US3632616A - Apparatus and process for the selective fractionation of fatty materials into useful fractions thereof - Google Patents

Apparatus and process for the selective fractionation of fatty materials into useful fractions thereof Download PDF

Info

Publication number
US3632616A
US3632616A US729489*A US3632616DA US3632616A US 3632616 A US3632616 A US 3632616A US 3632616D A US3632616D A US 3632616DA US 3632616 A US3632616 A US 3632616A
Authority
US
United States
Prior art keywords
miscella
fraction
fractionation
fractions
solvent
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US729489*A
Other languages
English (en)
Inventor
Richard Kassabian
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Individual
Original Assignee
Individual
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Application granted granted Critical
Publication of US3632616A publication Critical patent/US3632616A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
    • C11C1/00—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids
    • C11C1/007—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids using organic solvents
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B7/00—Separation of mixtures of fats or fatty oils into their constituents, e.g. saturated oils from unsaturated oils
    • C11B7/0008—Separation of mixtures of fats or fatty oils into their constituents, e.g. saturated oils from unsaturated oils by differences of solubilities, e.g. by extraction, by separation from a solution by means of anti-solvents
    • C11B7/0041—Separation of mixtures of fats or fatty oils into their constituents, e.g. saturated oils from unsaturated oils by differences of solubilities, e.g. by extraction, by separation from a solution by means of anti-solvents in mixtures of individualized solvents (water is not taken into account)

Definitions

  • Means are included to mix the fatty materials with a solvent blend, in which one of the solvents functions primarily as a diluent, to form a miscella which is then successively subjected to successively lower fractionation temperatures to selectively fractionate for removal the desired, useful fatty material fractions.
  • This invention relates to a new and improved apparatus and process for the fractionation of triglyceride or fatty acid mixtures into respectve, commercially valuable fractions thereof and, more particularly but by no means exclusively, to apparatus and process for the fractionation of palm oil to obtain therefrom a fraction which is eminently suitable for use as a commercial substitute for cocoa butter.
  • the prior art is, of course, replete with apparatus and processes for triglyceride oil and/or fatty acid mixture fractionations but, in most instances, each of the said prior art apparatus and processes are known to embody disadvantages when employed on commercial scale. More specifically, in some instances the said prior art apparatus and processes do not provide for sufficient fraction separation resolution, to thus render impractical the separation of closely related fractions or, alternatively, require the use of unduly large numbers of process stages to compensate for this lack of sufficient process resolution. In other instances, the said apparatus and processes of the prior art are far too complex and costly in fabrication, operation, and process material requirements for reasonable commercial application. In still other instances, the said apparatus and processes of the prior art are suitable for laboratory or pilot plant use but are inherently of such relatively small capacity as to be inapplicable to large scale commercial use.
  • Another object of this invention is the provision of apparatus and process as above which are of particularly simple and economical design, construction and manner of operation and which require therein the use of only readily available components of proven dependability, and of readily available process operating materials.
  • a further object of this invention is the provision of apparatus and process as above which are particularly adapted to economical, large-scale commercial use.
  • a still further object of this invention is the provision of apparatus and process as above which are particularly, though by no means exclusively, adapted to the fractionation from palm oil of a superior quality, eminently suitable commercial substitute for cocoa butter at a cost per unit weight of the latter far below currently prevailing costs of cocoa butter.
  • multi-stage fractionation apparatus comprise, for each stage thereof, fractionation means in the nature of a cold room wherein are contained fraction crystallization and separation means.
  • a process feed stage is provided and functions to form a miscella of predetermined proportions from the triglyceride oil and a solvent blend, and to feed the said miscella to the first of the fractionation means stages.
  • one of the solvents of the solvent blend in essence functions as a diluent to dilute the solvent action of the other solvent to thus enable fractionation at relatively high temperatures.
  • the respective fractionation stage cold rooms, and crystallization and separation apparatus contained therein are maintained at somewhat, although not greatly, differing temperatures and the miscella is fed to the first fractionation stage.
  • the desired fraction is removed from the miscella through the combined effects of the cold room temperature and the action of the solvent blend on the triglyceride oil, both of which result in the crystallization of the particular fraction commensurate with the cold room temperature, and the subsequent separation if the thusly crystallized fraction from the miscella through the operation of the fraction separation means.
  • the figure is a schematic diagram, in flow sheet form, of apparatus constructed in accordance with a preferred embodiment of my invention.
  • fractionation apparatus generally indicated at 6, particularly but by no means exclusively adapted to the selective fractionation of palm oil into a plurality of the useful fractions thereof with special emphasis being placed, in this instance, upon the fractionation therefrom of a superior quality, commercially acceptable substitute for cocoa butter at significantly lower cost per unit weight than that of the latter.
  • the apparatus 6 will be seen to include a process blending and feed stage, generally indicated at 8, and a process fractionation stage, generally indicated at 10.
  • the process blending and feed stage 8 comprises solvent supply tanks 12 and 14, connected as shown by conduits 16, 18 and 24, respectively, to readily adjustable pump means 19 and 20, and readily adjustable liquid metering means 22 of suitable performance characteristics, all arranged in the depicted manner.
  • solvent supply tanks 12 and 14 will hold different solventsfor example acetone and isopropanol, respectively, as discussed in detail hereinbelow-whereby the readily adjustable pump means 19 and 20 may be adjusted to provide a wide range of solvent blends, by volume, from the solvent supply tanks to the liquid metering means 22 and therefrom to a solvent blend delivery conduit 26 as should be obvious.
  • oil supply tanks 28 and 29 are provided for the supply of triglyceride oils which, in some instances, have been neutralized and washed in conventional manner, and are connected as shown by conduits 30 and 31 to readily adjustable pump means 32 of suitable performance characteristics.
  • Non-illustrated temperature control means in the nature, for example, of cooling or heating coils are incorporated in each of oil supply tanks 28 and 29 to enable the maintenance of the oils contained therein at desired temperature levels and in the liquid state.
  • Pump means 32 are in turn connected as shown to conduit 26 by conduit 34 extending therebetween, and readily adjustable liquid metering means 36 are connected as shown in conduit 34.
  • In-line mixer means 33 are arranged as shown in delivery conduit 26 downstream of the juncture thereof with conduit 34.
  • a miscella blend or make-up tank 38 is connected as shown to conduit 26 downstream of the said juncture, and is provided to insure proper blending of the solvent and triglyceride oil constituents of the said miscella prior to further utilization thereof.
  • the said makeup tank will preferably include non-illustrated agitator means to insure proper solvent-oil mixing and will, in addition, preferably include non-illustrated temperature control means to provide for the maintenance of the miscella at a desired temperature level.
  • a process feed tank 40 is connected to blend tank 38 by conduit 42, and readily adjustable pump means 44 are connected as shown in the latter.
  • tank 40 also preferably includes non-illustrated agitator and temperature control means, respectively.
  • the tank 40 is connected to the fractionation stage by delivery conduit 46, and readily adjustable pump means 48 are connected in the latter to thus provide for the steady delivery of the miscella, at a desired rate, and at a desired temperature, to the said fractionation stage.
  • the process blending and feed stage 8 may further include rework tanks 60 and 62, respectively, series connected as shown by conduit 64, and connected to readily adjustable pump means 68 by conduit 66, and therefrom to an outlet conduit 7 0.
  • An inlet conduit 72 may be utilized to connect tank 60 to any point in the fractionation stage 10 to thus provide for the storage of the miscella being processed in the event of fractionation stage failure.
  • outlet conduit 70 may be connected to any point in the fractionation stage 10 to provide for the re-introduction of the thusly stored miscella thereto after the said failure has been repaired.
  • the same may be seen to include a plurality of adjacent cold rooms or sub-stages A, B, and C, respectively, formed as shown by heavily insulated walls 80, 82, 84, 86, 88, and 90, respectively, each of which is selectively maintainable at a desired temperature through the use of temperature control means as indicated generally at 92, 94, and 96, respectively.
  • the temperature control means will preferably take the form of dual function, heat exchange means which are operable to lower the respective cold room temperatures if the desired levels thereof are below the prevailing ambient temperatures, and to conversely raise the said temperatures if the desired levels thereof are above the prevailing ambient temperatures.
  • thermocontrol means 92, 94 and 96 means in the nature of large, non-illustrated hot and cold tanks containing heat transfer fluids in the nature of THERMINOL FR as marketed by the Monsanto Chemical Company, might be employed to operate the temperature control means 92, 94 and 96 and could, in addition, he called upon to provide both heating and cooling fluid where and if required at other points in the process.
  • heat exchange means may, of course, be
  • Fractionation apparatus as generally indicated at 112A, 112B and 112C, respectively, are positioned as shown in the respective cold rooms, and are of substantially identical construction and manner of operation unless otherwise specifically noted.
  • the said fractionation apparatus namely 112A, will be described in detail, it being understood that the correspondingly numbered structural components of the others, which accordingly bear different identifying letter designations, are of the same constructions and manners of operation.
  • Fractionation apparatus 112A comprises jacketed heat exchange unit means in the nature of scraped surface crystallizer means 114A which are connected as shown to conduit 46 and will thus function to receive the triglyceride oil-solvent miscella from process feed tank 40 and retain it for a period of time sufficient to reduce the temperature thereof to the ambient temperature within cold room A.
  • a slurry mixing, cooling and holding tank 116A is provided and connected as shown to scraped surface crystallizer means 114A by conduit 118A.
  • the tank 116A functions to receive the crystal-miscella slurry from the crystallizer means 114A and retain the former for a period of time sufiicient to provide crystal growth while maintaining the same in suspension in the miscella- Pusher type centrifuge means 120A, including an inlet 132A, are connected as shown, by conduit 122A, to tank 116A to receive the cooled slurry and miscella therefrom.
  • a wash solvent blend holding tank is indicated at 124A and is connected to pusher type centrifuge means 120A by conduit 126A.
  • the tank1243A functions to receive solvent blend from without the col room Aas described hereinbelow-hold the said solvent blend for a period of time sufficient for it to assume the ambient temperature of cold room A, and introduce it, through conduit 126A, to pusher type centrifuge means 120A as a wash solvent blend to maintain a fraction in solution for purposes described in detail hereinbelow.
  • Self-thinker type centrifuge means are indicated at 128A, and the inlet thereof is connected as shown to an outlet of the pusher type centrifuge means 120A by conduit 130A.
  • Moyno type pump means 136A are connected as shown to the crystallized fraction output of the pusher type centrifuge means 120A, and a crystallized fraction discharge means 134A extend as shown from the crystallized fraction outlet of the self-thinker centrifuge means 128A to the said Moyno type pump means.
  • a crystallized fraction discharge means 134A extend as shown from the crystallized fraction outlet of the self-thinker centrifuge means 128A to the said Moyno type pump means.
  • the Moyno pump means extend as shown through cold room wall 88 to discharge into a separated fraction holding tank 138A.
  • the fraction separated from the triglyceride oil through the operation of the apparatus of cold room A, and any small quantity of solvent blend which may remain therewith, may be transferred to holding tank 138A for further processing.
  • a miscella discharge conduit 140A extends as shown from self-thinker type centrifuge means 128A, through heavily insulated 'wall 82, to the inlet of the scraped surface crystallizer means 11413 of cold room B.
  • miscella minus, of course, the triglyceride oil fraction separated therefrom through the operation of the elements of cold room A, may be conveyed to cold room B for the separation therefrom of another triglyceride oil fraction commensurate with the temperature prevailing in cold room B.
  • Fractionation apparatus 11213 and 1120 are of substantially the same construction as fractionation apparatus 112A and are, of course, connected in series therewith; with the miscella discharge conduit 140A of self-thinker type centrifuge means 128A extending, as described hereinabove, through cold room wall 82 into connection with the inlet of scraped surface crystallizer 114B, and miscella discharge conduit 140B of self-thinker type centrifuge means 128B similarly extending into connection with the inlet of scraped surface crystallizer 114C.
  • the Moyno type pump means 136B from cold room B extend as shown to fraction holding tank 138B, while the Moyno type pump means 136C from cold room C extend as shown to fraction holding tank 138C.
  • the miscella discharge conduit 140C from the selfthinker type centrifuge means 128C extends as shown to a processed miscella holding tank 142.
  • Each of the separated fraction holding tanks 138A, 138B and 138C, and the processed miscella hold tank 142 is connected as shown, by conduits 144, 146, 148 and 150 to solvent stripper means 152 whereby the solvent blend remaining with the said separated fractions and processed miscella may be readily stripped therefrom.
  • An evaporation means 143 is interposed in conduit 150 since a relatively large amount of solvent blend is present in the processed miscella from tank 142. Thus the evaporation means 143 will function to remove most of this solvent blend before the processed miscella is fed to the solvent stripper means 152.
  • Solvent blend return lines 154 and 155 extend respectively from the said solvent stripper and evaporation means for the supply of the solvent blend to a solvent blend reconstitution tank 157. After solvent blend reconstitution, in accordance with the desired solvent blend proportions, the reconstituted solvent blend may, if desired, be supplied for solvent blend wash purposes, to the respective cold room, wash solvent blend holding tanks 124A, 124B and 124C
  • Deodorizer means 158 are connected to solvent stripper means by conduit 156 and will, of course, function to deodorize the respective separated fractions prior to the transport thereof, as indicated by 160, to fraction collection means 162.
  • oil supply tanks 28 and 29 are filled with palm oil which has been neutralized and washed in conventional manner to insure that no soap is present therein.
  • solvent supply tank 12 is filled with acetone of commercially available grade
  • solvent supply tank 14 is filled with isopropanol of 99% purity, again a commercially available grade, it being here emphasized that other and different solvents may find satisfactory utilization in this process as discussed in detail hereinbelow.
  • This filling of the respective oil and solvent supply tanks may be effected in any convenient manner, as for example through the utilization of non-illustrated feed pump and tank inlet means, it being noted that non illustrated continuously operable tank filling means may be employed to maintain a constant supply of palm oil and solvent to the said tanks and thus enable substantially continuous operation of the process.
  • non illustrated continuously operable tank filling means may be employed to maintain a constant supply of palm oil and solvent to the said tanks and thus enable substantially continuous operation of the process.
  • batch type filling thereof could, of course, be employed.
  • each of pump means 19, 20 and 32, and liquid metering means 22 and 36 are adjusted to provide a solvent blend of approximately 25% by weight of acetone and approximately 75% by weight of isopropanol, commonly referred to as aciso 2575 by those skilled in this art, to conduit 26, and a blend or miscella of approximately 50% by weight of neutralized palm oil and 50% by weight of the said solvent blend, to miscella make-up tank 38 and, as follows, process feed tank 40.
  • solvent blends may be satisfactorily utilized and that as a general range for the fractionation of palm oil using acetone and isopropanol, solvent blends ranging from 5% to 50% by weight of acetone and 95% to 50% by weight of isopropanol may be used. Too, the proportion of the palm oil fatty material to solvent blend may range from a ratio of one part by weight of palm oil to two parts by weight of solvent blend, to two parts by weight of palm oil to one part by weight of blend.
  • heat exchanger means 92, 94, and 96 are regulated by the non-illustrated control means associated therewith to provide and maintain temperatures ranging from 70 F. to F. in cold room A, 55 F. to 65 F. in cold room B, and 45 F. to 55 F. in cold room C, respectively.
  • said temperatures will be approximately 75 F. in cold room A, 60 F. in cold room B, and 50 F. in cold room C.
  • the approximately 25-75 solvent blend by weight of acetone and isopropanol has been determined to result in very desirable crystallization characteristics, at the respective, relatively high sub-stage temperatures referred to hereinabove, within the respective fractionation apparatus 112A, 112B and 1120; it being noted that the isopropanol appears to fuunction primarily as an acetone diluent in that the use of a significantly larger proportion of acetone would require a lower temperature for the respective sub-stage crystallizations, and especially insofar as the crystallizations of the lower melting point diunsaturated and/ or tri-unsaturated triglycerides are concerned.
  • the diluted solvent power of the acetone causes the respective fatty fractions to be on the verge of precipitation whereby the latter can be selectively separated by the relatively slight, e.g. approximately 15 F., changes in temperature occurring between the respective cold rooms A, B and C.
  • the isopropanol is normally considered a solvent, it may, in this instance, be referred to as a diluent.
  • the relatively moderate cold room temperatures of crystallization can be employed as compared, for example, with the much lower temperatures of crystallization required by the somewhat similar processes of the prior art, whereby the significant economics of operation made possible by the process of the invention are believed made obvious.
  • the use of an approximately 1 to 1 ratio of oil and solvent blend made possible by the process of the invention greatly enhances the commercial feasibility thereof as compared, for example, with the somewhat similar processes of the prior art which requires 3 to 1 or even greater solvent to oil ratios and are thus forced to operate to overcome the significant economic disadvantages inherent in the fractionation of an extremely diluted oil. Too, by the use of the disclosed relatively high cold room temperatures, and the oilsolvent blend ratio and attendant avoidance of extreme oil dilution, the viscosity of the miscella is maintained in a range very conducive to proper miscella flow rates.
  • a typical plant constructed in accordance with the teachings of this invention for the selective fractionation of palm oil to produce a commercially acceptable substitute for cocoa butter might operate at an overall flow rate of two tons per hour and provide for an approximately three hour retention time for the miscella in each of the cold rooms. This would thus require an initial flow rate in the process feed stage 8 of approximately one ton per hour of palm oil and approximately one ton per hour of the solvent blend whereby pump means 20, 32, 44 and 48, and liquid metering means 22 and 36 may be adjusted accordingly.
  • wash solvent blend as described above would insure that fractions which are not to crystallize in any particular cold room will remain substantially in solution and pass therethrough for crystallization in a succeeding cold room, or removal with the processed miscella through conduit 140C from cold room C.
  • palm oil contains a relatively small, but very valuable beta carotene fraction
  • the addition of the wash solvent blend will function to retain this carotene fraction in solution for discharge with the processed miscella whereby the latter may, if desired, be further processed through the use of a similar solvent fractionation process to further concentrate the said carotene fraction to significant economic advantage.
  • operation of the depicted apparatus would thus entail the flow to and through the respective miscella make-up tank 38 and process feed tank 40 of approximately two tons per hour of the miscella with the said tanks functioning to both insure satisfactory mixing of the solvent and oil to form the miscella, and the maintenance of the latter at a temperature above that at which crystallization of the first triglyceride fraction will commence, in this instance a temperature above 80 F.
  • the resultant crystal-miscella slurry is then flowed to slurry mixing and cooling tank 116A wherein it is retained for a period of time sufficient to promote further crystal growth. In instances wherein a three hour cold room retention time is utilized, the period of retention in the tank 116A might approximate 2.0 hours or less.
  • Flow of the slurry from cooling tank 116A to pushertype centrifuge means 120A is then effected whereby the latter will function, through conventional centrifuge operation, to remove the crystallized fraction S from the miscella or mother liquor and deliver the former to the Moyno type pump means 136A.
  • the addition of the wash solvent blend to the centrifuge means 120A will enable the washing of the S fraction crystals in addi- 8 tional solvent blend to insure the removal of substantially all of the remaining miscella therefrom.
  • miscella or mother liquor is then introduced to self-thinker type centrifuge means 128A which will operate to remove any remaining, minor quan tities of S fraction crystals from the miscella and effect the delivery thereof to Moyno type pump means 136A through delivery conduit 134A.
  • the crystallized S fraction will be supplied from cold" room A, through Moyno type pump 136A, to the S holding tank 138A, while the miscella or mother liquor, including the additional solvent blend introduced thereto from wash solvent blend holding tank 124A, will be supplied, through conduit 140A, to the inlet of the scraped surface crystallizer 114B of cold room B.
  • fractionation stage 112B Operation of the fractionation stage 112B in cold room B and of fractionation stage 1120 in cold room C will be substantially as described hereinabove for frac tionation stage 112A in cold room A.
  • fractionation stage 112B will function to crystallize, at approximately 60 F., and separate from the miscella a second fraction, hereinafter referred to as S and discharge the same through Moyno type pump means 13613 to S holding tank 138B
  • fractionation stage 112C will function to crystallize, at approximately 50 F., and separate from the miscella a third fraction, hereinafter referred to as S and discharge the same through Moyno type pump means 136C to holding tank 138C.
  • fractionation stage 112C will function to discharge the solvent-blend-diluted residual miscella, hereinafter referred to as S to S holding tank 142 through conduit 140C.
  • the respective separated fractions, 8,, S and S and the residual miscella S are then delivered, through conduits 144, 146, 148 and 150, to solvent stripper means 152 wherein the solvent blend is stripped therefrom and returned, through return conduit 154 and reconstituted solvent tank 157, to the respective wash solvent blend holding tanks 124A 124B and 124C for re-use as described hereinabove.
  • fractions S S S and S the latter are then delivered through conduit 156 to deodorizer means 158 for deodorization in preparation for the use thereof in foodstuffs and/or pharmaceuticals.
  • deodorizer means 158 for deodorization in preparation for the use thereof in foodstuffs and/or pharmaceuticals.
  • the S S S and 5., fractions are delivered by conduit 160 to fraction collection means, as indicated at 162, which may take any form convenient to the collection and packaging of the said fractions.
  • the fraction collection means 162 will include flaking drum means to put the respective fractions S S and S in flake form. for final collection and packaging, it being understood that the 8.; fraction will be in liquid form at the ambient fraction collection point temperatures.
  • the system may be arranged, for example, to first deodorize and deliver for collection frac- 10 Consideration of Report of Analysis I is believed to make clear the eminent suitability of the S and S fractions for use as substitutes for cocoa butter, by making clear the marked similarity therebetween in the critical tion S then fraction S then fraction 8;, and finally fracareas of refractive index and melting point.
  • the S fraction is essentially a tri-saturated fraction and is suitable for all applications wherein hydrogenated flakes and saturated fats of similar nature are utilized. A distinct advantage of the S fraction resides in the fact that it has not been hydrogenated and would thus not contain any isomerized chains as are normally found in hydrogenated fats.
  • the S fraction will have a lower melting point than tri-saturated triglycerides containing isomerized fatty acids and will be particularly useful, for example, as a binder in peanut butter and/or halvah to prevent oil separation, and in candy coatings.
  • the S fraction can satisfactorily perform the functions of hydrogenated oils without giving rise to the elevated melting points encountered with isomerized oils.
  • Fuller discussion of this advantage of the S fraction may be found on page 540A, September Meeting Report of the I. Am. Oil Chemists Soc., vol. 44 of November 1967.
  • the S function is well suited for use as a salad or margarine oil and again, with an iodine value in the range of 60 to 70, offers the significant advantage of having almost no iso acids present since it has also not been hydrogenated.
  • the highly pigmented or carotene liquid layer of the 5.; fraction is, as discussed above, rich in beta carotene and can be used as a highly economical source thereof in the production of beta carotene for use as a food coloring agent.
  • the said carotene liquid, or CL as it is hereinafter referred to can be bleached and incorporated for use as above with the S fraction.
  • the S and S fractions are each, as discussed hereinabove, eminently suited for large scale commercial use as substitutes for cocoa butter at prices well below the current prices for the latter.
  • This eminent suitability of the S and 8;; fractions as cocoa butter substitutes, and further information on the chemical properties of the S S and CL fractions for the respective pscs thereof discussed above, are believed clearly illustrated by the following Report of Analysis I which presents the results of chemical analyses conducted by a highly qualified, independent chemistry laboratory at my request on my samples of the fractions S S S S CL as producediin accordance With the process of my invention as disclosed herein, and two samples of cocoa butter of commercially available grade. Also presented are the AOCS values for cocoa butter.
  • Cocoa butter Sample identification S1 S2 S3 S4 CL A B AOCS Melting point, C. (closed cap.) 60. 2 34. 31. 8 8. 5 11.8 32.1 32. 9 30-35 Iodine value (Wijs) 33.70 60. 65 61. 65 46. 14 47.17 32-40 Unsaponifiables, percent. 0.29 0.60 0.52 1.19 0.62 1 Refractive Index at 40 C 1. 4568 1. 4575 1.4583 1. 456-1. 458
  • triglyceride oils other than palm oil to which the fractionation apparatus and process of my invention are particularly applicable are tallow and fish oils, and other vegetable oils.
  • a process for the separation of one or more fractions from a fatty material in the nature of a fat or fatty acid the steps of, mixing said fatty material with a blend of acetone and isopropanol wherein the latter acts as a diluent to dilute the acetone to form a fatty material-solvent blend miscella, subjecting said miscella to the crystallization temperature of said fraction in said miscella to crystallize the latter, and removing said crystallized fraction from said miscella.
  • said fatty material and blend are mixed in proportions ranging from a ratio of one part by weight of fatty material to two parts by weight of blend, to a ratio of two parts by weight of fatty material to one part by weight of blend.
  • said separation is carried out in three stages with said miscella being initially subjected to a first temperature ranging from 70 F. to 80 F. to crystallize a first fraction for removal therefrom, said miscella minus said first fraction then being subjected to a second temperature ranging from F. to F., to crystallize a second fraction for removal therefrom, and said miscella minus said first and second fractions then being subjected to a third temperature ranging from 45 F. to 55 F. to crystallize a third fraction for removal therefrom.
  • said first temperature is approximately 75 B
  • said second temperature is approximately 60 F.
  • said third temperature is approximately 50 F.
  • miscella being initially subjected to a first temperature ranging from F. to 80 F. to crystallize a first fraction for removal therefrom, said miscella minus said first fraction then being subjected to a second temperature ranging from 55 F. to 65 F. to crystallize a second fraction for removal therefrom, and said miscella minus said first and second fractions then being subjected to a third temperature ranging from 45 F. to 55 F. to crystallize a third fraction for removal therefrom.
  • said first temperature is approximately F.
  • said second temperature is approximately 60 F.
  • said third temperature is approximately 50 F.
  • said fatty material is palm oil.
  • said fatty material is palm oil, and said second and third fractions thereof will constitute a cocoa butter substitute References Cited UNITED STATES PATENTS 7/1953 Pramuk et al 260-419 4/1956 Young et al. 260410.7

Landscapes

  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Wood Science & Technology (AREA)
  • Organic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Microbiology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Fats And Perfumes (AREA)
  • Edible Oils And Fats (AREA)
US729489*A 1968-04-24 1968-04-24 Apparatus and process for the selective fractionation of fatty materials into useful fractions thereof Expired - Lifetime US3632616A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US72948968A 1968-04-24 1968-04-24

Publications (1)

Publication Number Publication Date
US3632616A true US3632616A (en) 1972-01-04

Family

ID=24931276

Family Applications (1)

Application Number Title Priority Date Filing Date
US729489*A Expired - Lifetime US3632616A (en) 1968-04-24 1968-04-24 Apparatus and process for the selective fractionation of fatty materials into useful fractions thereof

Country Status (8)

Country Link
US (1) US3632616A (enrdf_load_stackoverflow)
BE (1) BE731942A (enrdf_load_stackoverflow)
CH (1) CH520191A (enrdf_load_stackoverflow)
DK (1) DK134704B (enrdf_load_stackoverflow)
GB (1) GB1239288A (enrdf_load_stackoverflow)
IL (1) IL30419A (enrdf_load_stackoverflow)
NL (1) NL6906334A (enrdf_load_stackoverflow)
SE (1) SE357208B (enrdf_load_stackoverflow)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS60123597A (ja) * 1983-07-26 1985-07-02 ソシエテ　デ　プロデユイ　ネツスル　ソシエテ　アノニム 脂肪の溶媒分別方法
WO2001057829A1 (en) * 2000-02-07 2001-08-09 Helio Zapata Retractable watch band calendar
US20110052781A1 (en) * 2007-12-21 2011-03-03 Leendert Wijngaarden Process for producing a palm oil product
WO2011092260A3 (de) * 2010-02-01 2011-12-01 Gea Mechanical Equipment Gmbh Fraktionierungsverfahren und fraktionierungsanlage
EP2373177A4 (en) * 2009-01-08 2016-06-15 Sime Darby Res Sdn Bhd REFINEMENT OF EDIBLE OIL

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1497165A (en) * 1975-08-08 1978-01-05 Unilever Ltd Mango kernel fat product

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS60123597A (ja) * 1983-07-26 1985-07-02 ソシエテ　デ　プロデユイ　ネツスル　ソシエテ　アノニム 脂肪の溶媒分別方法
WO2001057829A1 (en) * 2000-02-07 2001-08-09 Helio Zapata Retractable watch band calendar
US20110052781A1 (en) * 2007-12-21 2011-03-03 Leendert Wijngaarden Process for producing a palm oil product
US8414943B2 (en) 2007-12-21 2013-04-09 Loders Croklaan B.V. Process for producing a palm oil product
EP2373177A4 (en) * 2009-01-08 2016-06-15 Sime Darby Res Sdn Bhd REFINEMENT OF EDIBLE OIL
WO2011092260A3 (de) * 2010-02-01 2011-12-01 Gea Mechanical Equipment Gmbh Fraktionierungsverfahren und fraktionierungsanlage

Also Published As

Publication number Publication date
BE731942A (enrdf_load_stackoverflow) 1969-10-01
IL30419A (en) 1972-08-30
DK134704B (da) 1976-12-27
NL6906334A (enrdf_load_stackoverflow) 1969-10-28
CH520191A (de) 1972-03-15
DK134704C (enrdf_load_stackoverflow) 1977-05-23
IL30419A0 (en) 1968-09-26
SE357208B (enrdf_load_stackoverflow) 1973-06-18
GB1239288A (enrdf_load_stackoverflow) 1971-07-14

Similar Documents

Publication Publication Date Title
Rossell Fractionation of lauric oils
EP2242826B1 (en) Process for producing a palm oil product
Timms Fractionation
CN102655762A (zh) 用于糖食的高熔点向日葵脂肪
US2815285A (en) Method of making stable pourable oleaginous suspensions
US6069263A (en) Process for dry fractionation of fats and oils
US4217372A (en) Method for improving the structural properties of fats
US3632616A (en) Apparatus and process for the selective fractionation of fatty materials into useful fractions thereof
Young Interchangeability of fats and oils
US3093480A (en) Process for the preparation of cocoa butter substitutes
US2853390A (en) Process for shortening manufacture
EP1028159A1 (en) Method of dry-fractionating fat and stationary crystallization apparatus
US2797164A (en) Process for margarine manufacture
DE2814211A1 (de) Verfahren zum fraktionieren von talg und herstellung eines kakaobutter aehnlichen, plastischen fetts
DE102012110970A1 (de) Kontinuierliche Fraktionierung von Triglyceridölen
EP3227418B1 (en) Continuous process for dry fractionation of glyceride oils
US4276227A (en) Method of treating edible oil with alkali using interfacial surface mixer
Cavanagh Miscella refining
US2910363A (en) Method for the fractional crystallization of cottonseed oil
US3733343A (en) Continuous process for the separation of mixtures of fatty acid esters of different melting points
US2564407A (en) Purified oils and processes of preparing same
US5210241A (en) Process for preparing cocoa butter equivalent from semi-refined nontoxic Chinese Vegetable Tallow
US2875067A (en) Lard shortenings
US2325393A (en) Manufacture of margarine and cooking fats
AU2021234620B2 (en) Dry fractionation of edible oil