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Publication numberUS3200165 A
Publication typeGrant
Publication dateAug 10, 1965
Filing dateJul 5, 1962
Priority dateJul 8, 1961
Publication numberUS 3200165 A, US 3200165A, US-A-3200165, US3200165 A, US3200165A
InventorsWirth Hans, Eiseulohr Karl-Heinz, Offenbach Kreis
Original AssigneeMetallgesellschaft Ag
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Recovery of aromatic and olefinic hydrocarbons
US 3200165 A
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Description  (OCR text may contain errors)

g 10, 1955 KARL-HEINZ EISENLOHR ETAL 3,200,165

RECOVERY OF AROMATIC AND OLEFINIC HYDROCARBONS Filed July 5, 1962 h fi II o f? w Q n 53 v A w I T 6H M Q x w N\ & g m I 4 r! Q5; km N L w ATTORNEYS United States Patent 3,2titl,l- REQOVERY @F ARQMATM AND @LEEHNEC HYDR JQARFBQNS Karl-Heinz Eiseniohr, Buchschiag, Kreis Ofienbach (Main), and Hans Wirth, Trostberg, Upper llavaria, Germany, assignors to Metallgesellschait Airtiengesellschalit, Frankfurt am Main, Germany Filed luly 5, M62, Ser. No. M97515 Claims priority, application Germany, duly S, will, M 49,6111 6 Claims. (Cl. 269-674) The present invention relates to a process for recovering pure aromatics, such as benzene, toluene and xylene, from hydrocarbon mixtures, especially gasolines, which contain a considerable proportion of unsaturated compounds by partially hydrogenating the mixture and then extracting the desired components.

More particularly, the invention comprises a process for recovering pure aromatics from cracked gasolines (benzines), gasolines obtained by pressure gasification processes, gasolines recovered from low temperature carbonizations and generally hydrocarbon mixtures which contain a high content of unsaturated compounds besides aromatics. There are a large number of processes by which pure aromatics can be recovered from hydrocarbon mixtures by extraction. However, in these the hydrocarhon mixtures are not introduced since they are passed through a pretreatment in order to make them suitable for the extraction. The pretreatment depends on the properties and source of the starting materials. When products from reforming of petroleum hydrocarbons are employed, it is sufiicient merely to produce the corresponding boiling point out. But when coke plant oeuzine, petroleum gasification benzine, cracked gasolines, etc., are employed, a chemical treatment is necessary. In recent times these crude products are catalytically hydrogenated before further treatment. The hydrogenation of the products suitable for recovery of aromatics occurs under such conditions that all of the unsaturated corripounds are saturated but none of the aromatics are hydrogenated.

A very important source for recovering aromatics are liquid hydrocarbon mixtures which are obtained as byproducts in the pyrolysis of petroleum hydrocarbons in the production of heating gas or lower oiefins. By-products or similar composition also result under certain conditions in the pyrolysis of solid fuels, that is, by low temperature carbonization or gasification under pressure. These hydrocarbon mixtures are distinguished from coke plant benzine which has an aromatic content of 97 to 98% by a lower content of aromatics and a larger proportion of non-aromatic unsaturated constituents.

The technical use of such unsaturated hydrocarbon oils, which can contain 50% or more olefins, causes important dirhculties. They are essentially unsuited for recycling to the cracking because they consist in part of thermally very stable compounds. Their use in oil burners is just as unsuited since they cause fouling of the burner. Their use as a motor fuel is only possible after a costly catalytic hydrogenation and the catalytic hydrogenation is only considered economically feasible when products of higher value, for example, pure aromatics, can be recovered from the hydrogenated rai'finate. However, very much hydrogen is consumed for the hydrogenation due to the high unsaturated hydrocarbon content. Heretofore these disadvantages had to be accepted since economic possibilities for the use of such cracked products were not known.

In known processes it was only possible to extract the aromatics from mixtures which in addition consisted almost solely of saturated non-aromatics. The cracked gasoline which is very interesting for the recovery of "ice aromatics previously could only be subjected to extraction after the unsaturated aliphatic hydrocarbons had been completely hydrogenated.

It is an object of the present invention to provide a process for recovering the aromatics and olefins from these olefin rich hyrocarbon mixtures, wherein the olefins need not be first substantially completely converted into parahins in an additional step of the process, that is, into products which possess little value. Olefins also present a valuable raw product for a difierent synthesis when they are in admixture with parafiins.

Aromatic and olefinic hydrocarbons can be recovered according to the invention from hydrocarbon fractions having a high content of unsaturated compounds, especial- 1y from cracked gasolines and low temperature carbonization gasolines by first removing the polyunsaturated components in a known Way, while to a great extent retaining the olefins, and subsequently extracting the aromatics with a solvent containing a pyrrolidone compound.

The separation or" the diolefins and acetylenic compounds which have a strong tendency to form resins, and which are present in small amounts in the crude product mentioned, by a prehydrogenation under mild conditions, a bleaching earth treatment at elevated temperature or through the influence of a polymerization catalyst is known. Use was made of these type processes especially before the complete hydrogenation of the olefinic compounds since in the presence of these resin forming substances the hydrogenation or the necessary preceding vaporization or heating of the crude product caused difficulties.

It has now been found that this pretreatment for separating the polyunsaturated components while retaining a large mono-olefin content, results in a product from which the pure aromatics can be recovered with the help of a pyrrolidone solvent. Pyrrolidone itself or its derivatives, as, for example, N-allrylpyrrolidone, N-oxyalkylpyrrolidone and lI-acylpyrrolidone which have already been used to separate the aromatics from the paraifins, surprisingly also are suitable for recovering aromatics from mono-olefin rich fractions, insofar as these fractions are substantially freed of polyunsaturated components. Accordingto the process of the invention it is therefore also possible to separate starting materials which no longer contain easily polymerizable resin forming compounds (polyunsaturates) directly to olefin rich and aromatic frac tions.

The pyrrolidones expediently are employed as a mixture with small amounts of water for the extraction according to the invention. A mixture of N-methylpyrrolidone with 15 to 30% water is especially well suited. The selective solvent mixture is added preferably in such amounts that the volume ratio of the aromatics present in the starting mixture to the solvent amounts to 0.2 to 0.005.

The extraction of the aromatics is preferably carried out in a multi-stage counterilow apparatus in which the mixture to be separated is introduced into one of the central stages. The selective solvent is introduced into one end of the counterflow apparatus. The saturated and unsaturated non-aromatics, which flow countercurrent to the selective solvent, leave the extraction apparatus at the same end. The aromatics contained in the starting material are dissolved in the selective solvent and leave the extraction apparatus with this solvent.

Expediently a non-aromatic anti-solvent is introduced at the same end as that where the aromatics and selective solvent leave the extractor, so as to flow through the apparatus countercurrent to the selective solvent. The non-aromatic anti-solvent must be easily separable from the aromatics to be recovered through distillation, and it should only slightly dissolve in the selective solvent.

{B Preferably, a hydrocarbon fraction boiling below 60 C. is employed as the anti-solvent and the volume ratio of aromatics to anti-solvent should be between 1.2 and 0.5. A part of the recovered aromatics can be introduced in the form of an extract recycle together with the antisolvent or in place of it.

The selective solvent is separated from the aromatics by distillation and recycled back into the extraction apparatus for reuse. The anti-solvent, when used, is also separated from the non-aromatics in a separating column and recycled into the extraction process. When an antisolvent is used, the solubility of the aromatic mixture in the solvent in the presence of the anti-solvent should be about to 70%. The extraction can take place at room temperature or also at elevated temperatures as Well as under pressure.

With the process according to the invention a cracked gasoline containing less than 50% aromatics, which in addition consists chiefly of unsaturated hydrocarbons, can be processed to aromatics without trouble. The bromine number of such a mixture is about 80 g./100 g. To refine these products by hydrogenation more than 110 normal cubic meters of hydrogen per 1000 kilograms of charge are used up and it is necessary to employ temperatures of 300 to 400 C. at high pressures, that is, reaction conditions are required which make a hydrogenation apparatus that is very costly necessary. The great heat of the reaction and other phenomena also cause considerable technical difficulties.

According to the invention it was found possible to remove the materials. which disturb the extraction through a pretreatment requiring only a small amount of hydrogen using a mild, pressureless hydrogenation at temperatures below 100 C. in the presence of a noble metal catalyst, whereby the bromine number is lowered only to a value between 20 and 60 g./100 g. Comparatively small amounts of hydrogen are required for this pretreatment. When the pretreatment leaves a product still containing small amounts of polyunsaturates which cannot be separated from the aromatics by the extraction, the extract can undergo a post-treatment with various agents, Such post-treatment in view of the smaller volume of liquid involved and its more uniform composition is simpler than carrying out a complete hydrogenation of the crude product. Such post-treatment can, for example, be carried out with bleaching earth, sulfuric acid or fused alkalies.

The accompanying drawing is a schematic flow diagram of an illustrative embodiment of an extraction process according to the invention.

As shown in the drawing, the starting mixture was fed to a stage extraction column 1 by means of inlet 2. The solvent was supplied at 3. The solvent left the column 1 at 4 together with the aromatics contained in the starting mixture. A hydrocarbon mixture boiling under 50 C., consisting chiefly of peutane, was introduced as an anti-solvent at 5. The peutane flowed countercurrent to the solvent and carried the non-aromatics with it, with which it left the extraction at 6. The solvent enriched with aromatics coming from 4 was carried by way of 7 into the stripper column 8, in which the dissolved aromatics were separated from the solvent which was recycled by way of 9 and 3 into the extraction column 1. The column 8 was heated if necessary with steam supplied at 31. The vapor of aromatics and water, carried with the aromatics, was separated from the stripper column 8 at 10, condensed in cooler 11 and separated in separator 12 into an aqueous and a hydrocarbon phase. The water was again supplied to the solvent recycle in the necessary amounts by way of 13. Excess water left the system at 14. The separated aromatics were carried over line 15 into the indirectly heated distillation column 16. In the upper part of column 16 pure benzene was recovered which left the system at 18. The solvent separated from the extraction still contained small amounts of anti-solvent with which the solvent was in contact. This peutane was distilled off in the head of column 16 and carried by way of 19 after condensation in the cooler 20 over the lines 21 and 5 back into the extraction column. A small residue collected in the base of column 16 and was removed at 30. This residue contained constituents boiling higher then benzene. The principal part of the anti-solvent together with the non-aromatics left the extraction column at 6 and flowed by way of line 22 into the indirectly heated distillation column 23. In its bottom end the small amount of solvent, which was taken along with the nonaromatics, was recovered and returned to the solvent recycle by way of 24 and 3. The peutane distilled off at 25 was condensed in cooler 26 and flowed by way of lines 21 and 5 back into the recycle. The non-aromatics contained in the starting mixture were taken out of column 2 3 at side outlet 27, condensed in cooler 28 and left the system at 29.

The following examples were carried out employing this system.

Example 1 A hydrocarbon mixture, resulting as a by-product from the thermal cracking of petroleum to gaseous olefins, of the following composition served as the starting material for the recovery of benzene:

Percent Benzene 23 Toluene 22 Xylene 8 Higher aromatics 3 Unsaturated non-aromatics 30 Saturated aromatics 14 The product which has a bromine number of 83 g./ 100 g. was first catalytically hydrogenated over a palladium catalyst with 2% palladium on alumina with 98% hydrogen at 50 atmospheres and 50 C. in the liquid phase. The amount of cracked hydrocarbon passed over the catalyst amounted to 1 kg. per liter of catalyst per hour. After the hydrogenation the bromine number was reduced to 30 g./l00 g. A fraction boiling up to C. containing all the benzene and only traces of toluene was removed from this partially hydrogenated cracked hydrocarbon product. Such fraction was extracted in the system schematically illustrated in the drawing employing four times the amount of solvent consisting of 85% N-methylpyrrolidone (NMP) and 15% water. 30 parts peutane were supplied as the anti-solvent per parts of the fraction introduced. A benzene with a crystallization point of 5.5 C. was recovered in 99.5% yield.

Example 2 The same cracked hydrocarbon mixture that was used in Example 1 was employed for recovery of benzene, toluene and xylene. For this purpose it was first hydrogenated with the aid of a nickel catalyst that contained 15% nickel and had been reduced at 350 C. using 98% hydrogen at 50 atmospheres and 70 C. The amount of cracked hydrocarbon passed over the catalyst amounted to 1 kg. per liter of catalyst per hour. The hydrogenation caused the bromine number to decrease to a value of 41 g./ 100 g. By fractionation the constituents boiling below C. were separated and the distillate extracted in a similar system as employed in Example 1 with the same solvent. The amount of solvent was 3.5 times the amount of starting material and the amount of peutane employed was half as large as the mixture introduced. The recovered extract contained small amounts of polyunsaturated hydrocarbons. These were removed by treatment with bleaching earth at 200 C. under pressure. A pure benzene with a crystallization point of 5.5 C. in approximately quantitative yield was obtained from the thus treated extract. The recovered toluene and xylene were 99.8 to 99.9% pure and thus very highly pure.

We claim:

1. In an extraction process for preparing a very pure aromatic hydrocarbon fraction from a hydrocarbon mixture containing a large proportion of poly-unsaturated hydrocarbons, the steps comprising in combination sub jecting the mixture to selective hydrogenation at a temperature below 100 C. in the presence of a noble metal catalyst and hydrogen under mild hydrogenation conditions to yield a mixture consisting of mono-olefins and aromatics and thereafter extracting the aromatics by contacting the resulting mixture with a selective solvent consisting essentially of a major proportion of N-rnethyl pyrrolidone and a minor proportion of water, removing said selective solvent with said aromatics dissolved therein and recovering the aromatics to yield an aromatic hydrocarbon fraction which is at least 99.8% pure.

2. The process of claim 1 wherein said selective solvent comprises a mixture of N-methyl pyrrolidone and to 30% by weight water.

3. The process of claim 1 wherein an anti-solvent comprising a hydrocarbon fraction boiling below 60 C. is also employed in the extraction process.

t. The process of claim 1 wherein the volume ratio of said aromatics to said solvent is 0.2 to 0.05.

5. The process of claim 1 wherein an anti-solvent comprising a hydrocarbon fraction boiling below 60 C. is also employed in the extraction process, the volume ratio of said aromatics to the anti-solvent being 1.2 to 0.5.

6. In a process for preparing very pure benzene from hydrocarbon mixtures containing a large proportion of poly-unsaturated hydrocarbons, the steps comprising in combination subjecting the mixture to selective hydrogenation at a temperature of about C. in the presence of a palladium catalyst and hydrogen under mild hydrogenation conditions to yield a mixture consisting of monoolefins and aromatics, separating the hydrocarbons which boil below 90 C. from the resulting mixture and contacting these hydrocarbons which boil below 90 C. with a selective solvent consisting essentially of N-methyl pyrrolidone and about 15 to 30% water and an anti-solvent consisting essentially of a hydrocarbon fraction boiling below C., removing said selective solvent with benzene dissolved therein and recovering the benzene to yield benzene which is at least 99.8% pure and has a crystallization point of 5.5 C.

References Cited by the Examiner UNITED STATES PATENTS 2,737,538 3/56 Nelson 260-674 2,753,381 7/56 Nelson 260-674 2,799,627 7/57 Haensel 260-674 2,849,396 8/58 Nelson 208-326 X 2,870,226 1/59 Deanesly 20896 2,933,448 4/60 Morin et al 208-326 X 2,943,122 6/60 Templeman et al 260674 3,082,271 3/63 Weitz et al 208-326 X FOREIGN PATENTS 565,312 10/58 Canada. 812,114 4/59 Great Britain.

DELBERT E. GANTZ, Primary Examiner. ALPHONSO D. SULLIVAN, Examiner.

Patent Citations
Cited PatentFiling datePublication dateApplicantTitle
US2737538 *Jul 24, 1952Mar 6, 1956Phillips Petroleum Co2-pyrrolidone as a selective solvent for aromatic hydrocarbons
US2753381 *Dec 18, 1953Jul 3, 1956Phillips Petroleum CoNu-acyl pyrrolidines as selective solvents
US2799627 *Aug 17, 1953Jul 16, 1957Universal Oil Prod CoProcess for obtaining concentrated aromatic hydrocarbons
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US2870226 *Mar 19, 1956Jan 20, 1959Universal Oil Prod CoProduction and recovery of aromatic hydrocarbons
US2933448 *Dec 6, 1954Apr 19, 1960Ohio Oil CompanySeparation of aromatic hydrocarbons from non-aromatic hydrocarbons utilizing a lactam-water solvent
US2943122 *Jun 19, 1957Jun 28, 1960Ohio Oil CompanyFractionation of mixtures of aromatic compounds utilizing gamma lactum solvents
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CA565312A *Oct 28, 1958Exxon Research Engineering CoPreparation of olefinic-aromatic feeds for solvent extraction
GB812114A * Title not available
Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US3347948 *Apr 21, 1964Oct 17, 1967Ici LtdHydrocarbon separation process
US3422163 *Oct 21, 1965Jan 14, 1969Universal Oil Prod CoRecovery of aromatics from multiple hydrocarbon streams
US3434936 *Dec 18, 1967Mar 25, 1969Koppers Gmbh HeinrichMethod of separating aromatic compounds from hydrocarbon mixtures containing the same by extractive distillation with an n-substituted morpholine
US3437585 *Dec 28, 1967Apr 8, 1969Universal Oil Prod CoOlefin production and subsequent recovery
US4571442 *Sep 19, 1984Feb 18, 1986Institut Francais Du PetroleCatalyst of dalladium on alumina
US7270737Nov 13, 2003Sep 18, 2007Institut Francais Du PetroleProcess for desulfurization comprising a stage for selective hydrogenation of diolefins and a stage for extraction of sulfur-containing compounds
DE1645809C3 *Dec 22, 1967Jul 12, 1973Texaco Development CorpVerfahren zum Raffinieren von Schmieroel
Classifications
U.S. Classification585/259, 585/264, 208/325, 585/840, 585/808, 208/96, 585/865
International ClassificationC07C15/00, C10G67/04
Cooperative ClassificationC07C15/00, C10G2400/30
European ClassificationC07C15/00