DE2702423B2 - Process for obtaining the ethylene contained in a C2 fraction - Google Patents

Process for obtaining the ethylene contained in a C2 fraction

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Publication number
DE2702423B2
DE2702423B2 DE19772702423 DE2702423A DE2702423B2 DE 2702423 B2 DE2702423 B2 DE 2702423B2 DE 19772702423 DE19772702423 DE 19772702423 DE 2702423 A DE2702423 A DE 2702423A DE 2702423 B2 DE2702423 B2 DE 2702423B2
Authority
DE
Germany
Prior art keywords
fraction
ethylene
ethane
distillation
obtaining
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Withdrawn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
DE19772702423
Other languages
German (de)
Other versions
DE2702423A1 (en
Inventor
Luigi Mailand Gazzi
Oronzo San Donato Milanese Sguera
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.)
SnamProgetti SpA
Original Assignee
SnamProgetti SpA
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 SnamProgetti SpA filed Critical SnamProgetti SpA
Publication of DE2702423A1 publication Critical patent/DE2702423A1/en
Publication of DE2702423B2 publication Critical patent/DE2702423B2/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Withdrawn legal-status Critical Current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
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/04—Purification; Separation; Use of additives by distillation
    • 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
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/12—Refinery or petrochemical off-gas

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Description

Die Erfindung betrifft ein Verfahren zur Gewinnung des in einer Ci-Fraktion enthaltenen Äthylens unter Abtrennung von Äthan durch Destillation.The invention relates to a method for obtaining the ethylene contained in a Ci fraction with the separation of ethane by distillation.

Es ist bekannt, daß das in C2-Fraktionen enthaltene Äthylen destillativ von Äthan getrennt werden kann, wenn in dieser Fraktion darüber hinaus noch andere Bestandteile wie Methan, Acetylen und Propylen enthalten sind, welche jedoch in dem angestrebten Äthylen die zulässige Maximalmenge nicht überschreiten. Nachteilig bei einer derartigen destillativen Auftrennung einer C2-Fraktion in seine Hauptbestandteile zur Gewinnung von Äthylen ist die Tatsache, daß die weitgehend gleiche Flüchtigkeit von Äthylen und Äthan ein Fraktionieren außerordentlich aufwendig macht; denn man benötigt dafür Destillationskolonnen mit einer hohen Bodenzahl, deren Investition, Betrieb und Wartung hohe Kosten verursachtIt is known that the ethylene contained in C2 fractions can be separated from ethane by distillation, if in this fraction there are also other constituents such as methane, acetylene and propylene are contained, which, however, do not exceed the permitted maximum amount in the desired ethylene. A disadvantage of such a distillative separation of a C2 fraction into its main components for the production of ethylene is the fact that the largely same volatility of ethylene and Ethane makes fractionation extremely expensive; because you need distillation columns for this with a large number of trays, the investment, operation and maintenance of which are expensive

Aufgabe der Erfindung ist es nun, die Gewinnung des Äthylens aus einer C2-Fraktion durch Destillation zu erleichtern und ein wirtschaftliches Verfahren zur Verfügung zu stellen.The object of the invention is now to obtain the ethylene from a C2 fraction by distillation facilitate and provide an economical process.

Diese Aufgabe wird erfindungsgemäß durch die kennzeichnenden Maßnahmen des vorstehenden Patemanspruchs gelöstAccording to the invention, this object is achieved by the characterizing measures of the preceding patent claim solved

Überraschenderweise gelingt es nach dem erfindungsgemäßen Verfahren, die bei der bekannten Gewinnung von Äthylen aus C2-Fraktionen auftretenden Schwierigkeiten dadurch zu überwinden, daß die C2-Fraktion zuerst in zwei Fraktionen getrennt wird, deren Verhältnis Äthylen zu Äthan unterschiedlich ist Diese beiden Fraktionen werden nun getrennt anSurprisingly, the process according to the invention succeeds in overcoming the difficulties encountered in the known recovery of ethylene from C 2 fractions in that the C2 fraction is first separated into two fractions whose ratio of ethylene to ethane is different separately

Tabelle 1Table 1

bestimmten Stellen in die Destillationskolonne eingeleitet introduced into the distillation column at certain points

Es ist notwendig, daß die erste Fraktion, also die, dessen Gewichtsverhältnis Äthylen zu Äthan größer als in der C2-Fraktion ist, über der zweiten Fraktion in die Destillierkolonne eingeführt wird. Bei umgekehrter Einspeisung wird ein einwandfreies Arbeiten der Destillierkolonne nicht gewährleistet, da ja bekanntlichIt is necessary that the first parliamentary group, i.e. the whose weight ratio of ethylene to ethane is greater than in the C2 fraction, over the second fraction in the Distillation column is introduced. If the feed is reversed, the Distillation column not guaranteed, as is well known

das Äthylen als Kopfprodukt gewonnen wird, währendthe ethylene is recovered as overhead product while

das Äthan im Bodenprodukt verbleibtthe ethane remains in the soil product

In dem Beispiel wird gezeigt, daß die erfindungsgemäße Einführung der beiden getrennten Fraktionen aus der ursprünglichen C2-Fraktion an den angegebenen Stellen zu wesentlichen Vorteilen führt gegenüber der bisherigen Verfahrensweise, bei der die ganze C2-Fraktion an einer Stelle in die Destillierkolonne eingespeistThe example shows that the introduction according to the invention of the two separate fractions from the original C 2 fraction at the points indicated leads to significant advantages over the previous procedure in which the entire C2 fraction is fed into the distillation column at one point

wurden.became.

Beispielexample

In einer Anlage, bestehend aus einer Destillierkolonne, einer Ableitung für das Kopfprodukt mit der Möglichkeit der Rückspeisung und einer Ableitung für das Bodenprodukt mit der Möglichkeit einer Rückspeisung wurden an zwei getrennten Stellen nach dem erfindungsgemäßen Verfahren bzw. an einer einzigen Stelle nach dem Stand der Technik zwei Fraktionen (1 und 2) aus der C^-Fraktion eingeleitet Bei der Fraktion 1 war das Verhältnis Äthylen zu Äthan höher als in der C^-Fraktion und in der Fraktion 2 geringer. Es wurde mit einem Rückflußverhältnis von 4,455 gearbeitetIn a system consisting of a distillation column, a discharge for the top product with the Possibility of feeding back and a discharge for the soil product with the possibility of feeding back were at two separate points according to the method according to the invention or at a single one Place according to the state of the art two fractions (1 and 2) from the C ^ fraction introduced at the fraction 1 the ratio of ethylene to ethane was higher than in the C ^ fraction and lower in fraction 2. It was worked with a reflux ratio of 4.455

1. Fraktion1st parliamentary group 2. Fraktion2nd parliamentary group KopfproduktTop product BodenproduktSoil product RückflußReflux t/ht / h 1,0951.095 1,90741.9074 2,1912.191 1,8101,810 9,7689.768 Analyse: Mol-%Analysis: mol% CH4 CH 4 0,0120.012 0,0070.007 0,0160.016 0,0040.004 C2H4 C 2 H 4 63,75863.758 51,61451.614 99,9099.90 0,4950.495 99,87799.877 C2H6 C 2 H 6 35,85435.854 48,22748.227 0,0840.084 99,03399.033 0,1190.119 C3H8 C 3 H 8 0,3760.376 0,1520.152 -- 0,4720.472 --

Vergleichcomparison

In Abwandlung des Beispiels 1 wurde in die Zuführungsleitung zur Destillationskolonne die nicht vorfraktionierte, also Ausgangs-C2-Fraktion eingespeist Dabei ergab sich, daß man ein wesentlich höheres Rückfluß verhältnis, nämlich 4,931, benötigte.In a modification of Example 1, the non-pre-fractionated, ie starting C 2 fraction, was fed into the feed line to the distillation column. It was found that a much higher reflux ratio, namely 4.931, was required.

Tabelle 2Table 2

CrFraktion Kopfprodukt Bodenprodukt RückflußCr fraction top product bottom product reflux

2,1912.191

1,8101,810

10,89110,891

Analyse: Mol-%Analysis: mol% 0,0080.008 0,0160.016 -- 0,0040.004 CH4 CH 4 54,93354.933 99,9099.90 0,4950.495 99,87799.877 C2H4 C 2 H 4 44,84544.845 0,0840.084 99,03399.033 0,1190.119 C2H6 C 2 H 6 0,2140.214 -- 0,4720.472 -- C3H8 C 3 H 8

Aus dieser Gegenüberstellung ergibt sich, daß durch das erfindungsgemäße Verfahren mit geringem Rückflußverhältnis gearbeitet werden kann. Die Folge davonThis comparison shows that the process according to the invention has a low reflux ratio can be worked. The consequence of this

Tabelle 3Table 3

ist, daß man mit einem wesentlich geringeren Energieaufwand bei dem erfindungsgemäßen Verfahren rechnen kann, wie die Tabelle 3 zeigtis that you can use much less energy can calculate with the method according to the invention, as Table 3 shows

Erfindungsgemäß According to the invention

Stand der
TechnikState of
technology

RückflußverhältnisReflux ratio 4,4554.455 4,94.9 Wärmebedarf GJHeat demand GJ im Kondensatorin the condenser 96,496.4 106,8106.8 im Reboilerin the reboiler 87,887.8 87,887.8

Claims (1)

Patentanspruch:Claim: Verfahren zur Gewinnung des in einer CrFraktion enthaltenen Äthylens unter Abtrennung von Äthan durch Destillation, dadurch gekennzeichnet, daß man der Destillationsstufe zwei, mittels ein- oder mehrmaliger Fraktionierung des CrSchnitts erhaltene getrennte Fraktionen zuführt, nämlich eine erste Fraktion, in der das Gewichtsverhältnis von Äthylen zu Äthan größer als im Ausgangsgemisch ist, und eine zweite Fraktion, in der das Gewichtsverhältnis von Äthylen zu Äthan kleiner als im Ausgangsgemisch ist, wobei man die erste Fraktion in die Destillationskolonne an einer Stelle über der einführt, an welcher die zweite Fraktion eingeführt wird.Process for the recovery of the ethylene contained in a Cr fraction with separation of Ethane by distillation, characterized in that the distillation stage two, separate fractions obtained by means of one or more fractionation of the Cr section are added, namely a first fraction in which the weight ratio of ethylene to ethane is greater than in the Starting mixture is, and a second fraction, in which the weight ratio of ethylene to ethane is smaller than in the starting mixture, whereby the introduces first fraction into the distillation column at a point above that at which the second Parliamentary group is introduced.
DE19772702423 1976-01-21 1977-01-21 Process for obtaining the ethylene contained in a C2 fraction Withdrawn DE2702423B2 (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
IT1943976A IT1054284B (en) 1976-01-21 1976-01-21 PROCESS FOR THE SEPARATION OF ETHYLENE FROM ETHANE FROM A CUT 02

Publications (2)

Publication Number Publication Date
DE2702423A1 DE2702423A1 (en) 1977-07-28
DE2702423B2 true DE2702423B2 (en) 1979-09-20

Family

ID=11157976

Family Applications (1)

Application Number Title Priority Date Filing Date
DE19772702423 Withdrawn DE2702423B2 (en) 1976-01-21 1977-01-21 Process for obtaining the ethylene contained in a C2 fraction

Country Status (7)

Country Link
CY (1) CY1047A (en)
DE (1) DE2702423B2 (en)
EG (1) EG14553A (en)
ES (1) ES455564A1 (en)
GB (1) GB1539292A (en)
GR (1) GR59767B (en)
IT (1) IT1054284B (en)

Also Published As

Publication number Publication date
GR59767B (en) 1978-02-25
IT1054284B (en) 1981-11-10
ES455564A1 (en) 1978-01-16
EG14553A (en) 1984-09-30
GB1539292A (en) 1979-01-31
CY1047A (en) 1980-08-01
DE2702423A1 (en) 1977-07-28

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8230 Patent withdrawn