EP0448439B1 - Verfahren zur Fraktionierung von einem Gasgemisch enthaltend Wasserstoff, leichte alifatische Kohlenwasserstoffe und leichte aromatische Kohlenwasserstoffe - Google Patents

Verfahren zur Fraktionierung von einem Gasgemisch enthaltend Wasserstoff, leichte alifatische Kohlenwasserstoffe und leichte aromatische Kohlenwasserstoffe Download PDF

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Publication number
EP0448439B1
EP0448439B1 EP91400637A EP91400637A EP0448439B1 EP 0448439 B1 EP0448439 B1 EP 0448439B1 EP 91400637 A EP91400637 A EP 91400637A EP 91400637 A EP91400637 A EP 91400637A EP 0448439 B1 EP0448439 B1 EP 0448439B1
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fraction
gaseous fraction
stage
gaseous
liquid
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French (fr)
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EP0448439A1 (de
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Ari Minkkinen
Serge Mouratoff
Larry Mank
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IFP Energies Nouvelles IFPEN
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    • 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
    • C10G35/00—Reforming naphtha
    • 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
    • C10G5/04—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas with liquid absorbents

Definitions

  • the invention relates to a process for fractionating a gaseous mixture containing hydrogen, light aliphatic hydrocarbons and light aromatic hydrocarbons.
  • the invention aims, more particularly, to separately collect (1) hydrogen of high purity, and in particular only contain traces of aromatic hydrocarbons, (2), aliphatic hydrocarbons C2 - C5, in particular C3 or C3 - C4, which can be recycled, at least in part, to a hydrocarbon conversion process, for example a dehydrocyclodimerization process, and (3) light aromatic hydrocarbons alone or as a mixture (BTX).
  • a hydrocarbon conversion process for example a dehydrocyclodimerization process
  • BTX light aromatic hydrocarbons alone or as a mixture
  • the effluent is a mixture of hydrogen, light aliphatic hydrocarbons, in particular from C1 to C5, and light aromatic hydrocarbons, in particular benzene, toluene and / or xylene or their mixtures ( BTX).
  • these processes mention may be made of catalytic reforming, aromatization, dehydrogenation, dehydrocyclization, steam cracking and dehydrocyclodimerization.
  • light paraffins or olefins for example C3 and C4 are converted into light aromatic hydrocarbons in contact with zeolitic catalysts.
  • the hydrogen is separated in a high pressure separator and the hydrocarbons are separated in a train of distillation columns.
  • perm-selective membranes have also been proposed for separating hydrogen from hydrocarbons, for example in US 4180388, 4398926 and 4654047.
  • the use of a perm-selective membrane and fractionation columns is described in US 45488619 In this latter patent, the effluent from a dehydrocyclodimerization unit is first summarily fractionated; the liquid fraction is distilled to collect the BTX and the gaseous fraction is compressed and then washed with aromatic hydrocarbons or with C7 - C10 paraffinic hydrocarbons of external origin.
  • the present invention relates to a process for fractionating a gaseous mixture containing hydrogen, light aliphatic hydrocarbons and aromatic hydrocarbons, energy efficient, in particular in which the energy requirements for the fractionation of the products are reduced; and also a process in which the hydrogen obtained is substantially free of aromatic hydrocarbons; a process also which makes it possible to use membranes sensitive to aromatic hydrocarbons, due to the virtual absence of these in the gas subjected to permeation. In the process of the invention, the undesirable crystallization of aromatic hydrocarbons is avoided.
  • a gaseous mixture and for example the gaseous effluent from a hydrocarbon conversion reactor, which contains hydrogen, light aliphatic hydrocarbons and light aromatic hydrocarbons is first cooled at a temperature allowing the condensation of part of the hydrocarbons. Separating a first non-condensed gaseous fraction relatively poor in aromatics and a first liquid fraction relatively poor in aromatics and a first liquid fraction relatively rich in aromatics.
  • the first gaseous fraction is compressed and cooled, so as to condense at least a second liquid fraction, and the second liquid fraction is separated from a second non-condensed gaseous fraction.
  • the second gaseous fraction is brought into contact with a liquid phase of aliphatic hydrocarbons, defined below, in a contact zone, under conditions ensuring at the same time the vaporization of at least one fraction, for example at least 50% ( preferably 60-95%), of the liquid phase of aliphatic hydrocarbons, and the condensation of at least part of the aromatic hydrocarbons of the second gaseous fraction, said condensation being caused, at least in part by the cooling due to the vaporization of aliphatic hydrocarbons, and a third gas fraction is separated from a third liquid fraction comprising aliphatic hydrocarbons and aromatic hydrocarbons.
  • the second and third liquid fractions can also be drawn off as a mixture.
  • the third gas fraction is treated to bring it above the dew point, it is circulated in contact with at least one membrane permeable to hydrogen and a gaseous fraction enriched in hydrogen and a fourth depleted gaseous fraction are collected. into hydrogen.
  • the fourth gas fraction is cooled so as to partially condense it and a fifth gas fraction, rich in methane, which can constitute a "fuel gas", and a fourth liquid fraction containing at least one C3 hydrocarbon are collected. to C5.
  • the first, second, third and fourth liquid fractions are subjected to distillation, together or separately, in one or more columns, and at least a sixth gaseous fraction containing at least one C3 or C5 hydrocarbon is collected at the top and at least in the tail a fifth liquid fraction which constitutes a desired aromatic hydrocarbon fraction. At least a part of the hydrocarbons of the sixth gaseous fraction are condensed and sent to the contact zone to constitute at least a part of the liquid phase of aliphatic hydrocarbons.
  • Preferably another part of the sixth gaseous fraction is sent to the hydrocarbon conversion reactor, as a recycling stream, at least when one or more of the hydrocarbons from C3 to C5 constitute a reagent for said conversion.
  • the hydrocarbon conversion reactor can be, for example, a C2-C5, particularly C3 and / or C4 light hydrocarbon aromatization reactor, using a zeolite as catalyst, in particular a zeolite described in French patent 2634139 or 2634140 .
  • the pressure at the outlet of the reactor is, for example 1.5 to 10 bars, commonly 2-5 bars. If the temperature is high, it is lowered to 10-60 ° C, preferably 30-50 ° C, so as to condense part of the gaseous effluent from the reactor and to collect at least part of the aromatic hydrocarbons. If desired, the pressure can be modified to promote the condensation of aromatic hydrocarbons.
  • the first gas fraction is then compressed to, for example, 15-40 bars, preferably 20-30 bars, and cooled, to bring its temperature to 0-50 ° C, preferably 25-35 ° C, and condense at least a second liquid fraction, containing aromatics.
  • This liquid fraction is separated from the second gaseous fraction under the above pressure.
  • several compression stages can be used, each followed by partial condensation and fractionation.
  • the bringing of the second gaseous fraction into contact with the recycled liquid phase of aliphatic hydrocarbons containing at least one hydrocarbon C3 to C5, preferably C4-C5, constitutes an essential point of the invention.
  • the vaporization of at least 50% of the hydrocarbons C3 to C5 from this liquid phase causes cooling of the second gaseous fraction and the condensation of at least part of the residual aromatic hydrocarbons.
  • the temperature is, for example, between - 10 and + 40 ° C, preferably between 5 and 35 ° C. At the head the temperature is between - 10 and + 30 ° C, preferably for example between 0 and 20 ° C.
  • the pressure can be substantially that of the second gas fraction (after compression of the first gas fraction), that is to say, 15-40 bars, preferably 20-30 bars.
  • the quantity of liquid phase of aliphatic hydrocarbons can represent, for example, 5 to 35%, preferably 10 to 25% of the quantity of second gaseous fraction, but the invention is not limited to particular proportions. .
  • the recycled liquid phase of aliphatic hydrocarbons also to contain a certain proportion of non-aromatic C6, C7 and / or C8 hydrocarbons.
  • the resulting gas stream is then brought above its dew point, for example by heating or by dilution with a dry gas, but preferably by additional compression ensuring overheating (an increment of 2 to 7 bars is generally sufficient). It is then brought into contact with at least one selective permeation membrane, in one or more stages.
  • the overheating is preferably such that no condensation occurs during the withdrawal of hydrogen from the membrane.
  • permeation membrane may be a commercial or prior art membrane and will therefore not be described in detail.
  • the operating conditions depend on the membrane, for example around 80-150 ° C at 20-40 bars with the usual membranes.
  • the fraction of hydrogen-depleted gas which usually contains C1-C5 hydrocarbons is subjected to cooling to condense a liquid phase containing C3-C5 hydrocarbons.
  • the cooling may use, in part, relatively cold streams of the process, for example the stream of the fifth gas fraction, and, in part, streams of liquefied gas, for example a stream of liquid propane or ethane.
  • the distillation of the liquid fractions can be carried out separately or after mixing 2 or more fractions. It is also possible not to directly distill the second liquid fraction and return it to the first fractionation zone in order to be fractionated again in mixture with the reactor effluent.
  • a mixture of the first liquid fraction and the second liquid fraction can be distilled; the third and fourth liquid fractions are then distilled separately.
  • the first, second, third and fourth liquid fractions can also be distilled together. Other combinations of fractions can also be used.
  • the third gaseous fraction is compressed before passing through the permeation zone.
  • the compressor can then be in line with the compressors of the previous stages.
  • the compressor for the third gaseous fraction receives the energy, preferably mechanical energy, produced by a regulator placed on the circuit of the fifth gaseous fraction.
  • a turbocharger and a turboexpander are preferably used respectively.
  • the sixth gas fraction is subjected to partial condensation: at least part of the condensate rich in butanes and pentanes, is used as liquid for contacting with the second gas fraction, the rest is returned as reflux to the column in which said sixth gas fraction was separated from said fifth liquid fraction; the non-condensed part, constituting a seventh gas fraction rich in propane, can be returned to the dehydrocyclodimerization reactor.
  • the figure illustrates a non-limiting mode of implementation of the invention.
  • the gaseous effluent (1) of a paraffin flavoring unit C3 - C9 available at 1.5 - 5 bars is cooled to 30 - 40 ° C in the exchanger (2). It optionally receives the current (3).
  • part of the gas phase is condensed and a liquid phase (5) and a gas phase (6) are separated in the flask (4). This undergoes one or more compression stages (7) followed by cooling (8).
  • the liquids collected can be sent by line (9) for distillation or by line (3) at the entrance to the installation. From the flask (10) a gas stream (11) comes out which is contacted in the flask (12) with a liquid stream C3-C5 from the line (13).
  • the gas phase (14) undergoes compression with overheating in the compressor (15) and then passes into the permeation unit (16).
  • Purified hydrogen exits through line (17).
  • the residual gas (38) is cooled, for example by cold water (18), by a stream of cold gas (19-21) and by liquid propane (20) at low temperature, for example - 30 to - 40 ° C. Partial liquefaction occurs and a methane-rich gas is collected at the top of the column (23) via the line (21) and a liquid stream (22) at the bottom of the column (23).
  • the liquid stream (24) withdrawn from the contactor (12) is also sent to the column (23), but preferably at a point lower than that of admission of the stream from the permeation unit.
  • the liquid (22) is refracted in the column (25) which, in the example considered, also receives the liquid from line (5).
  • the latter is preferably introduced at a relatively low point of the column (25), lower than the level of introduction of the liquid (22).
  • a mixture rich in aromatic hydrocarbons is collected by line (26).
  • the vapors (27), rich in hydrocarbons (C3-C5) are cooled and partially condensed (28).
  • a liquid phase is collected, for example C3-C5 or C4-C5, which is returned in part to the contactor (12) by the line (13).
  • One can also recycle part of it to the aromatization reactor via line (30).
  • One can ensure a reflux by the line (31). If a gas phase remains (32), it can be returned to the dehydrocyclodimerization reactor.
  • the separator (10) is not used and the current which has passed through the cooler (8) is sent directly to the bottom of the contactor (12). In this case, the second and the third liquid fractions leave in mixture by the line (24). Lines (9) and (3) are then not used.
  • the heat released by compression in a compression stage (7) is used to heat the reboiler of a distillation column (23), the gas leaving (33) from the compressor (7) then passes through an exchanger in the reboiler (32) of this column then is sent (34) to the balloon (10) or to the contactor (12).
  • the cooler (8) can then be removed (35,36,37) are expansion valves.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Claims (11)

  1. Verfahren zum Fraktionieren einer gasförmigen Mischung, die Wasserstoff, leichte aliphatische Kohlenwasserstoffe und leichte aromatische Kohlenwasserstoffe enthält, dadurch gekennzeichnet, daß
    (a) man diese Mischung abkühlt, um einen Teil der Kohlenwasserstoffe zu kondensieren, und man eine nicht-kondensierte erste gasförmige Fraktion, die an Aromaten abgereichert ist, und eine kondensierte erste flüssige Fraktion, die mit Aromaten angereichert ist, trennt,
    (b) man den Druck der ersten gasförmigen Fraktion erhöht, man dann diese Fraktion abkühlt, derart, um eine zweite flüssige Fraktion und eine nicht-kondensierte zweite gasförmige Fraktion zu bilden, und man diese Fraktionen trennt,
    (c) man die zweite gasförmige Fraktion mit einer Flüssigphase aus aliphatischen Kohlenwasserstoffen, die wenigstens einen Kohlenwasserstoff, welcher 3 bis 5 Kohlenstoffatome aufweist, enthält, in einer Kontaktzone unter Bedingungen, welche gleichzeitig die Verdampfung wenigstens einer C3-bis C5-Fraktion der Flüssigphase aus aliphatischen Kohlenwasserstoffen und die Kondensation wenigstens eines Teils der aromatischen Kohlenwasserstoffe der zweiten gasförmigen Fraktion sicherstellen, in Kontakt bringt und man eine dritte gasförmige Fraktion von einer dritten flüssigen Fraktion trennt,
    (d) man die dritte gasförmige Fraktion behandelt, um sie oberhalb ihres Taupunktes zu führen, und man sie in Kontakt mit wenigstens einer Wasserstoff-durchlässigen Membran umlaufen läßt, und man eine gasförmige Fraktion, die mit Wasserstoff anreichert ist, und eine vierte gasförmige Fraktion, die an Wasserstoff abgereichert ist, sammelt,
    (e) man die vierte gasförmige Fraktion abkühlt, derart, um sie teilweise zu kondensieren, und man eine fünfte gasförmige Fraktion, die mit Methan angereichert ist, sowie eine vierte flüssige Fraktion, die wenigstens einen Kohlenwasserstoff, welcher 3 bis 5 Kohlenstoffatome aufweist, enthält, sammelt,
    (f) man die erste, zweite, dritte, vierte flüssige Fraktion gemeinsam oder einzeln destilliert und man wenigstens eine sechste gasförmige Fraktion, die wenigstens einen C3- bis C5-Kohlenwasserstoff enthält, und wenigstens eine fünfte flüssige Fraktion, die aromatische Kohlenwasserstoffe enthält, sammelt, und
    (g) man wenigstens einen Teil der Kohlenwasserstoffe der sechsten gasförmigen Fraktion kondensiert und man sie der Kontaktzone des Schrittes (c) zuführt, um wenigstens einen Teil der Flüssigphase aus aliphatischen Kohlenwasserstoffen zu bilden.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die zu fraktionierende Mischung das Produkt eines Reaktors zur Umwandlung von aliphatischen Kohlenwasserstoffen ist und man diesem Reaktor einen Teil der sechsten gasförmigen Fraktion als Reagenz zuführt.
  3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß der Schritt (a) bei 10 bis 60 °C unter 1,5 bis 10 bar durchgeführt wird, die Trennung des Schrittes (b) bei 0 bis 50 °C unter 15 bis 40 bar durchgeführt wird und der Schritt (c) bei -10 °C bis +40 °C unter 15 bis 40 bar durchgeführt wird.
  4. Verfahren nach Anspruch 3, dadurch gekennzeichnet, daß der Schritt (a) bei 30 bis 50 °C unter 1,5 bis 10 bar durchgeführt wird, die Trennung des Schrittes (b) bei 25 bis 35 °C unter 20 bis 30 bar durchgeführt wird, der Schritt (c) bei 5 bis 35 °C unter 20 bis 30 bar durchgeführt wird und der Schritt (d) bei 50 bis 150 °C unter 20 bis 40 bar durchgeführt wird.
  5. Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, daß die Erhöhung der Temperatur des Schrittes (d) durch Verdichtung der dritten gasförmigen Fraktion erhalten wird.
  6. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, daß man die zweite und dritte flüssige Fraktion mischt und daß man sie in Mischung destilliert.
  7. Verfahren nach einem der Ansprüche 1 bis 6, dadurch gekennzeichnet, daß man die dritte gasförmige Fraktion durch mechanische Verdichtungseinrichtungen vor einer Inkontaktbringung mit der Membran komprimiert, daß man die fünfte gasförmige Fraktion in mechanischen Entspannunseinrichtungen entspannt und daß man wenigstens einen Teil der mechanischen Energie, die durch die Entspannung erzeugt wird, auf die Verdichtungseinrichtungen der dritten gasförmigen Fraktion überträgt.
  8. Verfahren nach Anspruch 2, dadurch gekennzeichnet, daß die sechste gasförmige Fraktion einer Teilkondensation unterworfen wird, daß wenigstens ein Teil des Kondensats mit der zweiten gasförmigen Fraktion in Kontakt gebracht wird und daß wenigstens ein Teil der nicht-kondensierten Fraktion dem Reaktor zur Umwandlung von Kohlenwasserstoffen zugeführt wird.
  9. Verfahren nach einem der Ansprüche 1 bis 8, dadurch gekennzeichnet, daß die Abkühlung des Schrittes (b) realisiert wird, indem man die komprimierte erste gasförmige Fraktion in Kontakt mit wenigstens der einen der flüssigen Fraktionen bei der Destillation des Schrittes (f) umlaufen läßt.
  10. Verfahren nach einem der Ansprüche 1 bis 9, dadurch gekennzeichnet, daß man im Schritt (c) 60 bis 95 % der aliphatischen Kohlenwasserstoffe der Flüssigphase aus aliphatischen Kohlenwasserstoffen verdampft.
  11. Verfahren nach einem der Ansprüche 1 bis 10, dadurch gekennzeichnet, daß die zurückgeführte Flüssigphase aus aliphatischen Kohlenwasserstoffen gleichermaßen wenigstens einen nicht-aromatischen C6- bis C8-Kohlenwasserstoff enthält.
EP91400637A 1990-03-20 1991-03-07 Verfahren zur Fraktionierung von einem Gasgemisch enthaltend Wasserstoff, leichte alifatische Kohlenwasserstoffe und leichte aromatische Kohlenwasserstoffe Expired - Lifetime EP0448439B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9003652A FR2659964B1 (fr) 1990-03-20 1990-03-20 Procede de fractionnement d'un melange gazeux renfermant de l'hydrogene des hydrocarbures aliphatiques legers et des hydrocarbures aromatiques legers.
FR9003652 1990-03-20

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EP0448439A1 EP0448439A1 (de) 1991-09-25
EP0448439B1 true EP0448439B1 (de) 1995-07-26

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US (1) US5157200A (de)
EP (1) EP0448439B1 (de)
JP (1) JP2905942B2 (de)
DE (1) DE69111497T2 (de)
FR (1) FR2659964B1 (de)

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JPH10203803A (ja) * 1997-01-20 1998-08-04 Ngk Insulators Ltd 水素ガスの回収・精製・貯蔵装置
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DE3814294A1 (de) * 1988-04-28 1989-11-09 Linde Ag Verfahren zur abtrennung von kohlenwasserstoffen

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JPH04217632A (ja) 1992-08-07
FR2659964A1 (fr) 1991-09-27
DE69111497D1 (de) 1995-08-31
EP0448439A1 (de) 1991-09-25
US5157200A (en) 1992-10-20
DE69111497T2 (de) 1996-04-04
FR2659964B1 (fr) 1992-06-05
JP2905942B2 (ja) 1999-06-14

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