-09-12 | Ipsi Llc | Propane recovery methods |
DE10140584A1 (en) * | 2001-08-18 | 2003-02-27 | Linde Ag | Separation of lower hydrocarbons comprises use of de-methanizer and de-ethanizer, employing one or more defined strategies |
DE10140585A1 (en) * | 2001-08-18 | 2003-02-27 | Linde Ag | Separation of lower hydrocarbons comprises operating de-ethanizer at no less than de-methanizer pressure and combines head fractions for at least an interval |
WO2006066015A2 (en) * | 2004-12-16 | 2006-06-22 | Fluor Technologies Corporation | Configurations and methods for lng regasification and btu control |
US20090277219A1 (en) * | 2004-12-16 | 2009-11-12 | Fluor Technologies Corporation | Configurations and Methods for Offshore LNG Regasification and BTU Control |
US20100011810A1 (en) * | 2005-07-07 | 2010-01-21 | Fluor Technologies Corporation | NGL Recovery Methods and Configurations |
US20130061633A1 (en) * | 2005-07-07 | 2013-03-14 | Fluor Technologies Corporation | Configurations and methods of integrated ngl recovery and lng liquefaction |
WO2012087740A1 (en) * | 2010-12-23 | 2012-06-28 | Fluor Technologies Corporation | Ethane recovery and ethane rejection methods and configurations |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102016003305A1 (en) | 2016-03-17 | 2017-09-21 | Linde Aktiengesellschaft | Process for separating an ethane-rich fraction from natural gas |
Also Published As
Publication number | Publication date |
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RU2015136852A3 (en) | 2018-10-26 |
RU2689866C2 (en) | 2019-05-29 |
RU2015136852A (en) | 2017-03-06 |
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