EP0305668B1 - Procédé de production d'un concentré d'aromatique propre à l'utilisation comme composante de mélange pour essences - Google Patents

Procédé de production d'un concentré d'aromatique propre à l'utilisation comme composante de mélange pour essences Download PDF

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Publication number
EP0305668B1
EP0305668B1 EP88110072A EP88110072A EP0305668B1 EP 0305668 B1 EP0305668 B1 EP 0305668B1 EP 88110072 A EP88110072 A EP 88110072A EP 88110072 A EP88110072 A EP 88110072A EP 0305668 B1 EP0305668 B1 EP 0305668B1
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EP
European Patent Office
Prior art keywords
distillation
aromatics
boiling
extractive distillation
blending component
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.)
Expired - Lifetime
Application number
EP88110072A
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German (de)
English (en)
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EP0305668A1 (fr
Inventor
Gerhard Dr. Preusser
Gerd Emmrich
Martin Schulze
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.)
Krupp Koppers GmbH
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Krupp Koppers GmbH
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Publication date
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Priority to AT88110072T priority Critical patent/ATE64609T1/de
Publication of EP0305668A1 publication Critical patent/EP0305668A1/fr
Application granted granted Critical
Publication of EP0305668B1 publication Critical patent/EP0305668B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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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
    • C10G7/00—Distillation of hydrocarbon oils
    • C10G7/08—Azeotropic or extractive distillation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • C10L1/06—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for spark ignition

Definitions

  • the invention relates to a process for producing an aromatic concentrate suitable for use as a blending component for gasoline fuels from hydrocarbon mixtures with a boiling range between 40 and 170 ° C, which contain several aromatics in addition to non-aromatics, the hydrocarbon mixture being subjected to an extractive distillation using N-substituted morpholines and their substituents have no more than seven carbon atoms, is subjected as a selective solvent, and the low-boiling non-aromatics with a boiling range up to approx. 105 ° C are practically complete and the higher-boiling non-aromatics with a boiling range between approx.
  • 105 and 160 ° C predominantly Part are distilled off as raffinate overhead from the extractive distillation column, while the majority of the aromatics and the remaining non-aromatics together with the solvent used as an extract from the bottom of the extractive distillation column e are withdrawn, whereupon the solvent is separated by distillation from the other hydrocarbons of the extract in a downstream stripping column and these are used in whole or in part as a blending component.
  • a method of the generic type is described in DE-OS 36 12 384, which does not belong to the prior art. It is envisaged that the hydrocarbon used mixture is introduced into the extractive distillation column without prior separation into individual fractions. Particularly suitable feed hydrocarbon mixtures are reformates and platforms from petroleum processing with a not too high benzene content. Mixtures of such reformates and platforms with pyrolysis gasolines can also be used.
  • the boiling point of these feedstocks is normally 170 ° C. In practice, however, it has been shown that this boiling point is not observed in many cases, since condensation and polymerization products with a boiling point higher than 170 ° C. occur in the upstream production processes, and the reformates and platformates accordingly contaminate. Since these higher-boiling condensation and polymerization products are present in the reformates and platforms in concentrations of up to about 30% by weight, they can lead to impairments when the process described in DE-OS 36 12 384 is carried out.
  • the invention is therefore based on the object of improving the older method in such a way that the difficulties described above are avoided.
  • This object is achieved according to the invention in that when working up feed hydrocarbon mixtures which contain constituents boiling above 170 ° C., the feed hydrocarbon mixture is subjected to a pre-distillation in which constituents boiling up to 169 ° C. (under normal conditions) are separated off by distillation and fed to the extractive distillation, while the distillation residue is added to the aromatic concentrate serving as the blending component.
  • the process according to the invention therefore provides for a pre-distillation of the hydrocarbon feed mixture in such a way that the top product obtained contains only those constituents, which do not lead to permanent contamination of the solvent in the subsequent extractive distillation.
  • higher-boiling constituents which would not be difficult or difficult to remove from the solvent remain in the distillation residue (bottom product) from the pre-distillation, which according to the invention is added to the aromatic concentrate serving as the blending component.
  • the starting point here was the knowledge that the composition of the reformates and platforms normally used as starting material is generally such that non-aromatic compounds are not present in the fraction boiling above 170 ° C. or only in very small amounts.
  • a typical reformate from petroleum processing has a proportion of about 3% by weight of higher-boiling constituents with a boiling point> 170 ° C., which remains in the distillation residue in the process according to the invention and is added to the aromatic concentrate serving as a blending component.
  • the composition of this higher-boiling fraction is as follows:
  • the pre-distillation can be carried out with a relatively low investment and operating costs (low number of trays and low reflux ratio), since a sharp quantitative separation is not necessary in this case.
  • the operating conditions in the pre-distillation can even be set so that some of the o-xylene (bp 144 ° C) is also present in the distillation residue
  • the pre-distillation remains because even in this boiling range there are normally only so few non-aromatics in the feed hydrocarbon mixture that they do not have a disturbing effect when added to the aromatic concentrate serving as a blending component.
  • the non-aromatic content in the distillation residue of the pre-distillation is reduced anyway by the fact that azeotropes between aromatics and non-aromatics predominantly go into the top product of the pre-distillation and are therefore subjected to the subsequent extractive distillation process.
  • the n-nonane forms an azeotrope with the o-xylene.
  • a particularly economical embodiment of the method according to the invention is given when the pre-distillation is carried out under increased pressure.
  • the pressure can be set so that the pre-distillation can be operated at a higher temperature than the extractive distillation, so that the overhead product vapors obtained in the pre-distillation can be used for column heating in the extractive distillation and the condensate obtained is introduced into the extractive distillation.
  • the pre-distillation process uses a pressure of up to 15 bar.
  • the figure shows the flow diagram of an embodiment of the method according to the invention in a highly simplified representation.
  • the feed hydrocarbon mixture to be processed is first introduced via line 1 into column 2, in which the predistillation of the feed hydrocarbon mixture according to the invention is carried out is taken.
  • the top product obtained there is introduced via line 3 into the central part of the extractive distillation column 4 provided with internals and / or packing elements.
  • the hydrocarbons of the raffinate escape overhead from the extractive distillation column and pass via line 5 into column 6, in which the hydrocarbons of the raffinate are separated from the solvent residues by distillation.
  • the latter pass via line 7 into line 8, through which the solvent used is introduced into the upper part of the extractive distillation column 4.
  • the hydrocarbons of the raffinate freed from the solvent are withdrawn via the head 9 from the column 6 and fed to their further use.
  • the hydrocarbons of the extract are withdrawn together with the main amount of the solvent via line 10 from the bottom of the extractive distillation column 4 and from there into the middle part of the stripping column 11, which is also provided with internals and / or packing elements.
  • the hydrocarbons of the extract which consist mainly of aromatics, are driven off from the solvent, the recovered solvent, which accumulates in the bottom of the stripping column 11, being returned via line 8 to the extractive distillation column 4.
  • the hydrocarbons of the extract freed from the solvent are withdrawn from the stripping column 11 via line 12 or 13 and fed to their further use.
  • the operating conditions in the extractive distillation column 2 are set so that the benzene contained in the feed hydrocarbon mixture largely accumulates in the extract and a low-benzene raffinate is obtained.
  • the benzene contained in the extract is then separated from the other aromatics by distillation and withdrawn as salable pure benzene with a non-aromatics content of ⁇ 1000 ppm as overhead product via line 12, while in this case a practically more or less benzene-free aromatics concentrate as a side stream the line 13 or via a side column arranged at this point and not shown in the flow diagram is removed from the stripping column 11.
  • the distillation residue from the pre-distillation is then added to this aromatic concentrate. This is withdrawn via line 14 from the bottom of column 2 and mixed with the product stream flowing in line 13 so that the end product stream serving as blending component can be withdrawn via line 13.
  • the flow diagram shown in the figure contains only the parts of the system that are absolutely necessary for the explanation of the method according to the invention, while all auxiliary devices which are not directly related to the invention were not shown in the flow diagram. This applies in particular to the heat exchangers for heat exchange between the individual process streams, the circulating cookers for heating the individual columns, the devices for regenerating or supplementing the used solvent, and all measuring and control devices.

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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)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Claims (3)

1. Procédé pour fabriquer un concentrat de composés aromatiques utilisable comme constituant de mélange pour des carburants légers à partir de mélanges d'hydrocarbures qui présentent un point d'ébullition compris entre 40 et 170°C et qui contiennent, à côté de composés non-aromatiques, plusieurs composés aromatiques, tandis que le mélange d'hydrocarbures mis en oeuvre est soumis à une distillation extractive faisant appel, à titre de solvant sélectif, à des morpholines N-substituées, dont les substituants ne présentent pas plus de sept atomes de carbone, et que pratiquement la totalité des composés non-aromatiques d'un bas point d'ébullition, allant jusqu'à environ 105°C, et que la majeure partie des composés non-aromatiques, dont le point d'ébullition plus élevé est compris entre 105 et 160°C environ, sont soutirés, comme produits de raffinage, à la tête de la colonne de distillation extractive, à la suite de quoi le solvant est séparé, par distillation dans une colonne de séparation installée en aval, des autres hydrocarbures restant dans l'extrait et que ces derniers sont mis en oeuvre en tout ou partie à titre de constituant de mélange pour carburants légers, caractérisé par le fait dans le cadre du traitement de mélanges d'hydrocarbures de mise en oeuvre qui contiennent des fractions passant au-dessus de 170°C, le mélange d'hydrocarbures de mise en oeuvre est soumis à une distillation préalable au cours de laquelle on sépare par distillation (dans des conditions normales) les fractions dont le point d'ébullition va jusqu'à 169°C et les affecte à la distillation extractive, tandis que le résidu de la distillation est rajouté au concentré de composés aromatiques servant de constituant de mélange pour carburants légers.
2. Procédé selon la revendication 1, caractérisé par le fait que la distillation préalable est conduite sous une pression accrue, la pression étant chaque fois ajustée de manière telle que la distillation préalable puisse être conduite à une température plus élevée que la distillation extractive, de sorte que les vapeurs des produits de tête recueillies dans la distillation préalable peuvent être utilisées, moyennant condensation complète, pour chauffer la colonne dans la distillation extractive et que le condensat ainsi recueilli est introduit dans la distillation extractive.
3. Procédé suivant les revendications 1 et 2, caractérisé par le fait que l'on travaille, dans la distillation préalable, sous une pression pouvant aller jusqu'à 15 bars.
EP88110072A 1986-04-12 1988-06-24 Procédé de production d'un concentré d'aromatique propre à l'utilisation comme composante de mélange pour essences Expired - Lifetime EP0305668B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT88110072T ATE64609T1 (de) 1987-08-08 1988-06-24 Verfahren zur herstellung eines zur verwendung als blendingskomponente fuer vergaserkraftstoffe geeigneten aromatenkonzentrates.

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19863612384 DE3612384A1 (de) 1986-04-12 1986-04-12 Verfahren zur herstellung eines zur verwendung als blendingkomponente fuer vergaserkraftstoffe geeigneten aromatenkonzentrates
DE19873726449 DE3726449A1 (de) 1986-04-12 1987-08-08 Verfahren zur herstellung eines zur verwendung als blendingkomponente fuer vergaserkraftstoffe geeigneten aromatenkonzentrates
DE3726449 1987-08-08

Publications (2)

Publication Number Publication Date
EP0305668A1 EP0305668A1 (fr) 1989-03-08
EP0305668B1 true EP0305668B1 (fr) 1991-06-19

Family

ID=39361287

Family Applications (2)

Application Number Title Priority Date Filing Date
EP87100581A Expired - Lifetime EP0241638B1 (fr) 1986-04-12 1987-01-17 Procédé de préparation d'un concentré aromatique utilisable comme produit de mélange d'un combustible pour moteurs à carburateur
EP88110072A Expired - Lifetime EP0305668B1 (fr) 1986-04-12 1988-06-24 Procédé de production d'un concentré d'aromatique propre à l'utilisation comme composante de mélange pour essences

Family Applications Before (1)

Application Number Title Priority Date Filing Date
EP87100581A Expired - Lifetime EP0241638B1 (fr) 1986-04-12 1987-01-17 Procédé de préparation d'un concentré aromatique utilisable comme produit de mélange d'un combustible pour moteurs à carburateur

Country Status (11)

Country Link
US (1) US4925535A (fr)
EP (2) EP0241638B1 (fr)
JP (2) JP2550060B2 (fr)
AU (2) AU589508B2 (fr)
DE (2) DE3612384A1 (fr)
DK (2) DK167362B1 (fr)
ES (2) ES2020200B3 (fr)
FI (2) FI85872C (fr)
GR (2) GR3001286T3 (fr)
NO (2) NO169595C (fr)
SG (2) SG20992G (fr)

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3612384A1 (de) * 1986-04-12 1987-10-15 Krupp Koppers Gmbh Verfahren zur herstellung eines zur verwendung als blendingkomponente fuer vergaserkraftstoffe geeigneten aromatenkonzentrates
DE3805383A1 (de) * 1988-02-20 1989-08-31 Krupp Koppers Gmbh Verfahren zur herstellung eines zur verwendung als blendingkomponente fuer vergaserkraftstoffe geeigneten aromatenkonzentrates
DE3942950A1 (de) * 1989-12-23 1991-06-27 Krupp Koppers Gmbh Verfahren zur gleichzeitigen gewinnung von reinem benzol und reinem tuluol
DE4109632A1 (de) * 1991-03-23 1992-09-24 Krupp Koppers Gmbh Verfahren zur abtrennung von aromaten durch extraktivdestillation
WO2009043754A1 (fr) * 2007-09-28 2009-04-09 Basf Se Procédé de production d'hydrocarbures aromatiques à partir d'un mélange d'hydrocarbures
WO2009043753A1 (fr) * 2007-09-28 2009-04-09 Basf Se Procédé de production d'hydrocarbures aromatiques à partir d'un mélange d'hydrocarbures
DE102011001587B4 (de) * 2010-08-05 2016-12-29 Flagsol Gmbh Verfahren zum Aufbereiten eines Wärmeträgermediums eines solarthermischen Kraftwerks
DE102014005337A1 (de) 2014-04-11 2015-10-15 Friedrich-Alexander-Universität Erlangen-Nürnberg Tonoplastidäre Protonen/Zucker-Antiporter-Proteine und deren Verwendung zur Erhöhung der Saccharosekonzentration eines Saccharosespeicherorgans von Pflanzen
US20230183733A1 (en) 2020-05-20 2023-06-15 KWS SAAT SE & Co. KGaA Multiple virus resistance

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1568940A1 (de) * 1966-12-19 1970-07-16 Koppers Gmbh Heinrich Verfahren zur Abtrennung von Aromaten aus Kohlenwasserstoffgemischen beliebigen Aromatengehaltes

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2842484A (en) * 1954-12-30 1958-07-08 Union Oil Co Separation of hydrocarbons
US3216929A (en) * 1961-10-27 1965-11-09 Phillips Petroleum Co Method of making inherently stable jet fuels
IT1043581B (it) * 1974-12-17 1980-02-29 Krupp Koppers Gmbh Processo per l esercizio di impianti di estrazione e o di impianti di estrazione e o di distillazione estrattiva
DE2916175A1 (de) * 1979-04-21 1980-10-23 Krupp Koppers Gmbh Verfahren zur regelung der einer extraktivdestillationskolonne am sumpf zugefuehrten waermemenge
DE3032780A1 (de) * 1980-08-30 1982-04-15 Krupp-Koppers Gmbh, 4300 Essen Verfahren zur aufarbeitung des sumpfproduktes von extraktivdestillationsprozessen zur gewinnung reiner kohlenwasserstoffe
DE3135319A1 (de) * 1981-09-05 1983-03-24 Krupp-Koppers Gmbh, 4300 Essen "verfahren zur gewinnung reiner aromaten"
DE3409030A1 (de) * 1984-03-13 1985-09-19 Krupp Koppers GmbH, 4300 Essen Verfahren zur abtrennung von aromaten aus kohlenwasserstoffgemischen beliebigen aromatengehaltes
DE3409307A1 (de) * 1984-03-14 1985-09-19 Krupp Koppers GmbH, 4300 Essen Verfahren zur abtrennung von aromaten aus kohlenwasserstoffgemischen beliebigen aromatengehaltes
DE3612384A1 (de) * 1986-04-12 1987-10-15 Krupp Koppers Gmbh Verfahren zur herstellung eines zur verwendung als blendingkomponente fuer vergaserkraftstoffe geeigneten aromatenkonzentrates

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1568940A1 (de) * 1966-12-19 1970-07-16 Koppers Gmbh Heinrich Verfahren zur Abtrennung von Aromaten aus Kohlenwasserstoffgemischen beliebigen Aromatengehaltes

Also Published As

Publication number Publication date
NO871545L (no) 1987-10-13
JP2563985B2 (ja) 1996-12-18
AU7139587A (en) 1987-10-15
NO172248B (no) 1993-03-15
DE3726449A1 (de) 1989-02-16
EP0241638A3 (en) 1988-09-14
NO883356L (no) 1989-02-09
FI87657B (fi) 1992-10-30
DK441488D0 (da) 1988-08-05
DK179087D0 (da) 1987-04-08
FI882636A0 (fi) 1988-06-03
DK179087A (da) 1987-10-13
DK167362B1 (da) 1993-10-18
AU589508B2 (en) 1989-10-12
FI870266A0 (fi) 1987-01-21
EP0241638A2 (fr) 1987-10-21
NO883356D0 (no) 1988-07-28
SG20992G (en) 1992-04-16
AU2042788A (en) 1989-02-09
JP2550060B2 (ja) 1996-10-30
JPH0247191A (ja) 1990-02-16
JPS62243685A (ja) 1987-10-24
NO169595B (no) 1992-04-06
FI870266A (fi) 1987-10-13
NO172248C (no) 1993-06-23
FI882636A (fi) 1989-02-09
ES2023231B3 (es) 1992-01-01
US4925535A (en) 1990-05-15
NO169595C (no) 1992-07-15
EP0241638B1 (fr) 1991-01-02
EP0305668A1 (fr) 1989-03-08
ES2020200B3 (es) 1991-08-01
GR3002432T3 (en) 1992-12-30
AU602997B2 (en) 1990-11-01
NO871545D0 (no) 1987-04-13
FI85872C (fi) 1992-06-10
FI87657C (fi) 1993-02-10
FI85872B (fi) 1992-02-28
GR3001286T3 (en) 1992-08-26
SG90092G (en) 1992-12-04
DE3612384A1 (de) 1987-10-15
DK441488A (da) 1989-02-09

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