DE10027903A1 - Recovery of a C2+ fraction from a hydrocarbon feed, especially natural gas, comprises fractionation in a column with a C3+ reflux stream - Google Patents
Recovery of a C2+ fraction from a hydrocarbon feed, especially natural gas, comprises fractionation in a column with a C3+ reflux streamInfo
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- DE10027903A1 DE10027903A1 DE10027903A DE10027903A DE10027903A1 DE 10027903 A1 DE10027903 A1 DE 10027903A1 DE 10027903 A DE10027903 A DE 10027903A DE 10027903 A DE10027903 A DE 10027903A DE 10027903 A1 DE10027903 A1 DE 10027903A1
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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
- F25J3/0204—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
- F25J3/0242—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
- F25J2200/74—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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator 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
- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
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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
- 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
- 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
- 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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- 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
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
Abstract
Description
Die Erfindung betrifft ein Verfahren zum Gewinnen einer C2+-reichen Fraktion, indem eine Kohlenwasserstoff-reiche Fraktion, insbesondere Erdgas, abgekühlt und zumindest teilweise verflüssigt und in wenigstens einer Kolonne, insbesondere einer Rektifizierkolonne, in wenigstens eine C1-reiche Fraktion und in wenigstens eine C2+-reiche Fraktion aufgetrennt wird, wobei der Kolonne am Kopf ein Rücklauf aufgegeben wird.The invention relates to a process for recovering a C 2+ -rich fraction by cooling and at least partially liquefying a hydrocarbon-rich fraction, in particular natural gas, and in at least one column, in particular a rectification column, in at least one C 1 -rich fraction and in at least one C 2+ -rich fraction is separated, the column being fed a reflux at the top.
Gattungsgemäße Verfahren zum Gewinnen einer C2+-reichen Fraktion sind beispielsweise aus der US 4,889,545 sowie der US 5,568,737 bekannt. Bei den darin beschriebenen Verfahren wird der Kolonne, in der die Auftrennung in eine C1-reiche Fraktion und eine C2+-reiche Fraktion erfolgt, am Kopf ein Teilstrom der aus ihr abgezogenen C1-reichen Fraktion zugeführt. Dieser Teilstrom der C1-reichen Fraktion dient somit als Waschmittel für die C2+-Komponenten, die im Sumpf der Kolonne gewonnen werden. Nachteilig bei diesen Verfahren ist jedoch, dass sie vergleichsweise hohe Salesgasverdichterleistungen erfordern.Generic methods for obtaining a C 2+ -rich fraction are known for example from US Pat. No. 4,889,545 and US Pat. No. 5,568,737. In the processes described therein, the column in which the separation into a C 1 -rich fraction and a C 2+ -rich fraction takes place is fed at the top of a partial stream of the C 1 -rich fraction withdrawn from it. This partial stream of the C 1 -rich fraction thus serves as a detergent for the C 2+ components which are obtained in the bottom of the column. However, a disadvantage of these processes is that they require comparatively high sales gas compressor outputs.
Aufgabe der vorliegenden Erfindung ist es, ein gattungsgemäßes Verfahren zum Gewinnen einer C2+-reichen Fraktion anzugeben, das - bei einer gleichbleibend hohen Ausbeute an C2+-Komponenten - eine Verringerung der Salesgasverdichterleistung ermöglicht.The object of the present invention is to provide a generic method for obtaining a C 2+ -rich fraction which - with a consistently high yield of C 2+ components - enables a reduction in the sales gas compressor capacity.
Zur Lösung dieser Aufgabe wird ein Verfahren zum Gewinnen einer C2+-reichen Fraktion vorgeschlagen, das dadurch gekennzeichnet, dass als Rücklauf eine C3+-reiche Fraktion, eine C3/C4-reiche Fraktion oder eine C3/C4/C5-reiche Fraktion als Rücklauf aufgegeben wird.To achieve this object, a process for obtaining a C 2+ -rich fraction is proposed, which is characterized in that a C 3+ -rich fraction, a C 3 / C 4 -rich fraction or a C 3 / C 4 / C 5 -rich fraction is given as reflux.
Im Gegensatz zu den bekannten Verfahren wird nunmehr nicht ein Teilstrom der C1-reichen Salesgasfraktion, sondern eine Fraktion, bestehend aus C3+-, C3/C4- oder C3/C4/C5-Komponenten als Rücklauf auf die Kolonne aufgegeben. Diese Verfahrensweise hat zur Folge, dass bei einer gleichbleibend hohen Ausbeute an C2+-Komponenten - das Auswaschen dieser Komponenten lässt sich mit einem Waschmittel der vorgenannten Zusammensetzung ebenso gut realisieren - eine Verringerung der Salesgasverdichterleistung erreicht werden kann.In contrast to the known methods, a partial stream of the C 1 -rich sales gas fraction is now used, but rather a fraction consisting of C 3+ , C 3 / C 4 or C 3 / C 4 / C 5 components as a return to the Column abandoned. The consequence of this procedure is that with a consistently high yield of C 2+ components - these components can also be washed out with a detergent of the abovementioned composition - a reduction in the sales gas compressor output can be achieved.
Die auf die Kolonne aufzugebende Rücklauffraktion wird dieser vorzugsweise an deren höchsten Punkt zugeführt.The reflux fraction to be added to the column is preferably at the other highest point fed.
Die Erzeugung einer Rücklauffraktion mit den vorgenannten Zusammensetzungen erfolgt - entsprechend einer vorteilhaften Ausgestaltung des erfindungsgemäßen Verfahrens - in einer der Kolonne, in der die Auftrennung in eine C1-reiche Fraktion und eine C2+-reiche Fraktion erfolgt, nachgeschalteten Kolonne. Bei dieser handelt es sich vorzugsweise um einen sog. Deethanizer, einen sog. Depropanizer oder einen sog. Debutanizer.In accordance with an advantageous embodiment of the process according to the invention, a reflux fraction with the abovementioned compositions is generated in a column downstream of the column in which the separation into a C 1 -rich fraction and a C 2+ -rich fraction takes place. This is preferably a so-called deethanizer, a so-called depropanizer or a so-called debutanizer.
Hierbei kann die Rücklauffraktion aus der der ersten Kolonne nachgeschalteten Kolonne in flüssiger und/oder gasförmiger Form abgezogen werden. Sofern ein Abzug in gasförmiger Form erfolgt, ist es zweckmäßig, die Rücklauffraktion vor der Zurückführung zu verflüssigen.The reflux fraction from that downstream of the first column can be used here Column are withdrawn in liquid and / or gaseous form. Provided a deduction done in gaseous form, it is appropriate to the reflux fraction before Liquefy return.
Eine Zuführung in die erste Kolonne in flüssiger, unterkühlter Form ist zweckmäßiger, da dadurch eine Verbesserung der Waschmittelleistung erreicht wird.A feed into the first column in liquid, supercooled form is more expedient as this will improve detergent performance.
Das erfindungsgemäße Verfahren zum Gewinnen einer C2+-reichen Fraktion sowie weitere Ausgestaltungen desselben seien anhand der in den Fig. 1 und 2 dargestellten Ausführungsbeispiele näher erläutert. Hierbei besitzen identische Anlagenteile gleiche Bezugszeichen.The method according to the invention for obtaining a C 2+ -rich fraction and further refinements thereof are explained in more detail with reference to the exemplary embodiments shown in FIGS . 1 and 2. Identical system parts have the same reference symbols.
Über Leitung 1 wird eine Kohlenwasserstoff-reiche Fraktion, beispielsweise ein Erdgasstrom, einem ersten Wärmetauscher E1 zugeführt und in ihm gegen anzuwärmende Verfahrensströme sowie gegen einen oder mehrerer Kältekreisläufe - in der Figur dargestellt durch den Strom x - abgekühlt. Anschließend wird die abgekühlte Kohlenwasserstoff-reiche Fraktion über Leitung 1' einem zweiten Wärmetauscher E2 zugeführt und in diesem gegen anzuwärmende Verfahrensströme sowie weitere Kältemittelkreisläufe y und z abgekühlt und teilweise kondensiert. Die teilkondensierte Kohlenwasserstoff-reiche Fraktion wird sodann über Leitung 1" dem Abscheider D1 zugeführt. A hydrocarbon-rich fraction, for example a natural gas stream, is fed via line 1 to a first heat exchanger E1 and is cooled in it against process streams to be heated and against one or more refrigeration circuits - represented by stream x in the figure. The cooled hydrocarbon-rich fraction is then fed via line 1 'to a second heat exchanger E2, in which it is cooled against process streams to be heated and further refrigerant circuits y and z and partially condensed. The partially condensed hydrocarbon-rich fraction is then fed via line 1 "to the separator D1.
Aus dem Sumpf des Abscheider D1 wird über Leitung 2 eine C2+-reiche Fraktion abgezogen, im Wärmetauscher E2 weiter abgekühlt und anschließend über Leitung 2" einem Entspannungsventil a zugeführt und über dieses in die erste Kolonne K1 entspannt.A C 2+ -rich fraction is drawn off from the bottom of the separator D1 via line 2 , cooled further in the heat exchanger E2 and then fed via line 2 "to a relief valve a and expanded into the first column K1 via this.
Die am Kopf des Abscheiders D1 anfallende gasförmige C1-reiche Fraktion wird über Leitung 3 abgezogen, einer Entspannungsturbine T zugeführt und in dieser arbeitsleistend entspannt und dabei abgekühlt. Diese Fraktion wird anschließend über Leitung 3' ebenfalls in die erste Kolonne K1 entspannt. Der Zuspeisepunkt dieser Fraktion liegt hierbei unterhalb des Zuspeisepunktes der aus dem Sumpf des Abscheiders D1 abgezogenen Fraktion.The gaseous C 1 -rich fraction obtained at the head of the separator D1 is withdrawn via line 3 , fed to an expansion turbine T and expanded in a work-performing manner and cooled in the process. This fraction is then also expanded via line 3 'into the first column K1. The feed point of this fraction is below the feed point of the fraction drawn off from the bottom of the separator D1.
Oberhalb der Zuspeisungspunkte der Leitungen 2' und 3' wird eine Rücklauffraktion - auf die im Folgenden noch näher eingegangen werden wird - der Kolonne K1 über die Leitung 11' und das Entspannungsventil b zugeführt.Above the feed points of lines 2 'and 3 ', a reflux fraction - which will be discussed in more detail below - is fed to column K1 via line 11 'and expansion valve b.
Die Kolonne K1 weist Böden, Packungen oder Kombinationen aus den beiden Vorgenannten auf. Diese sind jedoch der Übersichtlichkeit halber in den Fig. 1 und 2 nicht dargestellt; nicht dargestellt sind ferner mögliche Seitenabzüge und Rückführleitungen, die der Erhöhung der Effizienz der Kolonne K1 dienen.The column K1 has trays, packings or combinations of the two aforementioned. For the sake of clarity, however, these are not shown in FIGS. 1 and 2; possible side draws and return lines, which serve to increase the efficiency of column K1, are also not shown.
Am Kopf der Kolonne K1 wird über Leitung 4 die C1-reiche (Salesgas)Fraktion abgezogen, in den Wärmetauschern E2 und E1 gegen abzukühlende Verfahrensströme angewärmt und anschließend über Leitung 4' einem ersten Verdichter V1 zugeführt. Eine Verdichtung der C1-reichen Salesgasfraktion ist erforderlich, da das Salesgas meist über Pipelines zu den Verbrauchern über große Distanzen transportiert wird.At the top of the column K1 the C 1 calcareous (Sales gas) fraction is withdrawn via line 4, warmed in the heat exchangers E1 and E2 against process streams to be cooled and then fed via line 4 'a first compressor V1. Compression of the C 1 -rich sales gas fraction is necessary because the sales gas is mostly transported to consumers over long distances via pipelines.
Der Verdichter V1 ist dabei so ausgelegt, dass er durch die bereits erwähnte Entspannungsturbine T angetrieben wird. Dem ersten Verdichter V1 ist wenigstens ein weiterer Verdichter V2 nachgeschaltet, in dem die Salesgasfraktion auf den gewünschten Abgabedruck - beispielsweise 50 bis 200 bar - verdichtet wird, bevor sie über Leitung 4" ihrem weiteren Verwendungszweck zugeführt wird. The compressor V1 is designed so that it is driven by the expansion turbine T already mentioned. At least one further compressor V2 is connected downstream of the first compressor V1, in which the sales gas fraction is compressed to the desired delivery pressure - for example 50 to 200 bar - before it is fed to line 4 ″ for its further use.
Aus dem Sumpf der Kolonne K1 wird über Leitung 5 eine C2+-reiche Flüssigfraktion abgezogen und über Ventil c in eine zweite, der ersten Kolonne K1 nachgeschalteten Kolonne K2 zugeführt. Diese ist im Falle der in den Fig. 1 und 2 dargestellten Ausführungsbeispiele als ein Deethanizer ausgelegt.A C 2+ -rich liquid fraction is drawn off from the bottom of column K1 via line 5 and fed via valve c into a second column K2 which is connected downstream of the first column K1. In the case of the exemplary embodiments shown in FIGS . 1 and 2, this is designed as a deethanizer.
Aus dem Sumpf der Kolonne K2 wird über Leitung 9 eine C3+-reiche Flüssigfraktion abgezogen. Ein Teilstrom dieser Flüssigfraktion wird nach einer Verdampfung im Wärmetauscher E4 über Leitung 10 der Kolonne K2 wiederum zugeführt.A C 3+ -rich liquid fraction is drawn off from the bottom of column K2 via line 9 . After evaporation in the heat exchanger E4, a partial stream of this liquid fraction is again fed to the column K2 via line 10 .
Am Kopf der Kolonne K2 wird über Leitung 6 eine C2-Fraktion abgezogen, im Wärmetauscher E3 gegen einen Kältemittelstrom v partiell kondensiert und einem Abscheider D2 zugeführt. Über Leitung 8 wird aus dem Abscheider D2 eine als Rücklauf für die Kolonne K2 dienende Flüssigfraktion entnommen, mittels der Pumpe P1 auf den Druck der Kolonne K2 gepumpt und über das Regelventil d der Kolonne K2 zugeführt.At the top of the column K2, a C 2 fraction is drawn off via line 6 , partially condensed in the heat exchanger E3 against a refrigerant stream v and fed to a separator D2. Via line 8 , a liquid fraction serving as reflux for the column K2 is withdrawn from the separator D2, pumped to the pressure of the column K2 by means of the pump P1 and fed to the column K2 via the control valve d.
Am Kopf des Abscheiders D2 kann bei dieser Ausführungsform eine C2-Fraktion gewonnen und gegebenenfalls einer weiteren Behandlung zugeführt werden.In this embodiment, a C 2 fraction can be obtained at the top of the separator D2 and, if appropriate, fed to a further treatment.
Im mittleren Bereich der Kolonne K2 - in der Figur dargestellt durch einen Boden - wird über Leitung 11 eine C3+-reiche Fraktion abgezogen und mittels der Pumpe P2 auf einen Druck gepumpt, der eine Zuführung dieser Fraktion in die Kolonne K1 ermöglicht. Der aus der Kolonne K2 über die Leitung 11 abgezogenen Fraktion kann ein Teilstrom der aus dem Sumpf der Kolonne K2 abgezogenen Flüssigfraktion beigemischt werden - dargestellt durch die gestrichelt gezeichnete Leitung 12.In the middle of the column K2 - represented by a tray in the figure - a C 3+ -rich fraction is drawn off via line 11 and pumped to a pressure by means of the pump P2 which enables this fraction to be fed into the column K1. The fraction withdrawn from column K2 via line 11 can be admixed with a partial stream of the liquid fraction withdrawn from the bottom of column K2 - represented by line 12 shown in broken lines.
Die Rücklauffraktion in der Leitung 11 wird in den Wärmetauschern E1 und E2 gegen anzuwärmende Verfahrensströme sowie gegen die bereits erwähnten Kältemittelströme x, y und z unterkühlt und anschließend über Leitung 11' einem Entspannungsventil b zugeführt und über dieses in die Kolonne K1 entspannt.The return fraction in line 11 is subcooled in heat exchangers E1 and E2 against process streams to be heated and against the previously mentioned refrigerant streams x, y and z and then fed via line 11 'to an expansion valve b and expanded via this into column K1.
Bei der in der Fig. 2 dargestellten Ausführungsform des erfindungsgemäßen Verfahrens wird die aus der Kolonne K2 abzuziehende Rücklauffraktion gasförmig über die Leitung 13 aus der Kolonne K2 abgezogen. Sie wird dann zunächst in einem Wärmetauscher E5 gegen ein entsprechendes Kältemittel verflüssigt. Mittels der Pumpe P2 wird sie auf einen Druck gepumpt, der eine Zuführung in die erste Kolonne K1 ermöglicht. In den Wärmetauschern E1 und E2 erfolgt ein Abkühlen gegen anzuwärmende Verfahrensströme sowie gegen die Kältemittelströme x, y und z, bevor die Rücklauffraktion über die Leitung 13' und das Entspannungsventil b auf den Kopf der Kolonne K1 aufgegeben wird.In the embodiment of the process according to the invention shown in FIG. 2, the reflux fraction to be withdrawn from column K2 is withdrawn in gaseous form from column K2 via line 13 . It is then first liquefied in a heat exchanger E5 against an appropriate refrigerant. By means of the pump P2, it is pumped to a pressure which enables it to be fed into the first column K1. In the heat exchangers E1 and E2, cooling takes place against process streams to be heated and against the refrigerant streams x, y and z, before the return fraction is fed via line 13 'and the expansion valve b to the top of column K1.
Für welche der beiden, in den Fig. 1 und 2 dargestellten Varianten sich der Fachmann entscheidet, hängt im Wesentlichen davon ab, ob sich in der C3+-Fraktion Komponenten befinden, die ggf. im sog. kalten Teil des Prozesses ausfrieren können. Das erfindungsgemäße Verfahren zum Gewinnen einer C2+-reichen Fraktion ermöglicht bei einer gleichbleibend hohen Ausbeute an C2+-Komponenten, eine deutliche Verringerung der für die Verdichtung des Salesgases erforderlichen Leistung.Which of the two variants shown in FIGS. 1 and 2 the person skilled in the art essentially depends on whether there are components in the C 3+ fraction which may freeze out in the so-called cold part of the process. The method according to the invention for obtaining a C 2+ -rich fraction enables, with a consistently high yield of C 2+ components, a significant reduction in the power required for the compression of the sales gas.
Claims (11)
Priority Applications (1)
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DE10027903A DE10027903A1 (en) | 2000-06-06 | 2000-06-06 | Recovery of a C2+ fraction from a hydrocarbon feed, especially natural gas, comprises fractionation in a column with a C3+ reflux stream |
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DE10027903A DE10027903A1 (en) | 2000-06-06 | 2000-06-06 | Recovery of a C2+ fraction from a hydrocarbon feed, especially natural gas, comprises fractionation in a column with a C3+ reflux stream |
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Cited By (6)
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DE10205366A1 (en) * | 2002-02-08 | 2003-08-21 | Linde Ag | Liquefaction of hydrocarbon stream, such as natural gas, with simultaneous recovery of liquid natural gas fraction comprises rectification and absorption process |
DE10221230A1 (en) * | 2002-05-13 | 2003-12-04 | Linde Ag | Removal of hydrocarbons from natural gas prior to liquefaction has washer releasing fraction containing hydrocarbons for liquefaction |
WO2004010064A1 (en) * | 2002-07-23 | 2004-01-29 | Linde Aktiengesellschaft | Method for liquefying a hydrocarbon-rich flow while simultaneously obtaining a c3/c4-rich fraction |
EP2597408A1 (en) * | 2011-11-23 | 2013-05-29 | Shell Internationale Research Maatschappij B.V. | Method and apparatus for preparing a lean methane-containing gas stream |
NO339384B1 (en) * | 2003-04-16 | 2016-12-05 | Air Prod & Chem | INTEGRATED HIGH PRESSURE NGL RECOVERY IN THE PREPARATION OF LIQUID NATURAL GAS |
WO2020244639A1 (en) * | 2019-06-06 | 2020-12-10 | 中国石化工程建设有限公司 | Oil and gas processing method and device |
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DE10205366A1 (en) * | 2002-02-08 | 2003-08-21 | Linde Ag | Liquefaction of hydrocarbon stream, such as natural gas, with simultaneous recovery of liquid natural gas fraction comprises rectification and absorption process |
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NO339384B1 (en) * | 2003-04-16 | 2016-12-05 | Air Prod & Chem | INTEGRATED HIGH PRESSURE NGL RECOVERY IN THE PREPARATION OF LIQUID NATURAL GAS |
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