Search Images Maps Play YouTube News Gmail Drive More »
Sign in
Screen reader users: click this link for accessible mode. Accessible mode has the same essential features but works better with your reader.

Patents

  1. Advanced Patent Search
Publication numberUS2158670 A
Publication typeGrant
Publication dateMay 16, 1939
Filing dateFeb 20, 1937
Priority dateFeb 20, 1937
Publication numberUS 2158670 A, US 2158670A, US-A-2158670, US2158670 A, US2158670A
InventorsDouglas Barnes Charles, Wright William A S
Original AssigneeUnion Oil Co
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Process for the recovery of essential oils
US 2158670 A
Abstract  available in
Images(3)
Previous page
Next page
Claims  available in
Description  (OCR text may contain errors)

Patented May 16, 1939 UNETED STATES PATENT OFFICE PROCESS FOR '1 ESSENTI RECOVERY 0F OILS No Drawing.

5 Claims.

This invention relates to a process for the recovery of essential oils, such as orange oil, lemon oil, lime oil or other oils from citrus fruit.

It is common practice at present to recover.-

orange oil from orange peel by cold pressing the orange rind and pulp to separatea portion of the oil contained therein and recover the remainder of the oil present in the pressed residue by steam distillation. Theoil recovered from the pulp by steam distillation is considered inferior to the cold pressed oil because of the inclusion of undesirable constituents due to their volatility with the steam. Consequently, the oil which is recovered by steam distillation is of inferior quality to the cold pressed oil and, therefore has a somewhat lower commercial value. The yield of cold pressed oil from orange peel, however, is rather low, in fact on the basis of the whole fruit, from 0.1 to 0.3% is about the highest yield of oil which can be recovered by cold pressing. Therefore, the remainder of the oil which may amount to 0.45 to 0.7% is recov:

ered by steam distilling the cold pressed rind or Pu pa By our process we have discovered a method by which we are able to recover a major portion of the oil present in the citrus'pulp orpeel and at the same time retain in the recovered oil the degoing'proce'ss 'weare'able to recover as high as sirable quality characteristics of cold pressed oil,

The oil recovered by our process is completely "I soluble in 95% ethyl alcohol, which permits its incorporation in alcoholic flavoring extracts without the necessity of filtration for the preparation of clear solutions. While it ispossible to treat unpulped orange peel by our process it is preferable that the citrus peel be pulped or ground by any suitable method into a line slurry 'Ihis'slurry or ground citrus peel is then extracted with a. suitable solvent which has a high solvent power" for the oil and a minimum solvent power for the undesirable constituents of the peel'or'puln; "The I solvent solution of the citrus oil is then separated from the pulp or slurry and subjectedto distilla-jj I in the presence or absence of water.

tion for the removal of solvent'from the oil.

More specifically, the process consists in pulp-I- ing the citrus peel orgrinding in the presence of water to form a slurry containing the highest possiblecontent of essential oil, which upon con ce'ntration by'rejecting the juice and oil free portions of the fruit may actually reach 1 to 5% of essential oil. This pulp or slurry isthen con- Application February 20, 1937, Serial No. 126,886

the essential oil at temperatures substantially above 32 F. inorder to avoid freezing of oil cells which would reduce the yield of oil. The solvent and citrus pulp or slurry is then thoroughly agitated for a period of time sufliciently long to completely extract the essential oil. The mixture is then permitted to settle, the heavier pulp pres cipitating to the bottom of the container. After removal of a major portion of the water and pulp by any suitable means, the butane or other hydrocarbon solution is then separated from the remainder of the insoluble material by ordinary decantation or by filtration or by a combination of decantation and filtration, or, if desired, the butane solution may also be separated from the butane insoluble materials by centrifuging the mass. The butane phase recovered by the foregoing extraction contains the major portion of the essential oil in solution as well as some undesirable resins. sirable resins from the butane solution of essential oil, this solution is cooled sufl'lciently to cause the resins present to precipitate. The chilled butane solution is filtered, centrifuged or settled forthe separation of the precipitated resinous removal of the butane from the oil. By the foreapproximately 90% of the essential-oil present inthe citrus fruit; r

It is, thereforaan' object of the present inven- 'tion to recover citrus oil from citrus fruit or products by means 'of a solvent and to purify the recovered oil by separating' 'wax'or resinous constituentstherefrom. I I

It is a further object of the present invention to remove wax or resinous material from citrus ,oilby dissolving'thecitrus'oil in an appropriate solvent such as liquid butane, cooling the-solvent solutio'n'of oil to a temperature sufiicie'ntly lowto precipitate the w'axlor resinous material, removing the precipitated resinous or waxy material by centrifuging, settling or filtering and then recovering the dewaxed or deresinated oil from the'solution by removing the solventpresent by distillation. 1 r a It is a further object of the presentinvention to recover citrusfoil from citrus fruit by preparing a pulp or slurry of citrus fruit andcontacting the pulp rating the normal butane solution or citrus oil from the pulp, chilling the'solution to precipitate the resinous material present in the solution,

v with an appropriate solvent," such as liquid normal butane, to dissolve the on, sepaseparating the precipitated resinous material I from the butane solution of oil and by recovering the oil from the solution by removing the butane from the distillation.

The following is a specific example of the' method for carrying out our invention:

Orange pulp and rind is ground or macerated in the presence of water to form a slurry containing approximately 2 orange oil. This slurry is then mixed with liquid normal butane at a temperature of about 70 to F. in the propor tion of 2.75 parts by volume of liquid normal butane to one part by volume of the orange slurry. The mixture of orange slurry and normal butane is then agitated at a temperature of 70 to 80 F. for a period of about thirty minutes, after which the mass is permitted to settle for a period up to about twelve hours. A large portion of the water and solid pulp is then withdrawn from the extraction vessel. The butane solution of the orange oil remaining in the extraction vessel is then cooled to a temperature of about 32 F. for the precipitation of the resinous materials in the solution. The chilled solution is then filtered through paper or other suitable medium and thereby freed from the precipitated resinous ma- -terial, after which it is heated to about F.

for the removal of the major portion of the normal butane and finally to a maximum of 212 F. for not over fifteen minutes to remove any heavy ends of the hydrocarbon extractant from the orange oil. The oil recovered by the foregoing method is equal in quality to cold pressed orange oil and a yield of 86% of the total orange oil present in the slurry is obtained.

The chilling step for the separation of the resinous material is subject to some variation since certain of the oils extracted contain more of the resinous-or waxy material than others. In general a temperature of about 32 F. is satisfactory to remove sufficient of these resinous materials, however, .we do not wish to limit ourselves to this specific temperature since we have satisfactorily employed temperatures as low as 0 F. for precipitation of the resinous or waxy material from the solvent solution of oil. In carrying out the resin separating step it is important to note that it is desirable to leave from 2 to 5% of the resin or wax in the oil since oil containing lower. concentrations than these tend to resemble artificial oil and has a somewhat poorer flavor.

We have described liquid normal butane as being the preferred solvent since it has a high solvent power for the essential oils and aminimum solvent power for the undesirable constituents, its vapor pressure is sufflciently low at 70 to 80 F. that it does not necessitate the use of especiallyheavy equipment, it is available commercially in a sufficiently high state of purity to prevent contamination of the essential oil, and the boiling point is sufficiently low to permit complete removal from the essential oil without heating to temperatures high enough to impair the quality of the oil. However, we do not wish to limit ourselves to this solvent since many other solvents may be employed, as for example, isobutane, liquid ethane, liquid propane, the liquid pentanes, a suitable fraction from casinghead or primary gasoline and mixtures thereof. Furthermore, we may also employ other-solvents, as for example, ketones such as acetone and methyl acetone, and ethers such as ethyl and isopropyl ether or mixtures of those solvents. Preferably the solvents which we employ should have a lower boiling point than that of the citrus oil in order to permit good fractional distillation between the oil and solvent. Furthermore the solvents should be free from malodorous or maltasting constituents which impart to the oil a bad taste or odor. It is also preferable that the solvent employed should not be water soluble to any appreciable extent. In some instances the solvent may be treated for removal of constituents present which unfavorably influence the quality of the oil. For example, low boiling hydrocarbon solvents may be pretreated with caustlcsoda for the removal of hydrogen sulphide or mercaptans both of which impart a highly undesirable odor to citrus oil. Furthermore, we have described a process in which 2.75 volumes of solvent and one volume of citrus are mixed together for the recovery of the oil, but we do not wish to limit ourselves to these proportions since in many cases it may be desirable to alter this ratio. In some instances it may require three or four volumes of the liquid butane to one volume of the citrus pulp or slurry and in other instances it may be desirable to use equal or even smaller volumes of solvent than of pulp ,or slurry.

We have described a process in which we have employed an extraction temperature of about that of atmospheric, namely 70 F. to 80 F. However, we do not wish to limit ourselves to this temperature since in some instances it may be desirable to employ temperatures which are greatly in excess of atmospheric, for example, the orange slurry may be charged into a pressure bomb together with the liquid normal butane and this mixture may be heated to a temperature of about F. to 200 F. together with agitation in order to insure complete solution of the oil in the solvent. After complete solution, the mixture, may then be cooled and after removal of the water and 'the resinous materials present in the solution by cooling and separating, as described above, the orange oil may then be recovered by simply removing the normal butane present.

Another modification of the process consists in leaching the slurry at a temperature at which the resinous material will not go into solution. This temperature will be about 32 F. to 35 F. At this temperature the slurry is a solid mass due to the crystallization of the water present. When operating according to this cold leaching method the chilled slurry at a temperature of 32 F. to 35 F. is intimately mixed with chilled normal butane at about the same temperature.

After thorough agitation the chilled mixture con-- taining the dissolved orange oil is then separated.

from the insoluble pulp and after filtration to remove any solid material which may be present the solvent is removed from the oil by distillation.

It is to be understood that these disclosures are presented as illustrative of the generic invention solvent under sufl'icient pressure to maintain said solvent in a liquid state, settling the mixture of slurry and solvent under pressure and thereby forming a solvent layer containingthe citrus oil and a slurry layer, separating said layers, cooling the solvent layer to precipitate resinous material, removing the precipitated resinous material from the solvent layer and removing the solvent from the de-resinated oil. i

2. A process according to claim 1 in which the solvent is liquid butane.

3. A process according to claim 1 in which the solvent layer is cooled to a temperature between 0 F. and 32 F. for precipitation of the resinous material.

4. A process for the purification of citrus oil containing resinous impurities which comprises grinding citrus peel with water and thereby forming a slurry, commingling said slurry with cooled liquefied normally gaseous hydrocarbon solvent under suflicient pressure to maintain said solvent in a liquid state, settling the mixture under pressure and thereby forming a liquidsolvent layer containing the citrus oil and a slurry layer, separating said layers, and removing the solvent from the layer containing the citrus oil.

5. A process according to claim 4 in which the leaching temperature is between 0 F. and 32 F.

CHARLES DOUGLAS BARNES. WILLIAM A. S. WRIGHT.

Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US2415600 *Jan 24, 1942Feb 11, 1947Meakin Edgar NMethod for the recovery of fluids
US2863861 *Jun 25, 1956Dec 9, 1958Ventura ProcessorsProcess for purifying citrus oils
US3155648 *Apr 3, 1961Nov 3, 1964Sunkist Growers IncProcess for producing de-waxed citrus oils
US4497838 *Apr 20, 1983Feb 5, 1985Tropicana Products, Inc.Process for the production of useful products from orange peel
US7060313 *Oct 27, 2003Jun 13, 2006Robert Allen JonesAfter fruit juice extraction, recovering citrus oil, aromas from peels, producing pectin pomace; food processing by adding water, heating, pressing, evaporating; low biological oxygen demand, the effluent water can be discharging into sewage systems; recycling waste
Classifications
U.S. Classification426/651, 426/429
International ClassificationA23L1/222, A23L1/221
Cooperative ClassificationA23L1/2225
European ClassificationA23L1/222B