US2265220A

US2265220A - Process for recovering toluene

Info

Publication number: US2265220A
Application number: US366675A
Authority: US
Inventors: Jr Frederick W Sullivan
Original assignee: Barrett Co Inc
Current assignee: Barrett Co Inc
Priority date: 1940-11-22
Filing date: 1940-11-22
Publication date: 1941-12-09
Anticipated expiration: 1958-12-09

Description

Dec. 9, 1941. F. w. SULLIVAN, JR 2,265,220

PROCESS FOR RECOVERING TOLUENE Filed NOV. 22, 1940 MMM ATTORNEY hydrocarbons.

atented Dec. 9, 1941 PROCESS FOR RECOVERING TOLUENE Frederick w. Sullivan, Jr., Westfield, N. J., as. signor to The Barrett Company, New York, N. Y., a corporation of New Jersey Application November 22, 1940, Serial No. 366,675

7 Claims.

This invention relates to a process for recovering toluene from hydrocarbon mixtures containlng toluene and like-boiling, non-aromatic hydrocarbons.

Numerous hydrocarbon oils are known which contain toluene and like-boiling, non-aromatic For example, catalytic treatment of a suitable petroleum fraction in the presence of hydrogen gives an oil consisting chiefly of hydrocarbons of both aromatic and non-aromatic character, and containing about 20% toluene. Gasoline fractions obtained by the distillation of certain types of petroleum frequently contain substantial proportions of toluene, although mainly consisting of other hydrocarbons. Oils of petroleum origin having a considerable content of aromatics, including toluene, may be treated by well known selective solvent processes to produce fractions rich in aromatics; for example, extraction of suitable fractions of such petroleum oils with sulfur dioxide may yield fractions of high toluene content. In such cases toluene is accompanied by non-aromatic oils which may be largely parafnic, naphthenic or olenic in character. A considerable portion of these oils cannot be completely separated from the toluene by direct fractional distillation because of the closeness of their boilingpoints to that of toluene or because they form constant boiling mixtures With toluene. Furthermore, while ordinarily toluene is readily separable by direct fractional distillation from light oils produced by the gasification of coal, in some cases the toluene is accompanied by dicultly separable non-aromatic oils 'of the same general character as described, owing to carbonization conditions, type of coal used or other special circumstances. Also synthetic hydrocarbon gas mixtures produced by various catalytic processes may contain toluene which, when recovered, is accompanied by similar dillcultly separable constituents.

By fractional distillation of these oils containing toluene, fractions relatively high in toluene content may be obtained. These toluene fractions, however, will still contain substantial amounts of .the other constituents of the oil having boiling points in the neighborhood of the boiling point of toluene or forming mixtures of constant boiling points in the range of temperatures at which toluene distills from the oil. vThe separation of the toluene from materials distilling from the toluene oil fraction at tempera.- tures substantially higher or lower than the toluene does not present any great technical dlfene from an oil fraction containing it, such as those referred to above, is presented by the problem of separating the toluene -from the like-boiling, non-aromatic hydrocarbons; i. e., from those hydrocarbons which by direct fractional distillation processes as commonly operated for the fractional distillation of oils, distill from the toluene fraction within the same temperature range as the toluene distills therefrom.

` A process has been developed whereby toluene of any desired purity up to substantially 100% toluene may be successfully recovered from oils separate from the like-boiling, non-aromatic hydrocarbons. 'I'hat process involves the azeotropic distillation of the toluene fraction with fractionation of the vapors of toluene and other hydrocarbons in the presence of a material forming low-boiling azeotropes with the toluene and with the accompanying like-boiling, non-aromatic hydrocarbons. Although the toluene and like-boiling, non-aromatic hydrocarbons distill from mixtures containing the same in the same temperature ranges, their azeotropes with materials such as methanol, ethanol, the propanols, acetic acid, pyridine, and the numerous other materials which form low-boiling azeotropes with toluene, have suiciently different. boiling temperatures for these azeotropes to be separated by fractionation. Accordingly, by azeotropic distillation of toluene fractions in the presence of azeotropic agents such as those mentioned, the toluene may be separated from like-boiling, non-aromatic hydrocarbons, the latter being distilled off as azeo.

tropes. Since materials contained in toluene fractions distilling therefrom below or above the toluene distillation range may be readily separated from the toluene by ordinary fractional distillation, this process employing azeotropic distillation provides a method whereby the diflicultly separable like-boiling, non-aromatic hydrocarbons may be separated from the toluene and a toluene of desired purity obtained.

An important factor in the successful azeo'- tropic distillation of toluene fractions is the provision of an azeotropic agent which sharply separates the toluene and the like-boiling, non-aromatic hydrocarbons so that-a high yield of toluene of a desired purity may be obtained in distilling the toluene fraction. It is also highly desirable that the azeotropic agent have a high capacity for carrying over as distillate the nonaromatic hydrocarbons; i. e., that the agents form with those hydrocarbons azetropes having a high ratio of hydrocarbons to azeotropic agent. Ac-

culties. The diiculty in recovering pure tolucordingly, it is an object of this invention to protaining like-boiling, non-aromatic hydrocarbons in the presence of crotonaldehyde. I t appears crotonaldehyde forms a low-boiling azeotrope with the toluene. HoweverI` have discovered crotonaldehyde forms with thenon-aromatic hydrocarbons low-boiling azeotropes which mai,r be

separated by fractional distillation fromthe toluene or any azeotrope containingtoluene and crotonaldehyde which may be formed. Thereis` a relatively wide spread between the boiling points 'of the azeotropes of the like-boiling, nonaromatichydrocarbons and of toluene or any azeotropes of tolueneand crotonaldehyde which facilitates the separation of these materials by fractional distillation. In addition, the ratio of hydrocarbons to crotonaldehyde'in the azeotropes formed with these non-aromatic hydrocarbons is relatively high. These characteristics of the crotonaldehydev contribute materially to its effectiveness as an azeotropic agent in the distillation of toluene oil fractions.

The toluene fraction treated in accordance with fmyinvention preferably will contain little, if any, hydrocarbons distilling from the hydrocarbon-toluene fraction at temperatures materially above those at which toluene distills therefrom. On the other hand, high boiling materials may be left with the toluene residue at the vconclusion of the azeotropic distillation of the toluene fraction under the conditions set forth above to separate the toluene from the hydrocarbons of similar boiling range. Once this separation has been effected,` the toluene may be separated lfrom the high boiling hydrocarbons by fractional distillation in the absence of an azeotropic agent. Whether or not high boiling constituents should be left in the toluene fraction to be azeotropically distilled or whether` if left in the toluene fraction, they will remain in the residue after azeotropic distillation, depends upon a number of factors, among which their boiling range and chemical characteristics are important. If the constituents form azeotropes with the agent used .which have boiling points close to 102 to 103 C., it is preferable to separate themby a direct fractional distillation before azeotropically distilling the toluene fraction. If they do not form azeotropes having boilingl points close to 102'to 103 C., or if their amount is small, this procedure is not so important.

When pure toluene is to be recovered it is preferred the toluene fraction subjected to azeotropic distillation in accordance with my invention be a fraction boiling in the range of 100 C. to 111 C. Such a fraction may be azeotropcally distilled by my process and pure toluene obtained with a relatively small quantity of azeotropic agent present during the distillation. Pure toluene may be obtained by distilling with an azeotropic agent a toluene fraction boiling, for example, from 95 C. to 118 C. but the quantity of azeotropic agent present in the distillation of the toluene fraction of wider boiling range must be substantially increased as compared with the quantity which suffices for distilling the fraction of the narrower boiling range.

Toluene of high purity is desired for nitration purposes and the process of my invention provides a method whereby such pure nitration grade toluene may be economically recovered from toluene oils. The invention, however, is not limited thereto. Toluene products of lower purity than nitration :gradeA toluene are industrially used for various purposes, vre. g.; products containing 85% to 90% toluene are used as solvents. The process of my invention may be used advantageously for recovering such products from hydrocarbon oils of lower toluene content. My process is particularly advantageous when the 'toluene is` to be separated from most of the likeboiling, non-aromatic hydrocarbons present in an oil fraction together with toluene, e. g., when a product is to be obtained containing toluene and no more than 5 parts by weight of like-boiling, non-aromatic hydrocarbons for every parts by weight of toluene. Y u

My invention will be more particularlyI described and illustrated by the following example of a process for the azeotropicv distillation of a toluene fraction iny the presence of crotonaldehyde.

The apparatus used for carrying out the process of this'example, diagrammatically illustrated in the accompanying drawing, comprised a still I with heater 2 and rectification column 3 of conventional design, the rectication column containing sufcient liquid-vapor contact elements for it to effectively fractionate the vapors evolved in the'vstill and passed therefrom through the rectification-column. A condenser 4 was provided to which the vapors from the top of the column were led and in which they were cooled and condensed. A pipe 5 was providedforreturning condensate from the condenser'to the top of the rectification column to serve as reflux for the column. A second pipe 6 was also provided for drawing ofl from the condenser a portion of the condensate formed therein and introducing it into a separator l. Separator I is provided with a pipe 8 through which water may be introduced to the separator. The separator is also provided with a pipe 9 for withdrawal of an upper liquid layer and a pipe I0 for withdrawal of a lower liquid layer which may be formed from the material treated in the separator. Suitable baffles may be provided in separator I to facilitate continuous separation therein. Pipe I0 leads to a storage Vessel II. Pipes I2 and I4 are provided for the introduction of liquids into still I. A pipe I5 serves for withdrawal of residue from this still. y

The above-described apparatus was employed for the treatment of a toluene fraction recovered from the product obtained by the catalytic reformation in the presence of hydrogen of a petroleum oil. This toluene fraction had the following characteristics:

Toluene content per cent 74.5 Boiling range degrees C 1095-1108 The toluene content of this oil was determined by the specific dispersion method for analyzing hydrocarbon oils described in Industrial and Engineering Chemistry, Analytical Edition, vol. 1l, page 614, November 15, 1939.

volumes of the above toluene fraction and 60 volumes of a crude crotonaldehyde product available in the market were charged into the still of the apparatus described above. This crude crotonaldehyde was a material boiling over the range 82.5 C. to 112 C. It contained substantially 90% or more crotonaldehyde and upwardly to water with small amounts of other impurities. The charge of crotonaldehyde and toluene fraction was boiled in the still and the vapors passing therefrom to the fractionating column were rectiiied in this column. The vapors leaving the top of the column were condensed, a part of the condensate withdrawn as distillate, and the remainder of the condensate returned as reux to the top of the fractionation column. Distillation started with the temperature of the vapors at the top of the fractionation column at-about 96 C. This vapor temperature rose as the distillation proceeded to about 102.5" C. During the initial stage of the distillation the oil recovered from the distillate by washing it with water inA separator 1 and separating theoil layer thus obtained from the aqueous layer containing the crotonaldehyde censisted of nonaromatic hydrocarbons and was free from toluene. As the distillation proceeded, however, with the temperature at the top of the rectification column rising to 102.4 and 102.8 C., the amount of toluene in the oil distillate increased. At the latter temperature, the distillate substantially consisted of toluene and crotonaldehyde.

When the hydrocarbons in the distillate consisted of toluene, the residue left in the still and rectification column was withdrawn and washed with water to separate any trace of remaining crotonaldehyde it contained. The oil layer recovered from the aqueous layer formed in thus Washing the residue of the distillation was 100% toluene. Of the toluene initially present in the toluene fraction subjected to the distillation, 90% was recovered as residue of the distillation in the form of *he pure toluene product. This high yield of toluene is attributable to the very small amounts of toluene carried over in the distillate during the first stage of the azeotropic distilla- -toluene residue substantially free from nontoluene hydrocarbons.

A further saving of the toluene may be effected by collecting separately all intermediate distillates, relatively rich in toluene, boiling over a range of about 102.0 to 103.0 C. and returning these distillates to a fresh batch of crude toluene fraction. Toluene contained in the intermediate distillates may then be recovered by a subsequent azeotropic distillation. Incidentally, the crotonaldehyde contained in such distillates will function directly, without any intervening recovery being necessary, as azeotropic distillation component.

The crotonaldehyde in the lower-boiling distillates containing very little toluene, may be recovered separate from the hydrocarbons in the distillate for reuse in the distillation of additional toluene fraction. As pointed out above, by treating the distillate with water the hydrocarbon oils may be taken oil from separator 1 through pipe 9 separate from an aqueous liquid phase containing crotonaldehyde drawn through pipe I0 to storage vessel I I. Anhydrous crotonaldehyde may be recovered from this aqueous phase.

Water may be present in the distillation of the toluene fraction in the presence of the crotonaldehyde, although it is preferred to carry out this distillation under substantially anhydrous conditions. Water forms ternary azeotropes with crotonaldehyde, toluene and non-toluene hydrocarbons which have closer boiling points than the binary azeotropes of the crotonaldehyde with the non-toluene hydrocarbons and the toluene. Accordingly, the presence of water in the distillation reduces the effectiveness with which the toluene is separated from the like-boiling, nonaromatic hydrocarbons. Nevertheless, the presence of water in the azeotropic distillation is within the scope of my invention. For example, in carrying out the process of the above example modified to charge into the still a mixture containing 100 volumes of toluene fraction containing 75.5% toluene, 30 volumes of crotonaldehyde and 15 volumes of water, this mixture was fractionally distilled to leave as residue a product in which the hydrocarbons were 100% toluene and which contained 82% of the toluene present in the original toluene fraction. The distillation of this mixture containing water started with a temperature at the top of the rectification column of about C. This temperature rose to 85.3 C. when the non-aromatic hydrocarbons had been carried over as distillate, leaving a residue the hydrocarbon content of which was 100% toluene.

One advantage which may be taken of the fact that crotonaldehyde is eiective in the presence of Water for the azeotroplc separation of toluene from like-boiling, non-aromatic hydrocarbons is that the azeotropes with water, when cooled, separate into two phases, an oil layer and an aqueous layer,.both containing crotonaldehyde. The aqueous layer may be returned from storage vessel I I or directly from separator 1 to the azeotropic distillation to reuse therein the crotonaldehyde without necessitating a separation of the crotonaldehyde from the water.

While both of the examples described above employ a batch operation for the distillation of the toluene fraction, this distillation may be carried out continuously. For example, crotonaldehyde and toluene fraction may be continuously supplied to a column still in which the toluene isy concentrated-and, flowing to the bottom of the still, is continuously withdrawn therefrom. The azeotropes of crotonaldehyde and non-aromatic hydrocarbons are continuously vaporized and withdrawn as distillate from the top of the distillation column. Suflicient crotonaldehyde should be supplied to carry over as distillate al1 of the hydrocarbons to be distilled from the toluene fraction and separated from the toluene. By observation of the vapor temperatures at a suitable point in the vapor rectification column, one may ascertain whether adequate crotonaldehyde is present. Whenever these vapor temperatures tend to exceed 102 C. to 103 C. under anhydrous conditions or to 86 C. when water is present before the toluene has been separated to the desired degree from the like-boiling, non-aromatic hydrocarbons, by supplying additional crotonaldehyde (with or without Water) to the still or rectification column will assure the presence of suflicient crotonaldehyde to obtain the desired separation of the toluene and like-boiling, non-aromatic hydrocarbons; e. g., until a residue of the distillation is obtained which contains toluene and no more than 5 parts by weight of like-boiling, non-aromatic hydrocarbons for every 95 parts by weight of toluene. This point of temperature observation in the apparatus in which the above examples of the process were carried out, was the top of the rectication column. One skilled in the art of fractional distillation will recognize for any particular type of apparatus suitable points for this temperature control.

While in the examples given the major part of the toluene has been recovered as distillation residue, the distillation may be combined after the removal of non-toluene constituents so that an enriched toluene product is recovered as overhead. `Alternatively, enriched toluene products may be taken off as one or more side streams. -Both of these modications are within the scope of my invention.

In this speciiication I have described the azeotropic distillation as being carried out under substantially atmospheric pressure. The temperatures as given herein are corrected temperatures for 1 atmosphere absolute (760 mm. of Hg). When carried out under pressures other than atmospheric, the temperature conditions will differ from those given. In any given case, however, the temperatures will correspond to the change in boiling points of the materials due to the difference in pressure.

I claim:

1. The process for the recovery of toluene from a toluene fraction containing the same and containing like-boiling, non-aromatic hydrocarbons which comprises fractionally distilling said toluene fraction in the presence of. crotonaldehyde, thereby vaporizing and removing as distillate said like-boiling, non-aromatic hydrocarbons and leaving a hydrocarbon residue of the distillation enriched in toluene.

2. The process for the recovery of toluene which comprises azeotropically distilling in the presence of crotonaldehyde a toluene oil fraction boiling in the absence of said crotonaldehyde in the range 95 C. to 118 C., thereby vaporizing and removing as distillate said like-boiling, nonaromatic hydrocarbons and leaving a hydrocarbon residue of the distillation enriched in toluene.

3. The process for the recovery of toluene from a toluene fraction containing the same and containing like-boiling, non-aromatic hydrocarbons which comprises fractionally distilling said toluene fraction in the presence of substantially anhydrous crotonaldehyde, thereby vaporizing and romoving as distillate said like-boiling, nonaromatic hydrocarbons and leaving a hydrocarbon residue of the distillation enriched in toluene.

4. The process for the recovery of toluene from a toluene fraction containing the same and containing like-boiling, non-aromatic hydrocarbons which comprises fractionally distilling said ,toluene fraction inthe presence of crotonaldehyde, said crotonaldehyde being present in amount such that at a point in the fractionation of the vapors evolved in distilling the toluene fraction the temperature does not exceed 102 C. to 103 C. for anhydrous conditions and does not exceed C. to 86 C. when water is present until said like-boiling. non-aromatic hydrocarbons have been vaporized leaving a. hydrocarbon residue of the distillation containing toluene and no more than 5 parts by weight of like-boiling, non-aromatic hydrocarbons for every parts by weight of toluene.

5. The process for the recovery of toluene from a toluene fraction containing the same and containing like-boiling, non-aromatic hydrocarbons which comprises Iractlonally distiiling said toluene fraction in the presence o! water and crotonaldehyde, thereby vaporizing and removing as distillate said like-boiling, non-aromatic hydrocarbons and leaving a hydrocarbon residue of the distillation enriched in toluene.

6. The process for the recovery of toluene which comprises azeotropically distllling in the presence of water and crotonaldehyde a toluene oil fraction boiling in the absence of said crotonaldehyde and water in the range 95 C. to 118 C., thereby vaporizingw and removing as distillate said like-boiling, non-aromatic hydrocarbons and leaving a hydrocarbon residue of the distillation enriched in toluene.

'7. The process for the recovery of toluene from a toluene fraction containing the same and like-boiling, non-aromatic hydrocarbons which comprises distilling said toluene fraction in the presence of Water and of crotonaldehyde, thereby vaporizing and removing as distillate azeotropes of said like-boiling, non-aromatic hydrocarbons with said water and crotonaldehyde and leaving a hydrocarbon residue of the distillation enriched in toluene, cooling and condensing 'the aforesaid distillate, thereby obtaining a condensate which separates into two liquid phases, one a hydrocarbonoil-crotonaldehyde phase and the other an aqueous` crotonaldehyde phase, and employing said aqueous phase in the azeotropic distillation of said toluene fraction containing toluene and like-boiling, non-aromatic hydrocarbons.

FREDERICK W. SULLIVAN, JR.4