EP0241638B1 - Procédé de préparation d'un concentré aromatique utilisable comme produit de mélange d'un combustible pour moteurs à carburateur - Google Patents

Procédé de préparation d'un concentré aromatique utilisable comme produit de mélange d'un combustible pour moteurs à carburateur Download PDF

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Publication number
EP0241638B1
EP0241638B1 EP87100581A EP87100581A EP0241638B1 EP 0241638 B1 EP0241638 B1 EP 0241638B1 EP 87100581 A EP87100581 A EP 87100581A EP 87100581 A EP87100581 A EP 87100581A EP 0241638 B1 EP0241638 B1 EP 0241638B1
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EP
European Patent Office
Prior art keywords
aromatics
extractive distillation
column
blending component
benzene
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
EP87100581A
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German (de)
English (en)
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EP0241638A3 (en
EP0241638A2 (fr
Inventor
Gerhard Dr. Dipl.-Chem. Preusser
Gerd Dipl.-Ing. Emmerich
Martin Chem.-Ing. 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
Application filed by Krupp Koppers GmbH filed Critical Krupp Koppers GmbH
Priority to AT87100581T priority Critical patent/ATE59670T1/de
Publication of EP0241638A2 publication Critical patent/EP0241638A2/fr
Publication of EP0241638A3 publication Critical patent/EP0241638A3/de
Application granted granted Critical
Publication of EP0241638B1 publication Critical patent/EP0241638B1/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 the separation of aromatics from these compounds and non-aromatics feed hydrocarbon mixtures with a boiling range between 40 and 170 ° C, the feed hydrocarbon mixture without prior separation into individual fractions of an extractive distillation using N-substituted morpholines, the substituents of which are not have more than seven carbon atoms as a selective solvent.
  • the object of the invention is to obtain an aromatic concentrate suitable for use as a blending component for gasoline fuels from the above-mentioned hydrocarbon mixtures.
  • octane improvers In addition to the increased use of alkylate and polymer spirits, certain alcohols, such as methanol, isopropanol and tert-butanol, and certain ethers, such as methyl tert-butyl ether and amyl ether, are also used as octane improvers. Very often, the required octane number is also set in the gasoline fuel by adding aromatic concentrates, which contain not only a little benzene but especially C7 to C9 aromatics.
  • aromatic concentrates suitable as blending components for gasoline fuels are becoming increasingly important.
  • These aromatic concentrates should not have too high a benzene content. This is sought not only because of the carcinogenic properties of benzene already mentioned, but above all because benzene has a lower octane-improving effect than other aromatics such as toluene.
  • aromatic hydrocarbon mixtures from petroleum processing, such as. B. Reformates and Platformates.
  • hydrocarbon mixtures with a high benzene content such as pyrolysis gasoline or coke oven crude benzene on the other hand, for the reasons described above, it is less suitable for the stated purpose.
  • the aromatics concentrates have hitherto been separated from these feed hydrocarbon mixtures in practice exclusively by liquid-liquid extraction using customary solvents, such as, for example, polyethylene glycol, sulfolane , N-methylpyrrolidone and others.
  • customary solvents such as, for example, polyethylene glycol, sulfolane , N-methylpyrrolidone and others.
  • solvents such as, for example, polyethylene glycol, sulfolane , N-methylpyrrolidone and others.
  • solvents such as, for example, polyethylene glycol, sulfolane , N-methylpyrrolidone and others.
  • counter solvent such as pentane.
  • Liquid-liquid extraction therefore causes not only high operating costs but also high investment costs.
  • an extractive distillation process of the type mentioned is known.
  • this process involves, on the one hand, the extraction of aromatics with the highest possible purity or, on the other hand, the extraction of hydrocarbon mixtures which are said to be largely free of aromatics.
  • the method according to this document is to be used in cases in which both the highest possible purity of the extract (aromatics) obtained is important, and in those cases in which the highest possible purity of the obtained raffinates (paraffins) is important. arrives.
  • a high weight ratio of the feed product to the solvent must be used in this process, which leads to a correspondingly high energy requirement per kg of feed product.
  • 105 and 160 ° C is mainly withdrawn as raffinate overhead from the extractive distillation column, whereupon the solvent is separated from the other hydrocarbons of the extract by distillation in a downstream stripping column and these are used in whole or in part as a blending component.
  • extractive distillation in the process according to the invention avoids the disadvantages of liquid-liquid extraction described above, since on the one hand the solvent used according to the invention is used without any addition of water and on the other hand - as is customary in extractive distillation - relatively simple columns Application. Since it is also possible to work with a very low ratio of starting material to solvent in the range from 1: 2 to 1: 3 when carrying out the process according to the invention, the energy requirement per kg of starting product is correspondingly low.
  • the figure shows a flow diagram of the inventive method in a greatly simplified representation.
  • the feed hydrocarbon mixture used for processing is used without any pre-fractionation introduced via line 1 into the central part of the extractive distillation column 2 provided with internals (trays).
  • the hydrocarbons of the raffinate escape overhead from the extractive distillation column 2 and pass via line 4 into column 5, in which the hydrocarbons of the raffinate are separated from the solvent residues by distillation.
  • the latter pass through line 6 into line 3, through which the solvent used is introduced into the upper part of the extractive distillation column 2.
  • the hydrocarbons of the raffinate freed from the solvent are withdrawn via the head 7 from the column 5 and fed to their further use.
  • the hydrocarbons of the extract are withdrawn together with the majority of the solvents via line 8 from the bottom of the extractive distillation column 2 and from there into the middle part of the stripping column 9, which may also be provided with internals (trays).
  • the hydrocarbons of the extract consisting mainly of aromatics are driven off from the solvent, the recovered solvent, which accumulates in the bottom of the stripping column 9, being returned via line 3 to the extractive distillation column 2.
  • the hydrocarbons of the extract freed from the solvent are withdrawn from the stripping column 9 via the lines 10 and 11 and fed to their further use.
  • the flow diagram shown in the figure contains only those parts of the system which 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.
  • the raffinates obtained when carrying out the process according to the invention can be obtained as so-called.
  • Chemical gasoline for further processing for example, these raffinates can be used as a starting material for ethylene pyrolysis or for isomerization processes.
  • the aromatic concentrates used as a blending component and obtained by the process according to the invention only have a low non-aromatic content of between 0.5 and 5.0% by weight.
  • N-formylmorpholine was used as the selective solvent for the extractive distillation.
  • the extractive distillation column 2 each had 50 trays.
  • the feed hydrocarbon mixture was introduced into the extractive distillation column 2 at a temperature of 70 ° C., and the top temperature of this column was in each case approximately 100 ° C.
  • process example 1 a so-called reformate from petroleum processing with an aromatic content of 65% by weight and an octane number (RON) of 92 was used as the input hydrocarbon mixture, process variant 2 being used.
  • process example 2 a so-called platformat with an aromatic content of 42% by weight and an octane number (RON) of 83 was used as the starting material, process variant 2 again being used.
  • process example 3 the same reformate as in process example 1 was finally used as the starting material. However, this starting material was worked up according to process variant 1.

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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 (4)

1. Procédé pour isoler des aromatiques de mélanges d'hydrocarbures de départ, qui contiennent ces composés et des non-aromatiques et qui possèdent un intervalle d'ébul­lition entre 40 et 170°C, dans lequel le mélange d'hydro­carbures de départ est soumis, sans avoir été préalablement fractionné en fractions distinctes, à une distillation ex­tractive en utilisant comme solvant sélectif des morpholi­nes N-substituées dont les constituants ne comprennent pas plus de sept atomes de carbone, caractérisé par le fait que, pour préparer un concentré d'aromatiques approprié pour être utilisé comme additif pour carburants légers, la distillation extractive est exé­cutée avec de la N-formyl-morpholine comme solvant sélec­tif, en respectant un rapport de 1 : 2 à 1 : 3 entre le produit de départ et le solvant, et dans lequel les non-­aromatiques à bas point d'ébullition, possédant un inter­valle d'ébullition allant jusqu'à environ 105°C sont ex­traits pratiquement totalement et les non-aromatiques à point d'ébullition plus élevé, possédant un intervalle d'é­bullition entre environ 105 et 160°C, sont soutirés en ma­jeure partie de la colonne de distillation extractive en qualité de raffinat, en tête, après quoi le solvant est sé­paré des autres hydrocarbures de l'extrait par une opéra­tion de distillation, dans une colone de rectification pla­cée en aval, et ces autres hydrocarbures sont utilisés en totalité ou en partie comme additifs.
2. Procédé selon la revendication 1, caractérisé par le fait que les concentrés d'aromatiques produits possèdent des teneurs en non-aromatiques de 0,5 à 5,0 % en poids.
3. Procédé selon les revendications 1 et 2, caractérisé par le fait que l'on soutire de la colonne de rectification, en tant que produit de tête, du benzène pur possédant une teneur en non-aromatiques inférieure à 1000 ppm, tandis que les hydrocarbures servant d'additifs sont soutirés de la partie centrale de la colonne de recti­fication en qualité de courant latéral ou par l'intermé­diaire d'une colonne latérale.
4. Procédé selon les revendications 1 à 3, caractérisé par le fait que les conditions de travail dans la colonne de distillation extractive sont réglées de ma­nière qu'une partie du benzol contenu dans le mélange d'hy­drocarbures de départ soit éliminée par distillation, en être de la colonne de distillation extractive, conjointe­ment avec les non-aromatiques, en qualité de raffinat, et par le fait que la fraction de benzol qui reste dans l'ex­trait n'excède pas une valeur maximale désirée, qui est in­férieure à 5 % en poids.
EP87100581A 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 Expired - Lifetime EP0241638B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT87100581T ATE59670T1 (de) 1986-04-12 1987-01-17 Verfahren zur herstellung eines zur verwendung als blendingkomponente 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
DE3612384 1986-04-12
DE19873726449 DE3726449A1 (de) 1986-04-12 1987-08-08 Verfahren zur herstellung eines zur verwendung als blendingkomponente fuer vergaserkraftstoffe geeigneten aromatenkonzentrates

Publications (3)

Publication Number Publication Date
EP0241638A2 EP0241638A2 (fr) 1987-10-21
EP0241638A3 EP0241638A3 (en) 1988-09-14
EP0241638B1 true EP0241638B1 (fr) 1991-01-02

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 After (1)

Application Number Title Priority Date Filing Date
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

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
WO2009043753A1 (fr) * 2007-09-28 2009-04-09 Basf Se Procédé de production d'hydrocarbures aromatiques à partir d'un mélange d'hydrocarbures
CN101808962B (zh) * 2007-09-28 2012-11-28 巴斯夫欧洲公司 从烃混合物中获得芳烃的方法
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
DE1568940C3 (de) * 1966-12-19 1978-12-07 Krupp-Koppers Gmbh, 4300 Essen 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
DE1568940C3 (de) * 1966-12-19 1978-12-07 Krupp-Koppers Gmbh, 4300 Essen Verfahren zur Abtrennung von Aromaten aus Kohlenwasserstoffgemischen beliebigen Aromatengehaltes

Also Published As

Publication number Publication date
AU602997B2 (en) 1990-11-01
ES2020200B3 (es) 1991-08-01
JPS62243685A (ja) 1987-10-24
NO169595C (no) 1992-07-15
AU2042788A (en) 1989-02-09
US4925535A (en) 1990-05-15
AU589508B2 (en) 1989-10-12
FI87657C (fi) 1993-02-10
FI870266A (fi) 1987-10-13
NO883356D0 (no) 1988-07-28
NO169595B (no) 1992-04-06
ES2023231B3 (es) 1992-01-01
EP0241638A3 (en) 1988-09-14
FI85872C (fi) 1992-06-10
DK179087A (da) 1987-10-13
SG90092G (en) 1992-12-04
DK179087D0 (da) 1987-04-08
SG20992G (en) 1992-04-16
NO172248B (no) 1993-03-15
GR3002432T3 (en) 1992-12-30
JP2563985B2 (ja) 1996-12-18
DK441488D0 (da) 1988-08-05
DK167362B1 (da) 1993-10-18
GR3001286T3 (en) 1992-08-26
NO871545D0 (no) 1987-04-13
JP2550060B2 (ja) 1996-10-30
AU7139587A (en) 1987-10-15
JPH0247191A (ja) 1990-02-16
NO871545L (no) 1987-10-13
EP0305668B1 (fr) 1991-06-19
DE3726449A1 (de) 1989-02-16
FI870266A0 (fi) 1987-01-21
DK441488A (da) 1989-02-09
EP0305668A1 (fr) 1989-03-08
FI882636A0 (fi) 1988-06-03
FI882636A (fi) 1989-02-09
FI87657B (fi) 1992-10-30
DE3612384A1 (de) 1987-10-15
NO172248C (no) 1993-06-23
NO883356L (no) 1989-02-09
FI85872B (fi) 1992-02-28
EP0241638A2 (fr) 1987-10-21

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