US2119871A

US2119871A - Separation of hydrocarbon mixtures into constituent parts

Info

Publication number: US2119871A
Application number: US582501A
Authority: US
Inventors: James M Whiteley
Original assignee: Standard Oil Development Co
Current assignee: Standard Oil Development Co
Priority date: 1931-12-21
Filing date: 1931-12-21
Publication date: 1938-06-07
Anticipated expiration: 1955-06-07

Description

Patented June 7, 1938 UNITED STATES Z,ll9,871:

SEPARATION OF HYDROCARBON MIXTURES INTO CONSTITUENT PARTS James M. Whiteley, Roselle, N. J., assignor to Standard Oil Development Company, a corporation of Delaware No Drawing. Application December 21, 1931, Serial No. 582,501. Renewed August 13, 1937 Claims.

This invention relates to the separation of hydrocarbon mixtures into constituent parts, and more specifically comprises a method for separating such hydrocarbon mixtures into fractions of different molecular weight and/ or fractions of dissimilar hydrocarbon structure by means of a selective hydrocarbon solvent.

The term hydrocarbon mixtures is intended to include hydrocarbon oils such as heavy gas oils, lubricating distillates, cylinder oils, residual oils, fuel oils and the like, as well as waxy hydrocarbon materials, such as petrolatum and paraflin wax or mixtures of oil and wax, whether obtained from petroleum, or by the cracking, destructive distillation or hydrogenation of shales, coals, lignites, tars, pitches, bitumens and other carbonaceous materials.

Hydrocarbon mixtures may be readily separated into fractions of different boiling point and rectification. They may also be separated into fractions of dissimilar hydrocarbon structure, that is, separated into paraffinic and aromatic or naphthenic fractions by means of selective solvents such as phenol, aniline, liquid sulfur dioxide, nitrobenzene and the like. In many cases, however, the application of heat even under high vacuum to heavy oils in order to distill the lower boiling fractions may be undesirable due to the cracking and polymerization which occurs. The use of the common selective solvents is wasteful and expensive and necessitates subsequent complete elimination of the solvent which is always a non-hydrocarbon material.

I have now found that hydrocarbon mixtures may be separated into their constituent parts according to molecular weight and/or hydrocarbon structure by the incorporation therewith of a selective hydrocarbon solvent. This avoids the necessity for applying heat and has the additional great advantage that the agent of separation is a hydrocarbon itself. The method by which this separation may be effected and the nature of the preferred selective hydrocarbon solvents will be fully understood from the following description.

It has been indicated that separation may be made either according to molecular weight or according to hydrocarbon structure. If a mixture of wide boiling range is selected as the initial material, separation 'will be principally according to molecular weight and only a small amount of separation according to structure occurs. If separation according to structure is principally desired it is preferable .to start with :a mixture molecular weight by distillation, fractionation or of more limited boiling range, say one with a boiling range of not more than 20 to- F. g

The hydrocarbon mixture to be separated into constituent parts is placed in a suitable vessel which is adapted to be maintained under a pressure sufficient at the temperature employed to retain the light hydrocarbons used to effect the separation in liquid phase. Temperatures between say -40 and F. or even 200 Rare suitable, and pressures varying from slightly above atmospheric to 50 or more atmospheres may be used.

The hydrocarbon mixture is then diluted with from 3 to 15 volumes or more of a selective hydrocarbon solvent. such as, for example, a liquefied normally gaseous hydrocarbon or mixture of liquefied hydrocarbons. If a hydrocarbon oil con,- taining substantial amounts of asphaltic materials is to be treated, it is preferable to add the liquefied hydrocarbon to the oil slowly or stepwise ln small quantities, this to avoid a sudden precipitation of such asphaltic materials and the entrapment of globules of oil which results therefrom. Vigorous agitation may be provided to facilitate the mixing of the hydrocarbon mixture with the diluent.

Selective hydrocarbon solvents suitable for the purpose of the present process comprise generally all those hydrocarbons the boiling point of which lies below about 0 C. Among these are methane, ,1

ethane, propane, butane, iso-butane, ethylene, propylene, butylene, iso-butylene or any mixtures of these. Other hydrocarbonssuch as acetylene and cyclobutane may also'be used. Small quantities of higher boiling hydrocarbons such as pentane, hexane and even higher are not objectionable, but in general the lower boiling hydrocarbons are preferred. The particular hydrocarbon or mixture of hydrocarbons chosen as the agent of separation will depend very largely on the nature of the material to be separated and also on practical and economical considerations of the pressure necessary to maintain the separating. agent in the liquid phase at the temperature of working. Thus, for example, methane alone would require a very great pressure, and unless a high degree of separation were desired, its use would hardly be economically justified. Pure methane or methane containing only small quantities of higher hydrocarbons may however be used with satisfactory results. Ethane and pro,- pane are the preferred hydrocarbons because these can be maintained in the liquid phase under moderate pressures say about 15 atmospheres, .more or less, depending upon the proportion of ethane to propane. The whole or a part of the normally gaseous hydrocarbon may if preferable be pumped into the hydrocarbon mixture in gaseous form and the whole mass then subjected to pressure to effect the liquefaction.

The gases obtained in the cracking of hydrocarbons normally contain small quantities of these lighter hydrocarbons and such gases may be liquefied and used as the diluent. Gases ob: tained in the stabilization of gasoline furnish an especially suitable source of the preferred hydrocarbons, ethane and propane.

The quantity of liquefied hydrocarbon used naturally depends upon the nature of the material to be separated into constituent parts. If the mixture is a hydrocarbon oil sufiicient diluent should be added to cause the formation of two distinct layers. If the mixture is a solid or waxy hydrocarbon the quantity of diluent should at least be sufficient to dissolve the soluble portions of the mass.

Following dilution of the hydrocarbon mixture, the two layers or the two fractions into which the mixture has been divided are separated the one from the other by any suitable means, such as decanting, filtering or otherwise and the liquefied hydrocarbon diluent removed from each part by vaporization or other means. The recovered diluent may be recycled with a fresh portion of material as will be understood. Prior to removing the diluent, either or both portions may be filtered while diluted with the liquefied hydrocarbon through adsorptive media such as clay or charcoal. Filtration in the light hydrocarbon solution is extremely rapid and efficient and results in an improved color and appearance of the separated products.

Although the above described method of separating hydrocarbon mixtures into constituent parts is applicable to all types of hydrocarbons Whether liquid, solid, or combinations of liquid and solid, it is particularly adapted to the separation of heavy hydrocarbon oils, especially the lubricating fractions of petroleum oils, into component oils of dissimilar composition and characteristics.

When working with petroleum oils a mixture of propane and ethane provides a very satisfactory selective solvent or separation agent. If such a solvent is used the ethane should be present in an amount preferably above say 15% and below say 85%, although smaller or larger quantities may be used. By increasing the proportion of ethane in the selective solvent the volumev of heavy oil thrown out in the bottom layer is correspondingly increased. Depending therefore upon what degree of separation is desired the ratio of ethane to propane may be increased or decreased. This of course applies also to other mixtures of hydrocarbons of 2 carbon atoms or less with hydrocarbons of 3 carbon atoms or more. When only 15% ethane is used the bottom layer contains a very small amount of a high molecular weight and high viscosity oil. On the other hand when 85% ethane is used the bottom layer comprises a very large proportion of the oil and has a correspondingly lower viscosity.

When carrying out the process for the purpose of separating the parafiinic from .the aromatic and naphthenic hydrocarbons, in which case a fraction of narrow boiling range is preferably chosen as the starting material, it may be advantageous to use selective solvents for aromatic and naphthenic hydrocarbons such as liquid sulfur dioxide, phenol, aniline, nitrobenzene and the like, in addition to the liquefied hydrocarbons which latter exhibit a selective solvent action for the paraflinic hydrocarbons.

By controlling the proportion of ethane and propane used, the total volume of separating agent, and the temperature and pressure at which the process is carried out it is possible to separate heavy hydrocarbon oils into fractions of different viscosity temperature characteristics and to increase the viscosity temperature characteristic of either the lighter fraction or the heavier fraction.

The following example illustrates the application of this process to a cylinder oil. A finished cylinder oil dewaxed to zero pour obtained from a Ranger crude is diluted with 5 Volumes of propane and 6 volumes of ethane at a temperature of about F. and under pressure of 20 atmospheres. Two distinct oil layers are formed which are separated and the liquefied hydrocarbon removed by vaporization. The top layer is found to contain 38% of the original oil, the bottom layer 62%. A comparison of the characteristics of the original oil and the top and bottom layers follows:

The viscosity index, V. 1., indicates the relation between the viscosity at 100 F. and the viscosity at 210 F. and is such that the smaller the difference in viscosity at these two temperatures the higher is the V. I. It is defined by Dean and Davis in Chemical and Metallurgical Engineering, Vol. 36, No. 10, October 1929.

To illustrate the efiect of varying the proportion of ethane and propane used another portion of the same oil is diluted with 5 volumes of propane and only 3 volumes of ethane. When the two layers are separated and the propane and ethane are flashed off, the top layer is found to contain 87% of the original oil and the bottom layer only 13%.

This example shows that by decreasing the proportion of ethane used the volume of oil thrown out is reduced. The increase in V. I. of the oil in the top layer over the V. I. of the original oil, however, is correspondingly reduced. For example, in this last example the V. I. of the top layer was only as compared with 96 in the first example.

This invention is not limited by any theory of the mechanism of the separation nor by any details or examples which have been given merely for illustrative purposes, but is limited only by the following claims in which I wish to claim all novelty inherent in the invention.

I claim:

1. Process for separating asphalt-free hydrocarbon oil into its lighter and heavier normally liquid hydrocarbon components which comprises diluting the oil with several volumes of a liquefied normally gaseous hydrocarbon mixture comprising hydrocarbons having two and threecarbon atoms and in which the hydrocarbon having two'carbon atoms is present in an amount between 15 and maintaining the diluted oil under pressure sufficient to retain the normally gaseous hydrocarbons in liquid phase, separating the two layers into which themixture is thereby caused to separate, and recovering oil from each layer.

2. Process according to claim 1 in which liquefied gases obtained in the stabilization of gasoline are used as the diluent.

3. Process according to claim 1 in which the hydrocarbon oil is one derived by the destructive hydrogenation of petroleum.

4. Process according to claim 1 in which the hydrocarbon oil is one derived from shale.

5. Process for obtaining a lubricating oil of high viscosity index from a heavy asphalt-free hydrocarbon oil fraction having a narrow boiling range and a relatively low viscosity index which comprises diluting the oil with between three and fifteen volumes of a mixture of liquefied propane and ethane in which the ethane is present in an amount of at least 15% but not more than about separating the two layers into which the heavier hydrocarbon oil is thereby caused to separate and recovering the high viscosity index oil from the upper layer.

6. In a process for separating an asphalt-free hydrocarbon oil into its normally liquid hydrocarbon components by means of a liquefied normally gaseous hydrocarbon solvent, the method of regulating the molecular weight of the two fractions into which the oil is separated which comprises utilizing a mixture of liquefied propane and ethane and regulating the amount of ethane in the mixture between the limits of 15% and 85%, the molecular weight of the lower layer being decreased as the quantity of ethane in the liquefied hydrocarbon mixture is increased.

7. Process for separating asphalt-free hydrocarbon oil into its lighter and heavier normally liquid hydrocarbon components which comprises diluting the oil with several volumes of a liquefied normally gaseous hydrocarbon mixture comprising hydrocarbons having 2 and 3 carbon atoms, maintaining the diluted oil under pressure sufficient to retain the normally gaseous hydrocarbons in liquid phase, separating the two layers into which the mixture is thereby caused to separate, and recovering oil from each layer.

8. Process for separating asphalt-free hydrocarbon oil into its lighter and heavier normally liquid hydrocarbon components which comprises diluting the oil with several volumes of a liquefied normally gaseous hydrocarbon mixture comprising hydrocarbons having 2 and 3 carbon atoms in such proportions that the oil is caused to separate into two layers, maintaining the diluted oil under pressure sufficient to retain the normally gaseous hydrocarbons in liquid phase, separating the two layers, and recovering oil from each layer.

9. Process for obtaining a lubricating oil of high viscosity index from a heavy asphalt-free hydrocarbon oil fraction having a narrow boiling range and a relatively low viscosity index, which comprises diluting the oil with between 3 and 15 volumes of a mixture of liquefied propane and an effective quantity of ethane, separating the two liquid layers into which the heavier hydrocarbon oil is thereby caused toseparate and recovering the high viscosity index oil from the upper layer.

10. In a process for separating an asphalt-free hydrocarbon oil into its normally liquid hydrocarbon components by means of a liquefied normally gaseous hydrocarbon solvent, the method of regulating the molecular weight of the two fractions into which the oil is separated, which comprises utilizing a mixture of liquefied propane and an effective quantity of ethane and regulating the amount of ethane in the mixture, the molecular weight of the lower layer being decreased as the quantity of ethane in the liquefied hydrocarbon mixture is increased.

JAMES M. WHI'I'ELEY.