US2840511A

US2840511A - Process of extraction with 2-oxazolidone solvents

Info

Publication number: US2840511A
Application number: US520924A
Authority: US
Inventors: Paul N Rylander; Jr William A Junk
Original assignee: Standard Oil Co
Current assignee: Standard Oil Co
Priority date: 1955-07-08
Filing date: 1955-07-08
Publication date: 1958-06-24
Anticipated expiration: 1975-06-24

Description

United States Patent PROCESS OF EXTRACTION WITH Z-GXAZOLIDONE SOLVENTS No Drawing. Application July Serial No. 520,924

-16 Claims. (Cl. 196--14.27)

This invention relates to a process for the separation of mixtures of hydrocarbons into fractions of diverse structural type by selective solvent extraction with specified S-mernbered ring compounds of the 2-oxazolidone series. In one particular aspect this invention is concerned with separation of aromatic hydrocarbons from mixtures thereof with aliphatic hydrocarbons. Such mixtures of hydrocarbons may be commercially produced as processed or unprocessed petroleum oils or mineral oils, coal tar oils, shale oils and the like. The production of highly aromatic extracts from such mixtures is commercially desirable to produce benzene, toluene, xylene, and mixtures thereof, or higher molecular weight aromatics for use as solvents; plasticizers, components of aviation gasoline and as stocks for sulfonation and manufacture into water-soluble, detergents. Dearomatization of hydrocarbon mixtures may be desired in order to prepare hydrocarbon stocks for thermal or catalytic cracking, for

hydrogenation operations, for use as heater oils or for other purposes.

With the commercial development of new processes for producing aromatic hydrocarbons boiling within the gasoline boiling range by cyclization-dehydrogenation of paraffinic hydrocarbons and by the dehydrogenation of cycloalkanes, there has come an increased demand for processes to separate and concentrate the aromatichydrocarbons thus produced. Thus with the commercial development of such processes as hydroforming, platinum catalyst reforming of naphthas, and the like, a tremendous potential has been created for the production of nitration-grade aromatics such as benzene, toluene and xylenes for use by both the petroleum and chemical industries.

The use of solvent extraction for the separation of mix-' 'tures of hydrocarbons has long been known. This method, of purifying hydrocarbon mixtures takes advantage of the differences in solubility of various hydrocarbon types in solvents or mixtures of solvents. Such hydrocarbon types may be conveniently designated by the ratio of hydrogen to carbon atoms in the compound. Thus for hydrocarbons of approximately equal molecular weight, i. e. equal carbon content, the H/ C ratio will vary from a high value for the paraffinic compounds to a low value for the aromatic hydrocarbon compounds. For example, the H/C ratio may be calculated for compounds containing 8 carbon atoms, and is found to vary from 2.25 for paraflEinic hydrocarbons to 1.25 for unsubstituted aromatic hydrocarbons, with intermediate values of 1.50 for cyclic dienes, 1.75 for open-chain dienes and alicyclic mono-olefins and 2.00 for cycloparaffins and open-chain mono-olefins. The solubility of such hydrocarbon types is roughly related to the hydrogen-carbon ratio, and for polar solvents the solubility has been found to increase as the H/C ratio decreases.

Numerous solvents have been proposed to efiect the separation of mixtures of such diverse hydrocarbon types having similar boiling points by extractive processes. For example, aromatic hydrocarbonscan be separated from parafiinic hydrocarbons by extraction with a numice her of well known solvents. Saunders, Industrial and Engineering Chemistry, 43, 121, (1951) has reported his study of many such solvents and has recommended several nitrile's such as beta,beta'-oxydipropionitrile for the separation of aromatics and non-aromatics. Wilkes, U. 8. Patent No. 2,439,534 has proposed nine solvents of the some class, that is, nitriles.

It is an object of our invention to provide a process for the selective extraction of hydrocarbon mixtures with a solvent selected from the group comprising l-oxazolidone and certain of its N-substituted derivatives as hereinafter described. A further object of.our invention is to provide the art with certain novel solvents forjthe extraction of hydrocarbon mixtures. Another object is to provide a method for separating hydrocarbon mixtures into fractions of diverse structure type. object of our invention is to provide a process for the concentration and purification of aromatic hydrocarbons by solvent extraction with 2-oxazolidone and certain of its N-substituted derivatives. Yet another object is to provide a process for the separation of close boiling or azeotropic mixtures of hydrocarbons. A further object is to provide a solvent extraction process for the separation of aromatic hydrocarbons from mixtures thereof with olefinic hydrocarbons. An additional object is to provide a process for refining hydrocarbon oils by extraction with a novel class of solvents as herein described. A further object is to provide a process for the separation of hydrocarbon mixtures by extractive distillation with liquid solvents comprising 2-oxazolidone or certain of its N-substituted derivatives. These and other objects of our invention will become apparent from the ensuing description thereof.

The novel solvents which are employed in the process of our invention comprise 5-membered ring compounds of the 2-oxazolidone series. These compounds have the general formula R H2CI I 0:0 H2CC/ in which R is selected from the group consisting of hydrogen, methyl and hydroxyethyl. The parent compound of the series, 2-oxazolidone, as Well as the aforementioned N-substituted derivativesare Water-soluble, high boiling They are colorless, odorless 'and'neutral compounds of substantial stability both to chemical reagents and to pyrolysis. They are readily prepared by the reaction of a beta-amino alcohol and an alkyl carbonate e. g. as described in U. S. Patent No. 2,399,118 of A. H. Homeyer. Although the aforementioned hydroxyethyl derivative may be either the N-(a-hydroxyethyl)-2-oxazolidone or the B-hydroxyethyl isomer, the latter was chosen to illustrate the process of our invention because of the ease of preparation thereof from the readily available diethanolamine.

The 2-oxazolidone selective solvents or our invention are useful for the separation of monocyclic aromatic hydrocarbons, such as benzene, toluene, xylenes or the like, from mixtures containing the same. The solvents may also be used for the separation of polycyclic'a'romatic hydrocarbons such as naphthalene, methylnaphthalene, tetralin and the like from mixtures containing the same. 'They are effective in separating an aromatic fraction from a mixture containing more than one aromatic compound, and their effectiveness is not limited by the concentration of aromatic hydrocarbons in the mixture treated. Such mixtures containing aromatics are obtained commercially in a variety of Ways. Among them may be mentioned the alkylation of aromatics, the catalytic cracking of gaso- A still further of coal, the aromatization of selected petroleum hydrocarbon fraction and the like. In general such mixtures are in the gasoline boiling range, and consist of hydrocarbon mixtures having a molecular weight range of 72 to 200. The 2 -0xazolidone solvents of this invention may be employed in aqueous solution or in conjunction with various f other diluents which will affect their solvent power for aromatics. Such diluents are partially or completely miscible with water, and generally contain hydroxy groups, although thisis not a limitation. Such diluents maybe effective in modifying the solvency, while avoidingthe corrosivity characteristic of water. Among the diluents may be mentioned. glycerol, ethylene glycol, diethyle'ne g'lycol, 'pentaerythritol, formic acid, lactic acidQethanolamines. suchas mono-, di-, and tri-ethanolamine name like. Certain of these diluents may be more advantageous than water since long continued contact or water with the oxazolidone solvents c'ancause partial hydrolysis. For this reason formic acid and bases such as ethanolamines may be less efficient. Other examples of diluents which may be mentioned are liquid sulfur dioxide, the sulfolanes, dimethyl sulfoxide, dimethyl sulfone, methyl ethyl sulfone, various nitriles such as acetonitrile, bis-2cyanoethylether and the like; others or glycol ethers, tetrahydrofuran and the like; betabeta-oxydipropionitrile, beta, beta'-thiadipropionitrile and the like; halogenated hydrocarbon solvents; esters of monocarboxylicacids and dicarboxylic acids; neutral organic nitrogencompounds such as dimethyl formamide, dimethyl hydantoin and the like; ketones such assacetone, methyl ethyl ketone, methyl isobutyl ketone and the like; aldehydes forv example furfuraldehyde, crotonaldehyde and the like; compounds such as N- methylpyridone, gamma-butyrolactone, gammaebutyrolactam, ethylene carbonate, etc. When a diluent or corsolventlsuch as We have described is used, we prefer to use. from about 0.1 to about 20% by volume thereof ,based onthe volume of oxazolidone solvent employed.

In addition to the co-solvents or diluents described above, anti-solvents can also be used to aid in the exrivative thereof. A liquid extract phase is produced which contains the more aromatic portion of the feedstock as well as any polar impurities derived from the feedstock, for example, organic compounds of oxygen, nitrogen or sulfur. Separation of the resultant layers, for example by decantation, is followed by removal of the solvent from the separated layers by suitable means, as by dilution with water. It is thus possible to recover from the extract phase and from the raflinate phase hydrocarbons of similar boiling point, but of different physical characteristics and chemical composition as characterized, for example, by different H/C ratios.

In carrying out the process of our invention we can use temperatures in the range of about 0 C. or even less to about 200 C. Economic considerations indicate the use of temperatures of about 35 C. to about 80 C. whenever this temperature range is technically feasible. Suflicient pressure is maintained within the extraction zone to prevent substantial volatilization of the hydrocarbon charging stock or solvent under the liquidliquid extraction conditions, and it is obvious that pressure and temperature are related variables in the extraction process. Usually pressures within the range of about 0 to about 100 p. s. i. g. are sufficient, it being appreciated thatthe particular pressure which is required in a given case can readily be determined by experiment.

This invention is illustrated by experimental extraction data obtained on a toluene-n-heptane feedstock by the use of 2-oxazolidone or its N-substituted derivatives, alone or with a diluent. All of these were single stage batch operations which were effected at the indicated temperatures. A feedstock of volume percent nheptane-SO volume percent toluene was contacted with an equal volume of solvent until equilibrium was established; the phases were then separated and the hydrocarbons were recovered from both phases by Washing out the solvent with water. The ,B-value or separation factor in the table is the molar ratio of toluene to heptane in the extract divided by the ratio of these components in the raflinate, and corresponds to alpha, the separation factor calculated in fractional distillation processes.

TABLE I EXTRACTION 0F n-HEP'IANE-TOLUENE MIXTURES Mol Fraction Toluene Extract Vol. per- Exarnple Solvent Temp., 5 Yield, cent of O. Value Vol. Toluene Feed Extract Raflinate percent Extracted 2-Oxazolid0ne 100 580 940 511 15. 0 13. 0 26. 0 N-Methyl-2-Oxazolidone 25 .580 850 353 10. 4 24. 5 42. 6 N-Methyl-2- Oxazoltdone, 25 580 913 570 13. 0 l4. 7 25. 9

10 vol. percent H10. N 8 Hydroxy ethyl) 100 580 .916 476 12.0 8. 1 15.0

2-Oxazolldone.

traction step. Suitable anti-solvents such as saturated hydrocarbons, perfluorocarbons, perfluoroamines, perfiuoroethers and the like may be used in proportions of about 10 toabout 100 volumepercent of the feedstock treated, and may be added to the feedstock to .be dearomatized or introduced directly into the extraction zone.

In conducting the extraction we prefer to use an amount of solvent sufficient to form a twophasesystern, and preferably from about 1 to about 20 volumes of solvent per volume of the hydrocarbon feed to be treated. In the practice of the;invention either continuous, semicontinuous, or batch operation may be employed. Known types of solvent extraction or extractive distillation equipment can be, used.

In accordance with our invention, we first contact the hydrocarbon feed mixture either as liquidv or vapor with arsuitable proportionof the liquid 2-oxazolidone' or de- Example 5 A feed having the composition 50 volume percent toluene-50% octene-Z was subjected to single-batch extraction with an equal volume of2-oxazolidone at C. This operation yielded 22.2 volume percent, based on feed, of extract hydrocarbons containing 82.7 volume percent toluene, corresponding to 36.7 volume percent toluene extraction from the feedstock. The selectivity factor, B, was 6.8.

Example 6 The following is an example of the use of an auxiliary solvent with 2-oxazoli-ilone. The solvent consisted of 50 weight percent of .Z-oxazolidone and 50' weight percent diethylene glycol. A feed having the. composition 50 volume percent toluene-50 volume percent nheptane was subjected to one stage batch-extraction with an equalvolume of the mixed solvent at 100 CL, This operation yielded 106 volume percent, based on feed,

of, extract hydrocarbons containing 94.0 volume percent toluene corresponding to volume percent toluene extraction from the feedstock. The selectivity'factor, 13, I

was 13.3. In general, diethylene glycol: 2-oxazolidone molar ratios of about 0.25 to about 4 may be employed in extraction. 1

While the process of the present invention has been illustrated by examples in which the hydrocarbon mixture and the selective solvent are employed as liquids, it should be understood that the solvent may be charged as a liquid and the feedstock may be charged to the process as vapor, as in extractive distillation. In extractive distillation of naphthas, the temperature should be between the dew point of the hydrocarbon mixtures and about 240 C. and contacting of the liquid solvent and feed vapors is usually countercurrent. In Table H, data are supplied to show the etfect of 2-oxazolidone as an extractive distillation solvent. These data were obtained byboiling a system of known composition, namely 50 volume percent toluene50 volume percent of n-heptane with the solvent in the proportions indicated in the table at total reflux until equilibrium was attained, and analysis of a small sample of condensed vapor by refractive index after removing the solvent by water washing. Also included in the table are data for phenol, a solvent which is widely used in commercial installations for extractive distillation processes in which aromatic concentrates are produced. In this table the selectivity factor, alpha, is defined as 0: Mol Fraction Toluene Mol Fraction n-Heptane new,

M01 Fraction n-Heptaue Mol Fraction Toluene The data above show that 2-oxazolidoneis highly etfective in the separation of aromatics from paraflins by extractive distillation, as indicated by the high value of alpha obtained with this solvent. It may be further noted that at approximately equal solvent concentration, the 2- oxazolidone solvent is superior to the commercially used phenol solvent.

The present process may also be applied to the refining of various hydrocarbon oil fractions derived from petroleum coal, shale, etc. In the refining of such fractions the present refining agents serve not only to effect selective extraction of aromatic hydrocarbons but also to remove sulfur compounds, oxygen compounds and nitrogen compounds. It should be understood that the above specific examples of feedstocks which may be refined in accordance with the present invention are illustrative only and are not intended to delimit the field of applicability of the process of the present invention.

The present invention can be carried out in batch, continuous or semi-continuous operating cycles and in one or more actual or theoretical stages, employing contacting and separation of equipment such .as hasheretofore been employed in selective solvent refining of petroleum stocks. Various types of liquid-liquid extraction operations and suitable extraction equipment are well known in the art and it should be understood that the-specific .equiprnent 'employed forms no part of the present invenwherein R is selected from the group consisting of hydrogen, methyl and hydroxyethyl.

2. A process for the selective extraction of an aromatic hydrocarbon from a mixture of aromatic and aliphatic hydrocarbons, which process comprises contacting said mixture with a liquid 2-oxazolidone compound having the formula i H2 C-N wherein R is selected from the group consisting of hydrogen, methyl and hydroxyethyl, and separating an extract phase comprising essentially said 2-oxazolidone compound and said aromatic hydrocarbon.

3. The process of claim 2 wherein said compound is 2-oxazolidone. 1

4. The process of claim 2 wherein said compound is N-methyl-Z-oxazolidone.

5. The process of claim 2 wherein said compound is an N-hydroxyethyl-Z-oxazolidone.

6. The process of claim 2 wherein said 2-oxazolidone compound contains from about 1 to about 20 percent by volume of water.

7. A process for the extraction of an aromatic hydrocarbon from a mixture containing aromatic and aliphatic hydrocarbons, which process comprises contacting each volume of said mixture in the liquid'phase with from about 0.5 volumes to about 50 volumes of a liquid 2- oxazolidone compound having the formula at a temperature of from about 0 C. to about C.11

and at a pressure sufiicient to maintain liquid phase ex traction conditions, and separating a rafiinate phase and an extract phase compnisingessemiallysaid 2-oxazolidone which said: aromatic hy- W drocarbon is toluene.

11. Theprocess of claim 7 wherein said 2-oxazolidone compoundcontains'from about 1 to about 20 percent by volume of water. a

12. A process for the refining of hydrocarbon oils which comprises contacting said oils with a liquid 2-oxazolidone compound having the formula H2CN HzC-O wherein R is selected from the group consisting of hydrogen, methyl and hydroxyethyl, and separating liquid raffinate and extract phases. 7

13. A process for the extractive distillation of a naphtha containing aromatic hydrocarbons, which process comprises contacting the vapors of said naphtha at a temperatune above its dew point but below about 2.40 with a liquid 2-oxaz olidonecompound having the formula HzC-N V a a 0:0,

HzO-O wherein R is selected from the group consisting of hydrogen, methyl and hydroxymethyl, and separating an extract 'phas e comprising essentially said 2-0xazolidone compound and said aromatic hydrocarbons.

14. The process of claim 13 wherein said compound is 2-oxazolidonev 15. The process of claim 13 wherein said compound is N-rnethyl-Z-oxazolidone.

16. The process of claim 13 wherein said compound is V an N-hydroxyethyl-Z-oxazolidone.

References Cited in the file of this patent Badertscher et a] Sept. 7, 1954

Claims

1. A PROCESS FOR SELECTIVELY SEPARATING A HYDROCARBON FROM A MIXTURE OF HYDROCARBONS OF DIVERSE STRUCTURAL TYPE WHICH PROCESS COMPRISES SELECTIVELY EXTRACTING SAID MIXTURE WITH A LIQUID 2-OXAZOLIDONE COMPOUND HAVING THE FORMULA