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DE10140585A1 - Separation of lower hydrocarbons comprises operating de-ethanizer at no less than de-methanizer pressure and combines head fractions for at least an interval - Google Patents

Separation of lower hydrocarbons comprises operating de-ethanizer at no less than de-methanizer pressure and combines head fractions for at least an interval

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Publication number
DE10140585A1
DE10140585A1 DE2001140585 DE10140585A DE10140585A1 DE 10140585 A1 DE10140585 A1 DE 10140585A1 DE 2001140585 DE2001140585 DE 2001140585 DE 10140585 A DE10140585 A DE 10140585A DE 10140585 A1 DE10140585 A1 DE 10140585A1
Authority
DE
Germany
Prior art keywords
rich fraction
demethanizer
deethanizer
ethanizer
temperature
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
DE2001140585
Other languages
German (de)
Inventor
Hans Schmidt
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to DE2001140585 priority Critical patent/DE10140585A1/en
Priority to NO20023888A priority patent/NO20023888L/en
Publication of DE10140585A1 publication Critical patent/DE10140585A1/en
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
    • C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G7/00—Distillation of hydrocarbon oils
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
    • C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
    • C10G70/041—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes by distillation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
    • C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
    • C10G70/043—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes by fractional condensation
    • 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
    • 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
    • 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
    • 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
    • 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
    • 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
    • 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
    • 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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/60—Integration in an installation using hydrocarbons, e.g. for fuel purposes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/20—Control for stopping, deriming or defrosting after an emergency shut-down of the installation or for back up system
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/12—Particular process parameters like pressure, temperature, ratios

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

A de-ethanizer (E) is operated at the same, or a higher pressure than the de-methanizer (M). At least some of the 2C-rich fraction (9) withdrawn at the head of the de-ethanizer is supplied for at least an interval to the 1C-rich fraction (11, 11') withdrawn at the head of the de-methanizer. Preferred Features: The fluid fraction (5) withdrawn from the sump of the de-methanizer, which is supplied to the de-ethanizer, is made available at least at a pressure permitting admixture of the head product (8, 9) of the de-ethanizer to the head product (11, 11') of the de-methanizer, without an additional compression of the former. For an interval , especially when recovered 2C-rich fraction is not extracted, one or more of the following measures is adopted. The temperature of the recycle stream (2, 3''') supplied to the demethanizer (M) is increased by up to 20 K, preferably by 10-15 K. The quantity of this recycle is reduced, or supply is interrupted. The temperature of the hydrocarbon-rich fraction (3''') fed to expansion (T) is increased by up to 20 K, preferably by 10-15 K. The sump temperature of the demethanizer (M) is increased by up to 15 K, preferably by 5-10 K (measures end). Should several of these measures be adopted, they are carried out simultaneously or at least overlap for an interval. Temperature and/or temperature conditions in the de-methanizer remain unaltered, whilst the pressure in the de-ethanizer is left constant or raised. Supply of 2C-rich fraction (9) withdrawn at the head of the de-ethanizer to the 1C-rich fraction (11, 11') withdrawn at the head of the demethanizer is effected before and/or after possible compression of the C-rich fraction

Description

Die Erfindung betrifft ein Verfahren zum Abtrennen einer C2-reichen Fraktion aus einer Kohlenwasserstoff-reichen Fraktion mit gleichzeitiger C3+-, C4+- und/oder C5+- Gewinnung, wobei die Kohlenwasserstoff-reiche Fraktion entspannt, mehrstufig partiell kondensiert und in wenigstens einem Demethanizer und wenigstens einem Deethanizer aufgetrennt wird. The invention relates to a process for separating a C 2 -rich fraction from a hydrocarbon-rich fraction with simultaneous C 3+ , C 4+ and / or C 5+ recovery, the hydrocarbon-rich fraction being relaxed, partially condensed in several stages and is separated in at least one demethanizer and at least one deethanizer.

Kommt es bei gattungsgemäßen Verfahren zum Abtrennen einer C2-reichen Fraktion zu einer Unterbrechung der Abnahme dieser C2-reichen Fraktion aus dem Prozess, kann der Betrieb der gleichzeitigen C3+-, C4+- und/oder C5+-Gewinnung nur dadurch aufrecht erhalten werden, indem die C2-reiche Fraktion wenigstens zu einem großen Teil abgefackelt und damit ungenutzt vernichtet wird. If there is an interruption in the removal of this C 2 -rich fraction from the process in the generic method for separating a C 2 -rich fraction, the operation of the simultaneous C 3+ , C 4+ and / or C 5+ recovery can be carried out can only be maintained by flaring at least a large part of the C 2 -rich fraction and thus destroying it unused.

Diese Situation tritt besonders häufig während der Inbetriebnahme von neuen Anlagen auf. Derartige Anlagen werden oftmals im Wesentlichen durch die vorgenannten höherwertigen C3+-, C4+- sowie C5+-Produkte amortisiert. Diese, als Flüssigkeiten anfallenden Produktströme können im Gegensatz zu der abgetrennten C2-reichen Fraktion kostengünstig in atmosphärischen gekühlten Tanks (zwischen)gelagert werden. This situation occurs particularly often during the commissioning of new plants. Such systems are often essentially amortized by the aforementioned higher-quality C 3+ , C 4+ and C 5+ products. In contrast to the separated C 2 -rich fraction, these product streams, which are produced as liquids, can be stored (temporarily) inexpensively in atmospheric cooled tanks.

Kommt es daher zu einer Unterbrechung der Abnahme der gewonnenen C2-reichen Fraktion und soll gleichzeitig die Produktion bzw. Gewinnung der C3+- Kohlenwasserstoffe aufrecht erhalten werden, so muss die C2-reiche Fraktion - wie beschrieben - abgefackelt und damit vernichtet werden. Dies bedeutet zum einen einen Wertstoffverlust und stellt zum anderen eine Schädigung der Umwelt dar. If there is therefore an interruption in the decrease in the C 2 -rich fraction obtained and at the same time production or recovery of the C 3+ hydrocarbons is to be maintained, the C 2 -rich fraction must be flared - as described - and thus destroyed , On the one hand, this means a loss of valuable materials and, on the other hand, it damages the environment.

Prinzipiell wäre es zwar möglich, derartige gattungsgemäße Verfahren auch für die alleinige Gewinnung einer C3+-reichen Fraktion auszulegen, jedoch erfordert dies ein grundlegend geändertes Anlagendesign, woraus wiederum erhebliche Mehrkosten resultieren würden. In principle, it would be possible to design such generic methods for the sole extraction of a C 3+ -rich fraction, but this requires a fundamentally changed plant design, which would in turn result in considerable additional costs.

Aufgabe der vorliegenden Erfindung ist es, ein gattungsgemäßes Verfahren zum Abtrennen einer C2-reichen Fraktion aus einer Kohlenwasserstoff-reichen Fraktion mit gleichzeitiger C3+-, C4+- und/oder C5+-Gewinnung anzugeben, das auch bei der Unterbrechung der Abnahme der gewonnen C2-reichen Fraktion wirtschaftlich arbeitet. The object of the present invention is to provide a generic method for separating a C 2 -rich fraction from a hydrocarbon-rich fraction with simultaneous C 3+ , C 4+ and / or C 5+ recovery, which also applies to the interruption the decrease in the C 2 -rich fraction obtained works economically.

Das erfindungsgemäße Verfahren ist dadurch gekennzeichnet, dass der Deethanizer auf dem gleichen oder einem höheren Druck als der Demethanizer betrieben wird und die am Kopf des Deethanizers abgezogene C2-reiche Fraktion zumindest zeitweilig wenigstens teilweise der am Kopf des Demethanizers abgezogenen C1-reichen Fraktion zugeführt wird. The process according to the invention is characterized in that the deethanizer is operated at the same or a higher pressure than the demethanizer and the C 2 -rich fraction drawn off at the top of the deethanizer is at least temporarily fed at least partially to the C 1 -rich fraction drawn off at the head of the demethanizer becomes.

Kommt es bei dem erfindungsgemäßen Verfahren zum Abtrennen einer C2-reichen Fraktion zu einer Unterbrechung der Abnahme der C2-reichen Fraktion aus dem Prozess, kann der Betrieb der gleichzeitigen C3+-, C4+- und/oder C5+-Gewinnung nunmehr dadurch aufrecht erhalten werden, indem die C2-reiche Fraktion wenigstens teilweise der am Kopf des Demethanizers abgezogenen C1-reichen Fraktion zugeführt wird. Ein Abfackeln dieser C2-reichen Fraktion ist somit nicht mehr erforderlich. If the process according to the invention for separating a C 2 -rich fraction leads to an interruption in the removal of the C 2 -rich fraction from the process, the operation of the simultaneous C 3+ -, C 4+ - and / or C 5+ - Extraction can now be maintained by at least partially feeding the C 2 -rich fraction to the C 1 -rich fraction drawn off at the top of the demethanizer. A flaring of this C 2 -rich fraction is therefore no longer necessary.

Da erfindungsgemäß der Deethanizer auf dem gleichen oder einem höheren Druck als der Demethanizer betrieben wird, kann die Zuspeisung der C2+-reichen Fraktion zu der am Kopf des Demethanizers abgezogenen C1-reichen Fraktion ohne ein vorheriges Pumpen der C2+-reichen Fraktion auf einen höheren Druck erfolgen. Since, according to the invention, the deethanizer is operated at the same or a higher pressure than the demethanizer, the C 2+ -rich fraction can be fed to the C 1 -rich fraction drawn off at the top of the demethanizer without prior pumping of the C 2+ -rich fraction done at a higher pressure.

Gemäß einer vorteilhaften Ausgestaltung des erfindungsgemäßen Verfahrens wird die aus dem Sumpf des Demethanizers abgezogene Flüssigfraktion, die dem Deethanizer zugeführt wird, wenigstens auf einem Druck bereitgestellt, der es erlaubt, dass das Kopfprodukt des Deethanizers dem Kopfprodukt des Demethanizers - ohne eine zusätzliche Verdichtung des Kopfproduktes des Deethanizers - zugemischt werden kann. Dies kann - wie nachfolgend anhand der Figurenbeschreibung erläutert werden wird - mittels einer zwischen Demethanizer und Deethanizer vorzusehenden Pumpe erfolgen. According to an advantageous embodiment of the method according to the invention, the liquid fraction drawn off from the bottom of the demethanizer, the deethanizer is supplied, at least at a pressure which allows the Deethanizer header product Demethanizer header product - without one additional compression of the head product of the deethanizer can. This can be explained as follows using the description of the figures is - by means of a pump to be provided between the demethanizer and deethanizer respectively.

Alternativ dazu kann jedoch auch mittels einer entsprechenden räumlichen Anordnung von Demethanizer und Deethanizer ein Druckgefälle zwischen Demethanizer und Deethanizer realisiert werden. As an alternative to this, however, a corresponding spatial arrangement can also be used of Demethanizer and Deethanizer a pressure drop between Demethanizer and Deethanizers can be realized.

Insbesondere dann, wenn eine Abnahme der gewonnenen C2-reichen Fraktion nicht erfolgt bzw. erfolgen kann, können - entsprechend einer Ausgestaltung des erfindungsgemäßen Verfahrens - eine oder mehrere der nachfolgenden Maßnahmen a) bis d) durchgeführt werden:

  • a) Erhöhung der Temperatur des dem Demethanizer aufgegebenen Rücklaufstromes um bis zu 20 K, vorzugsweise um 10 bis 15 K
  • b) Verringerung der Menge oder Unterbrechung der Zuführung des dem Demethanizer aufgegebenen Rücklaufstromes
  • c) Erhöhung der Temperatur der der Entspannung zugeführten Kohlenwasserstoffreichen Fraktion um bis zu 20 K, vorzugsweise um 10 bis 15 K
  • d) Erhöhung der Sumpftemperatur des Demethanizers um bis zu 15 K, vorzugsweise um 5 bis 10 K.
In particular, if a decrease in the C 2 -rich fraction obtained cannot or cannot take place, one or more of the following measures a) to d) can be carried out, in accordance with an embodiment of the method according to the invention:
  • a) increasing the temperature of the reflux stream fed to the demethanizer by up to 20 K, preferably by 10 to 15 K.
  • b) Reduction in the amount or interruption of the supply of the return stream fed to the demethanizer
  • c) increasing the temperature of the hydrocarbon-rich fraction fed to the expansion by up to 20 K, preferably by 10 to 15 K.
  • d) increasing the bottom temperature of the demethanizer by up to 15 K, preferably by 5 to 10 K.

Die Maßnahme a) lässt sich beispielsweise dadurch realisieren, dass das Fremdkälteangebot für die Abkühlung der aufzutrennenden Kohlenwasserstoff-reichen Fraktion - also des Rohgases - verringert wird; gleiches gilt für die Maßnahme c). Measure a) can be implemented, for example, in that the Offer of external cooling for cooling the hydrocarbon-rich to be separated Fraction - ie the raw gas - is reduced; the same applies to measure c).

Wird wenigstens eine der Maßnahmen a) bis d) realisiert, so reduziert sich die C2+- Konzentration im Sumpf des Demethanizers auf etwa 70 bis 85% der Designmenge, was eine entsprechende Entlastung des dem Demethanizers nachgeschalteten Deethanizers zur Folge hat. If at least one of the measures a) to d) is implemented, the C 2+ concentration in the sump of the demethanizer is reduced to about 70 to 85% of the design amount, which results in a corresponding relief of the deethanizer downstream of the demethanizer.

Gemäß einer weiteren vorteilhaften Ausgestaltung des erfindungsgemäßen Verfahrens bleiben während der Realisierung der vorgenannten Maßnahmen die Temperatur und/oder die Temperaturverhältnisse im Demethanizer (M) unverändert, während der Druck im Deethanizer (E) unverändert bleibt oder angehoben wird. According to a further advantageous embodiment of the method according to the invention remain the temperature during the implementation of the aforementioned measures and / or the temperature conditions in the demethanizer (M) unchanged during the Pressure in the deethanizer (E) remains unchanged or is raised.

Während bei normaler Verfahrensweise etwa 99,9% der C3-Kohlenwasserstoffe, die im Einsatz- bzw. Rohgas enthalten sind, gewonnen werden, werden im Falle der entsprechend der Erfindung veränderten Betriebsweise noch etwa 97,7% der C3- Kohlenwasserstoffe im Sumpf des Demethanizers gewonnen. Der Verlust an C3- Kohlenwasserstoffen beschränkt sich somit auf ca. 2% und ist daher nahezu vernachlässigbar. Allerdings werden auf Grund der höheren Temperatur im Deethanizer ca. 20 bis 50% des C3-Produktes mitkondensiert und gelangen dadurch in das sog. Sales- bzw. Verkaufsgas. Nunmehr kann jedoch die gesamte C2-reiche Fraktion in die C1-reiche Fraktion - dies ist das sog. Verkaufsgas - zurückgeführt werden, wodurch keine diesbezüglichen Verluste entstehen. While about 99.9% of the C 3 hydrocarbons contained in the feed gas or raw gas are obtained in a normal procedure, about 97.7% of the C 3 hydrocarbons are still in the sump in the case of the mode of operation modified according to the invention of the demethanizer won. The loss of C 3 hydrocarbons is thus limited to approx. 2% and is therefore almost negligible. However, due to the higher temperature in the deethanizer, approx. 20 to 50% of the C 3 product is also condensed and thereby reaches the so-called sales gas. However, the entire C 2 -rich fraction can now be returned to the C 1 -rich fraction - this is the so-called sales gas - which means that there are no losses in this regard.

Sofern die vorgenannten Verluste an C3-Kohlenwasserstoffen nicht tolerierbar sind, kann der Kondensator des Deethanizers für eine Totalkondensation - ggf. bei höherem Druck - ausgelegt werden, wodurch jedoch der Kältemittelbedarf auf dieser Druckstufe erhöht wird. Ferner erhöht sich der apparative Aufwand, da ein größerer Reboller sowie eine größere Reinjektionspumpe erforderlich werden. If the aforementioned losses of C 3 hydrocarbons cannot be tolerated, the condenser of the deethanizer can be designed for total condensation - if necessary at higher pressure - which, however, increases the refrigerant requirement at this pressure level. Furthermore, the expenditure on equipment increases, since a larger re-roller and a larger reinjection pump are required.

Da in einigen Staaten aufgrund entsprechend strenger Umweltrichtlinien ein Abfackeln der C2- oder C2+-reichen Fraktion nicht erlaubt ist und bei einer Unterbrechung der Abnahme dieser Fraktion die gesamte Anlage stillgelegt werden müsste, wird mittels des erfindungsgemäßen Verfahrens überhaupt erst ein Weiterbetrieb der Anlage auch bei einer Unterbrechung der Abnahme des C2-Produktes ermöglicht. Since in some countries due to correspondingly stringent environmental guidelines, flaring of the C 2 - or C 2+ -rich fraction is not permitted and the entire plant would have to be shut down if the removal of this fraction was interrupted, the process according to the invention only allows the plant to continue operating even if the acceptance of the C 2 product is interrupted.

Das erfindungsgemäße Verfahren sowie weitere Ausgestaltungen desselben, die Gegenstände der abhängigen Patentansprüche sind, seien im Folgenden anhand des in der Figur dargestellten Ausführungsbeispieles näher erläutert. The inventive method and further refinements of the same Subjects of the dependent claims are, based on the illustrated in the figure embodiment.

Über Leitung 1 wird die zu zerlegende Kohlenwasserstoff-reiche Fraktion - das sog. Rohgas - dem Prozess zugeführt und in dem Wärmetauscher E1 gegen anzuwärmende Verfahrensströme, auf die im Folgenden noch näher eingegangen werden wird, sowie ggf. gegen einen oder mehrere, in der Figur der Übersichtlichkeit halber nicht dargestellte Kältemittel und/oder Zwischenheizungen des Demethanizers M abgekühlt, partiell kondensiert, in Flüssig- und Gasphase getrennt (Ströme 2 bzw. 3) und - eventuell nach einer kälteleistenden Entspannung bzw. mit oder ohne weitere Abkühlung im Wärmetauscher E1 - dem Demethanizer M zugeführt. In der Figur nicht dargestellt sind die in den Leitungen 2 und/oder 3' ggf. vorzusehenden Entspannungsventile. The hydrocarbon-rich fraction to be separated - the so-called raw gas - is fed to the process via line 1 and in the heat exchanger E1 against process streams to be heated, which will be discussed in more detail below, and optionally against one or more in the figure For the sake of clarity, the refrigerant and / or intermediate heaters of the demethanizer M, not shown, are cooled, partially condensed, separated in the liquid and gas phases (streams 2 and 3 ) and - possibly after a cooling relief or with or without further cooling in the heat exchanger E1 - the Demethanizer M fed. The expansion valves that may be provided in lines 2 and / or 3 'are not shown in the figure.

Über Leitung 12 wird dem Demethanizer M ein Rücklaufstrom, der im Wärmetauscher E1 ab- bzw. unterkühlt wird, zugeführt. A return flow, which is cooled or subcooled in the heat exchanger E1, is fed to the demethanizer M via line 12 .

Am Kopf des Demethanizers M wird eine C1-reiche Fraktion - das sog. Verkaufsgas - gewonnen und über Leitung 11 abgezogen. Diese Fraktion wird im Wärmetauscher E1 gegen abzukühlende Verfahrensströme angewärmt und über Leitung 11' beispielsweise einer ein- oder mehrstufigen, in der Figur nicht dargestellten Verdichtung und anschließend einer Pipeline zugeführt. A C 1 -rich fraction - the so-called sales gas - is obtained at the head of the demethanizer M and drawn off via line 11 . This fraction is heated in the heat exchanger E1 against process streams to be cooled and is fed via line 11 ', for example, to a one- or multi-stage compression, not shown in the figure, and then to a pipeline.

Die Sumpfheizung des Demethanizers M sei durch die Leitung 4 sowie den darin angeordneten Wärmetauscher E2 dargestellt. The bottom heater of the demethanizer M is represented by the line 4 and the heat exchanger E2 arranged therein.

Aus dem Sumpf des Demethanizers M wird über Leitung 5 eine C2+-reiche Flüssigfraktion abgezogen, mittels der Pumpe P1 auf den in dem Deethanizer E herrschenden Druck gepumpt und anschließend dem Kopf des Deethanizers E zugeführt. A C 2+ -rich liquid fraction is drawn off from the bottom of the demethanizer M via line 5 , pumped to the pressure prevailing in the deethanizer E by means of the pump P1 and then fed to the head of the deethanizer E.

Auch der Deethanizer E weist eine Sumpfheizung auf, die durch die Leitung 6 sowie den darin angeordneten Wärmetauscher E3 dargestellt ist. The deethanizer E also has a sump heater, which is represented by the line 6 and the heat exchanger E3 arranged therein.

Aus dem Sumpf des Deethanizers E wird über Leitung 7 eine C3+-reiche Flüssigfraktion abgezogen und ggf. einer Nachbehandlung, wie beispielsweise einer weiteren ein- oder mehrstufigen Zerlegung, zugeführt. A C 3+ -rich liquid fraction is drawn off from the bottom of the deethanizer E via line 7 and, if appropriate, fed to an aftertreatment, such as a further one- or multi-stage decomposition.

Am Kopf des Deethanizers E wird über Leitung 8 eine C2+-reiche Gasfraktion abgezogen, im Wärmetauscher E4 partiell kondensiert und dem Abscheider D2 zugeführt. At the top of the deethanizer E, a C 2+ -rich gas fraction is drawn off via line 8 , partially condensed in the heat exchanger E4 and fed to the separator D2.

Am Kopf des Abscheiders D2 wird über Leitung 9 eine C2-reiche Produktfraktion abgezogen und - ggf. nach einer Anwärmung, CO2-Entfernung mit Einstellung des Wassertaupunktes - einer Ethylenanlage als Rohstoff zugeführt; diese Verfahrensführung bzw. dieser Betriebszustand ist in der Figur nicht dargestellt. At the head of the separator D2, a C 2 -rich product fraction is drawn off via line 9 and - if necessary after heating, CO 2 removal with adjustment of the water dew point - fed to an ethylene plant as raw material; this procedure or operating state is not shown in the figure.

Aus dem Sumpf des Abscheiders D2 wird über Leitung 10 eine C2+-reiche Fraktion abgezogen und im Normalbetrieb über Leitung 10' mittels der Pumpe P2 als Rücklauf auf den Kopf des Deethanizers E zurückgegeben. A C 2+ -rich fraction is drawn off from the bottom of the separator D2 via line 10 and returned in normal operation via line 10 'by means of the pump P2 as a return to the head of the deethanizer E.

Im Falle der Realisierung des erfindungsgemäßen Verfahrens wird nunmehr die C2- reiche Produktfraktion über Leitung 9 der aus dem Kopf des Demethanizer M über Leitung 11 abgezogenen C1-reichen Gasfraktion zugespeist. In the case of the implementation of the method according to the invention, the C 2 -rich product fraction is now fed via line 9 to the C 1 -rich gas fraction drawn off from the top of the demethanizer M via line 11 .

Die Zuführung der C2-reichen Fraktion über Leitung 9 zu dem Verkaufsgas erfolgt hierbei an einer von der Temperatur und dem Druck geeigneten Stelle während der Anwärmung der über Leitung 11 am Kopf des Demethanizers M abgezogenen Verkaufsgasfraktion. Dadurch wird die Kältenutzung der zugeführten C2-reichen Flüssigfraktion maximiert und gleichzeitig der Fremdkältebedarf auf der Niederdruckseite verringert. Nachteilig hierbei ist jedoch, dass die im Regelfall vorzusehende Verdichtung des Verkaufsgases geringfügig höher belastet wird. The supply of the C 2 -rich fraction via line 9 to the sales gas takes place here at a point which is suitable for the temperature and the pressure during the heating of the sales gas fraction drawn off via line 11 at the top of the demethanizer M. This maximizes the cold use of the supplied C 2 -rich liquid fraction and at the same time reduces the need for external cooling on the low pressure side. The disadvantage here, however, is that the compression of the sales gas to be provided as a rule is subject to a slightly higher load.

Alternativ dazu kann die C2-reiche Flüssigfraktion dem Verkaufsgas auch erst nach dessen Verdichtung und vor dem der Verdichtung nachgeschalteten Kühler zugeführt werden. Dies hätte den Vorteil, dass der Kühlmittelbedarf des Verkaufsgaskühlers verringert wird und der Verkaufsgasverdichter keine höhere Belastung erfährt. Denkbar wäre zudem eine Kombination aus den beiden vorbeschriebenen Verfahrensvarianten. As an alternative to this, the C 2 -rich liquid fraction can also be supplied to the sales gas only after it has been compressed and before the cooler connected downstream of the compression. This would have the advantage that the coolant requirement of the sales gas cooler is reduced and the sales gas compressor is not subjected to a higher load. A combination of the two above-described process variants would also be conceivable.

Claims (6)

1. Verfahren zum Abtrennen einer C2-reichen Fraktion aus einer Kohlenwasserstoffreichen Fraktion mit gleichzeitiger C3+-, C4+- und/oder C5+-Gewinnung, wobei die Kohlenwasserstoff-reiche Fraktion entspannt, mehrstufig partiell kondensiert und in wenigstens einem Demethanizer und wenigstens einem Deethanizer aufgetrennt wird, dadurch gekennzeichnet, dass der Deethanizer (E) auf dem gleichen oder einem höheren Druck als der Demethanizer (M) betrieben wird und die am Kopf des Deethanizers (E) abgezogene C2-reiche Fraktion (9) zumindest zeitweilig wenigstens teilweise der am Kopf des Demethanizers (M) abgezogenen C1- reichen Fraktion (11, 11') zugeführt wird. 1. A process for separating a C 2 -rich fraction from a hydrocarbon-rich fraction with simultaneous C 3+ , C 4+ and / or C 5+ recovery, the hydrocarbon-rich fraction being relaxed, partially condensed in several stages and in at least one Demethanizer and at least one deethanizer is separated, characterized in that the deethanizer (E) is operated at the same or a higher pressure than the demethanizer (M) and the C 2 -rich fraction ( 9 ) drawn off at the top of the deethanizer (E) at least temporarily at least partially to the C 1 -rich fraction ( 11 , 11 ') drawn off at the top of the demethanizer (M). 2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die aus dem Sumpf des Demethanizers (M) abgezogene Flüssigfraktion (5), die dem Deethanizer (E) zugeführt wird, wenigstens auf einem Druck bereitgestellt, der es erlaubt, dass das Kopfprodukt (8, 9) des Deethanizers (E) dem Kopfprodukt (11, 11') des Demethanizers (M), ohne eine zusätzliche Verdichtung des Kopfproduktes (8, 9) des Deethanizers (E), zugemischt werden kann. 2. The method according to claim 1, characterized in that the liquid fraction ( 5 ) drawn off from the bottom of the demethanizer (M) and which is fed to the deethanizer (E) is provided at least at a pressure which allows the top product ( 8 , 9 ) of the deethanizer (E) can be mixed with the top product ( 11 , 11 ') of the demethanizer (M) without additional compression of the top product ( 8 , 9 ) of the deethanizer (E). 3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, dass zeitweilig, insbesondere dann, wenn eine Abnahme der gewonnenen C2-reichen Fraktion nicht erfolgt, eine oder mehrere der nachfolgenden Maßnahmen a) bis d) durchgeführt werden: a) Erhöhung der Temperatur des dem Demethanizer (M) aufgegebenen Rücklaufstromes (2, 3''') um bis zu 20 K, vorzugsweise um 10 bis 15 K b) Verringerung der Menge oder Unterbrechung der Zuführung des dem Demethanizer (M) aufgegebenen Rücklaufstromes (2, 3''') c) Erhöhung der Temperatur der der Entspannung (T) zugeführten Kohlenwasserstoffreichen Fraktion (3") um bis zu 20 K, vorzugsweise um 10 bis 15 K d) Erhöhung der Sumpftemperatur des Demethanizers (M) um bis zu 15 K, vorzugsweise um 5 bis 10 K. 3. The method according to claim 1 or 2, characterized in that one or more of the following measures a) to d) are carried out temporarily, in particular when there is no decrease in the C 2 -rich fraction obtained: a) increasing the temperature of the return stream ( 2 , 3 ''') fed to the demethanizer (M) by up to 20 K, preferably by 10 to 15 K. b) Reduction in the quantity or interruption of the supply of the return flow ( 2 , 3 ''') fed to the demethanizer (M) c) increasing the temperature of the hydrocarbon-rich fraction ( 3 ") supplied to the expansion (T) by up to 20 K, preferably by 10 to 15 K. d) increasing the bottom temperature of the demethanizer (M) by up to 15 K, preferably by 5 to 10 K. 4. Verfahren nach Anspruch 3, dadurch gekennzeichnet, dass für den Fall, dass mehrere der unter a) bis d) genannten Maßnahmen durchgeführt werden, diese zeitgleich oder zumindest zeitweilig überlappend durchgeführt werden. 4. The method according to claim 3, characterized in that in the event that several of the measures mentioned under a) to d) are carried out, these be carried out simultaneously or at least temporarily overlapping. 5. Verfahren nach einem der vorhergehenden Ansprüche 1 bis 4, dadurch gekennzeichnet, dass die Temperatur und/oder die Temperaturverhältnisse im Demethanizer (M) unverändert bleiben, während der Druck im Deethanizer (E) unverändert bleibt oder angehoben wird. 5. The method according to any one of the preceding claims 1 to 4, characterized characterized in that the temperature and / or the temperature conditions in the Demethanizer (M) remain unchanged while the pressure in the Deethanizer (E) remains unchanged or is raised. 6. Verfahren nach einem der vorhergehenden Ansprüche 1 bis 5, dadurch gekennzeichnet, dass die Zuführung der am Kopf des Deethanizers (E) abgezogenen C2-reichen Fraktion (9) zu der am Kopf des Demethanizers (M) abgezogenen C1-reichen Fraktion (11, 11') vor und/oder nach einer möglichen Verdichtung der C1-reichen Fraktion erfolgt. 6. The method according to any one of the preceding claims 1 to 5, characterized in that the supply of the C 2 -rich fraction ( 9 ) drawn off at the head of the deethanizer (E) to the C 1 -rich fraction drawn off at the head of the demethanizer (M) ( 11 , 11 ') before and / or after a possible compression of the C 1 -rich fraction.
DE2001140585 2001-08-18 2001-08-18 Separation of lower hydrocarbons comprises operating de-ethanizer at no less than de-methanizer pressure and combines head fractions for at least an interval Withdrawn DE10140585A1 (en)

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NO20023888A NO20023888L (en) 2001-08-18 2002-08-16 Process for separating a C2-rich fraction from a hydrocarbon-rich fraction with simultaneous C3 +, C4 + and / or C5 + recovery

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WO2008022998A3 (en) * 2006-08-23 2008-11-20 Shell Int Research Method and apparatus for treating a hydrocarbon stream
DE102014005935A1 (en) * 2014-04-24 2015-10-29 Linde Aktiengesellschaft Process for separating heavy hydrocarbons
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WO2017125438A1 (en) * 2016-01-18 2017-07-27 Linde Aktiengesellschaft Method for the separation processing of a gas mixture

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