Method of producing estolide having high structural stability

Abstract

Disclosed is a method of producing an estolide having high structural stability, including: a) preparing a fatty acid mixture from biomass-derived oil; b) separating the fatty acid mixture into a C16 fatty acid and a C18 fatty acid; c) converting the C18 fatty acid into a C18 or C17 linear internal olefin; and d) subjecting the C18 or C17 linear internal olefin and the C16 fatty acid to an estolide reaction, thus obtaining an estolide.

Claims

1. A method of producing an estolide having high structural stability, comprising: a) preparing a fatty acid mixture comprising C4 to C24 from biomass-derived oil; b) separating the fatty acid mixture into a C16 fatty acid and a C18 fatty acid, respectively; c) converting the separated C18 fatty acid into a C18 or C17 linear internal olefin; and d) subjecting the C18 or C17 linear internal olefin and the separated C16 fatty acid to an estolide reaction, wherein the estolide reaction is a crosslinking reaction of unsaturated double bonds of hydrocarbons with a fatty acid using an acid catalyst, thus obtaining an estolide.

2. A method of producing an estolide having high structural stability, comprising: A) preparing a fatty acid mixture comprising C4 to C24 from biomass-derived oil; and B) subjecting the fatty acid mixture to an estolide reaction and then hydrodeoxygenation, wherein the estolide reaction is a crosslinking reaction of unsaturated double bonds of hydrocarbons with a fatty acid using an acid catalyst, thus obtaining an estolide.

3. The method of claim 1, wherein c) comprises converting the C18 fatty acid into a C18 linear internal olefin through partial hydrogenation and dehydration.

4. The method of claim 1, wherein c) comprises converting the C18 fatty acid into a C17 linear internal olefin through decarbonylation.

5. The method of claim 1, further comprising e) performing hydrotreating to increase stearic acid content, between steps a) and b).

6. The method of claim 1, further comprising f) hydrotreating the C18 fatty acid separated in b) to increase stearic acid content, between steps b) and c).

7. The method of claim 2, further comprising C) performing hydrotreating to increase stearic acid content, after A).

8. The method of claim 2, further comprising D) separating or purifying the estolide obtained in B) to obtain a desired estolide.

9. The method of claim 1, wherein a) or A) is performed through de-esterification or hydrolysis of triglyceride in the biomass-derived oil.

10. The method of claim 2, wherein a) or A) is performed through de-esterification or hydrolysis of triglyceride in the biomass-derived oil.

11. An estolide, produced by the method of claim 1, wherein the estolide comprises an estolide represented by Chemical Formula 1 or Chemical Formula 2 below: ##STR00003##

12. An estolide, produced by the method of claim 2, wherein the estolide comprises an estolide represented by Chemical Formula 1 or Chemical Formula 2 below: ##STR00004##

13. A lubricating oil, comprising an estolide produced by the method of claim 1, wherein the estolide comprises an estolide represented by Chemical Formula 1 or Chemical Formula 2 below: ##STR00005##

14. A lubricating oil, comprising an estolide produced by the method of claim 2, wherein the estolide comprises an estolide represented by Chemical Formula 1 or Chemical Formula 2 below: ##STR00006##

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) FIG. 1 schematically illustrates a production process according to an embodiment of the present invention;

(2) FIG. 2 schematically illustrates a production process according to another embodiment of the present invention;

(3) FIG. 3 schematically illustrates a production process according to still another embodiment of the present invention; and

(4) FIGS. 4 and 5 illustrate the results of SimDist analysis of the C18 linear internal olefin obtained from a stearyl alcohol feed in Example 1 using an r-Al.sub.2O.sub.3 catalyst.

DESCRIPTION OF SPECIFIC EMBODIMENTS

(5) Hereinafter, a detailed description will be given of embodiments of the present invention. Such embodiments are merely illustrative, but are not to be construed as limiting the present invention.

(6) In an embodiment of the present invention, a method of producing estolide having high structural stability comprises a) preparing a fatty acid mixture from biomass-derived oil; b) separating the fatty acid mixture into C16 and C18 fatty acids; c) converting the C18 fatty acid into C18 or C17 linear internal olefin; and d) subjecting the C18 or C17 linear internal olefin and the C16 fatty acid to an estolide reaction, thus obtaining an estolide.

(7) In an exemplary embodiment referring to FIG. 1, the method of producing an estolide having high structural stability includes converting biomass-derived oil into a fatty acid mixture comprising C16 and C18 fatty acids. Then, the fatty acid mixture is separated into C16 fatty acid and C18 fatty acid, the separated C18 fatty acid is converted into C18 saturated fatty alcohol through partial hydrogenation, and the C18 saturated fatty alcohol is converted into C18 linear internal olefin through dehydration. Then, the C18 linear internal olefin and the separated C16 fatty acid are subjected to an estolide reaction, yielding an estolide.

(8) In an exemplary embodiment referring to FIG. 2, hydrotreating the fatty acid mixture may be further performed, unlike the embodiment of FIG. 1.

(9) Conversion of Biomass-Derived Oil Into Fatty Acid

(10) A biomass-derived oil component mainly contains triglycerides and fatty acids. Triglycerides are present in the form of three fatty acids that are ester-linked to glycerol. As such, the ratio (by weight) of triglyceride to fatty acid in the biomass-derived oil is, for example, about 100:1 to 6:1, particularly about 20:1 to 6:1, and more particularly about 10:1 to 6:1, and may vary depending on the source of biomass and is not necessarily limited to the above numerical ranges. More typically, triglyceride may constitute about 90 to 95 wt % of biomass-derived oil.

(11) Also, the carbon chain of triglyceride is approximately composed of C4 to C24, and more typically of C16 and C18. Such triglycerides, or some mono- and di-glycerides, may be converted into mixed C16 and C18 fatty acids through de-esterification, as represented by Scheme 1 below.

(12) ##STR00002##

(13) De-esterification, illustrated as above, is a typical reaction for preparing fatty acid methyl ester (FAME) from biomass.

(14) In an exemplary embodiment, de-esterification enables the conversion of triglyceride into fatty acid in the presence of a strong acid (e.g. H.sub.2SO.sub.4, HNO.sub.3, HCl, HBr, HI, HClO.sub.4, HClO.sub.3, HBrO.sub.4, HBrO.sub.3, HIO.sub.4, HIO.sub.3, etc.) or a strong base (e.g. NaOH, KOH, Ca(OH).sub.2, an amine compound, etc.) or steam at high temperature (typically about 100 to 300° C., and more typically about 100 to 200° C.).

(15) Also, ester bonds of triglycerides may be hydrolyzed, thus affording fatty acids. In addition, various reactions for converting triglycerides into fatty acids as known in the art may be adopted without particular limitation.

(16) Separation of C16 and C18 Fatty Acids

(17) The biomass-derived oil contains various kinds of saturated fatty acids and unsaturated fatty acids. Examples of fatty acids derived from palm oil may include myristic acid, palmitic acid, oleic acid, linoleic acid, linolenic acid, monoglyceride, and diglyceride. Various kinds of fatty acids have different boiling points, whereby desired fatty acids may be selectively extracted and separated through fractional distillation.

(18) Thus, the converted biomass-derived fatty acids may be separated and extracted into C16 fatty acid and C18 fatty acid through fractional distillation. The C16 fatty acid may be palmitic acid, and the C18 fatty acid may include stearic acid, oleic acid, linoleic acid, linolenic acid, or a combination thereof.

(19) Hydrotreating

(20) In an embodiment of the present invention, hydrotreating may be further performed after a) or b), whereby stearic acid content may be increased.

(21) Specifically, this process is related to converting C18:2 (linoleic acid), C18:3 (linolenic acid), or C18:1 (oleic acid), of the biomass-derived oil, into C18:0 (stearic acid).

(22) When using hydrotreating at high temperature under high pressure, unsaturated double bonds may be completely converted into C18:0 (stearic acid).

(23) For example, a catalyst for use in a hydrotreating reaction may be configured such that NiMo, CoMo, or Mo metal is loaded on a water-resistant carrier. The reaction may be carried out under conditions of about 250 to 300° C. and about 20 to 30 bar.

(24) Under typical hydrogenation conditions of 300° C. or higher and hydrogen pressure of 40 bar or more, a carboxyl functional group is removed. Hence, hydrotreating according to the present process for selectively removing only unsaturated double bonds may be carried out under mild operating conditions. More specifically, under conditions of about 250 to 300° C. and about 20 to 30 bar using a NiMo/ZrO.sub.2 catalyst, the C18 fatty acid having unsaturated double bonds may be converted into stearic acid.

(25) As such, the catalyst and reaction conditions for hydrotreating are not limited thereto, and any hydrotreating conditions known in the art may be utilized so long as the C18 unsaturated fatty acid of the biomass-derived oil may be converted into the C18 saturated fatty acid.

(26) The hydrotreating process according to the present invention is different from a conventional hydrotreating process in terms of the peculiarities of biomass itself. Biomass has very high oxygen content compared to crude oil. When oxygen is removed through the hydrotreating reaction, such oxygen may be removed in the form of H.sub.2O by the reaction with hydrogen, thus melting the active metal and the carrier of the catalyst, undesirably seriously causing the inactivation of the catalyst. Hence, hydrotreating of biomass may be seriously problematic because the catalyst may be inactivated due to the water byproduct. In the present technique, a water-resistant carrier such as ZrO.sub.2, TiO.sub.2, etc. is used, thereby overcoming the problem of inactivation of the catalyst owing to catalyst leaching.

(27) Even when some of the unsaturated double bonds of the olefins may remain under the above reaction conditions, all fatty acids having unsaturated double bonds are converted into saturated fatty acids through recycling treatment. Therefore, the suppression of side reactions is regarded as more important than the reaction yield.

(28) Conversion into C18 or C17 Linear Internal Olefin

(29) The conversion of the separated C18 fatty acid into C18 or C17 linear internal olefin is described below.

(30) The reactions for conversion into linear internal olefin may be largely classified into two types.

(31) One type of reaction is carried out in a way such that fatty acid is converted into alcohol through hydrogenation, and then into linear internal olefin through dehydration. As such, since 2 mol of H.sub.2 are fed per 1 mol of fatty acid to remove 2 mol of H.sub.2O to thereby prepare 1 mol of linear internal olefin, there is no weight reduction, and all of the processes used are fixed-bed processes, making it possible to achieve mass production. The reaction for producing fatty alcohol may operate using a Cu-based partial hydrogenation catalyst under conditions of about 200 to 400° C., H.sub.2 pressure of about 20 to 100 bar, WHSV of about 0.05 to 10 h.sup.−1, and a gas oil ratio (GOR) of about 50 to 5000, so that fatty acid is converted into fatty alcohol. Using a typical metal oxide catalyst for dehydration, the reaction is carried out under conditions of about 200 to 500° C., N.sub.2 pressure of about 1 to 30 bar, WHSV of about 0.05 to 10 h.sup.−1, and GOR of about 50 to 5000, yielding linear internal olefin.

(32) The other type of reaction for preparing linear internal olefin is to use decarbonylation. Decarbonylation is carried out in a way such that two fatty acid molecules are converted into a fatty acid anhydride and one molecule of each of CO and H.sub.2O is removed, thereby yielding one molecule of linear internal olefin and one molecule of fatty acid. Mainly using a Fe-triphenyl phosphine chelate catalyst, linear internal olefin is prepared under conditions of 120 to 300° C. and N.sub.2 or CO pressure of 1 to 70 bar in a batch reactor. In order to increase the decarbonylation activity, when a salt such as NaCl, KCl, NaI, or KI is added, the halogen material participates as the chelating agent of the catalyst, thereby accelerating the conversion into linear internal olefin. In order to remove water produced during the reaction and to accelerate the decarbonylation reaction rate, light acid is added in the form of an anhydride. Since the produced linear internal olefin is a material produced via decarbonylation, it has a number of carbons lower by 1 than the original number of carbons. This reaction has no large initial investment cost because the yield of linear internal olefin is high and a batch reactor is used.

(33) When using the above two exemplary methods, linear internal olefin may be prepared, and the conversion into linear internal olefin is not necessarily limited thereto. Also, the type of preparation of linear internal olefin may be adopted depending on the need and industrial scale.

(34) Production Reaction of Estolide

(35) Estolide is synthesized through the estolide reaction between the C16 fatty acid and the C18 or C17 linear internal olefin.

(36) A typical reaction for producing estolide is carried out using an acid catalyst. The acid for use in the catalyst is mainly a strong acid, such as H.sub.2SO.sub.4 or HClO.sub.4, and an acid having intermediate strength such as formic acid may be used, but more severe conditions are required. The estolide reaction does not occur as rapidly as typical oligomerization and alkylation, thus causing no side reactions, and taking a long period of time under the estolide reaction conditions, thereby increasing the estolide yield. The experimental parameters for producing estolide include not only acidity, acid value, and temperature, but also reaction time and stirring rate. Although estolide is produced within several hours, the yield thereof is not high, and thus the reaction time is typically set to 12 hours or more. Furthermore, the stirring rate is regarded as very important. As the stirring rate is increased, the reaction may become more efficient. The reaction pressure is also important. Thus, the production of estolide at low reaction pressure is adopted because changes in color of the product may decrease and the yield may increase, but a vacuum unit is required.

(37) A conventional method of producing estolide includes adding an acid catalyst to oleic acid and preparing estolide, which is then subjected to esterification with alcohol such as methanol without additional cutting, yielding a final estolide product. Accordingly, not only oleic acid dimer type estolides but also trimer or higher estolides may be produced simultaneously, and thus the product may be provided in the form of a mixture. Furthermore, since the ratio thereof is difficult to adjust, the produced materials have to be separately used, or the conditions for preparing reproducible mixtures have to be ensured.

(38) The estolide reaction is typically carried out at a reaction temperature of 45 to 300° C. When a vacuum is applied, the estolide reaction is induced in the temperature range of −20 to 30° C. depending on the strength of the vacuum. Furthermore, the reaction can be induced using 0.01 to 20 wt % of an acid catalyst relative to the feed. The reaction for producing estolide is conducted under conditions of a reaction time of 0.5 to 48 hr, and a stirring rate of 50 to 2000 rpm.

(39) With reference to FIG. 3, biomass-derived oil is converted into a fatty acid mixture. Then, the fatty acid mixture is sequentially subjected to estolide reaction and hydrodeoxygenation, thus obtaining an estolide. As necessary, separating or purifying the estolide to isolate a desired estolide may be further performed.

(40) The preparation of the fatty acid mixture from the biomass-derived oil is as described above. The fatty acid mixture may be a mixture of C16 fatty acid and C18 fatty acid, and may be subjected to an estolide reaction. To this end, the aforementioned estolide reaction may be applied. Below is a description of hydrodeoxygenation.

(41) Hydrodeoxygenation

(42) The catalyst for use in hydrodeoxygenation is configured such that NiMo, CoMo, or Mo metal is loaded on a water-resistant carrier. The reaction may be carried out under conditions of about 150 to 300° C. and H.sub.2 pressure of about 10 to 30 bar, particularly about 170 to 250° C. and H.sub.2 pressure of about 15 to 25 bar, and more particularly about 180° C. and H.sub.2 pressure of about 20 bar, rather than typical hydrogenation conditions of high temperature of 250° C. or more and high pressure of 40 bar or more.

(43) Upon hydrodeoxygenation, the reaction conditions are appropriately controlled, so that an ester functional group is left behind, and only a carboxyl functional group, which is externally exposed, is selectively removed. Such a selective reaction may be carried out by controlling the reaction conditions. When the reaction temperature is 350° C. or higher, ester is broken and is thus converted into linear paraffin. Hence, the reaction is conducted at about 200 to 250° C., at which carboxylic acid begins to be removed, and unreacted carboxylic acid may be recycled, thereby removing all carboxylic acids.

(44) A better understanding of the present invention may be obtained via the following examples which are set forth to illustrate, but are not to be construed as limiting the present invention.

EXAMPLE 1

(45) 1512 g of palm fatty acid distillate (PFAD) as a byproduct of biomass-derived oil was cut at a boiling point of 360° C., thus obtaining 807 g of C18 unsaturated fatty acid. Through analysis of SimDist and GC-MS thereof, the ratios of C18:0, C18:1, C18:2, and C18:3 were measured. The results are shown in Table 2 below. The obtained PFAD-derived C18 unsaturated fatty acid was subjected to partial hydrogenation using a NiMo/ZrO.sub.2 catalyst, and was thereby converted into C18 saturated fatty acid. The NiMo/ZrO.sub.2 catalyst was prepared as follows.

(46) Specifically, the catalyst was prepared by loading about 10 wt % of Mo and about 3 wt % of Ni on a ZrO.sub.2 carrier having a diameter of 1 mm. The Mo precursor was ammonium heptamolybdate tetrahydrate (AHM), and the Ni precursor was nickel nitrate hexahydrate (NNH). Mo and Ni were fed using various precursors, but the invention is not limited thereto.

(47) Specifically, an aqueous solution of AHM dissolved in deionized (DI) water was incorporated in a ZrO.sub.2 carrier, dried at 150° C. for 2 hr, and continuously burned at 500° C. for 2 hr, thus obtaining Mo/ZrO.sub.2.

(48) Then, NNH was dissolved in DI water, impregnated with the Mo/ZrO.sub.2 catalyst, dried at 150° C. for 2 hr, and continuously burned at 500° C. for 2 hr, yielding the NiMo/ZrO.sub.2 catalyst.

(49) 6 cc of the catalyst thus prepared was placed in a cylindrical reactor, loaded with an R-LGO feed at a rate of 0.08 cc/min at room temperature, heated to 320° C. under conditions of a reaction pressure of 45 bar and H.sub.2 flow rate of 16 cc/min, and pretreated for 3 hr at 320° C.

(50) 6 g of the NiMo/ZrO□ catalyst thus pretreated was placed in a fixed-bed reactor, after which 807 g of the PFAD-derived C18 feed and 8.1 g of dimethyl disulfide (DMDS) were reacted at a rate of 0.1 cc/min (LHSV=1) under conditions of a reaction temperature of 240° C., a reaction pressure of 20 bar, and H.sub.2 flow rate of 100 cc/min. The feed bottle was maintained at 70° C., and the reaction mixture was stirred and retained in a liquid phase. Sampling was conducted at 8-hr intervals, and the properties of the obtained products were measured through GC-MS, and the leaching of the catalyst was checked using ICP.

(51) Based on the results of analysis of GC-MS, almost all of the unsaturated fatty acids were able to be converted into saturated fatty acids. Although C18:1 (oleic acid) was left behind in an amount of about 25%, it was able to be converted into C18:0 (stearic acid) through recycling treatment.

(52) TABLE-US-00002 TABLE 2 A series A, Feed A A, 240-20 Myristic acid (14:0) 0.0 0.0 Palmitic acid (16:0) 0.0 0.6 Stearic acid (18:0) 6.8 74.6 Oleic acid (18:1) 78.8 24.8 Linoleic acid (18:2) 12.2 0 Linolenic acid (18:3) 2.2 0

(53) Conversion of Stearic Acid into Stearyl Alcohol

(54) Stearic acid was converted into stearyl alcohol using a fixed-bed reactor containing a CuCr/Al.sub.2O.sub.3 catalyst. Specifically, 6 g of a commercially available CuCr/Al.sub.2O.sub.3 catalyst was placed in a fixed-bed reactor, the top and bottom of the catalyst were closed with glass wool, the remaining portion of the reactor was filled with silica beads, and a thermocouple was disposed so as to be in contact with the catalyst. The reaction temperature was increased to about 400° C. at a rate of about 5° C./min under conditions of N.sub.2 flow rate of about 200 sccm and H.sub.2 flow rate of 200 sccm, and was then maintained for about 3 hr at a reaction pressure of about 50 bar. Thereafter, the reaction temperature was decreased to about 300° C., after which the mixed solution of C18 fatty acid and ethanol at a molar ratio of 1:5 was fed at about 0.13 sccm, and the reactor was operated at a space velocity (WHSV) of about 1 hr.sup.−1. Draining for the first 16 hr and then sampling at 8-hr intervals were performed, and hydrogenation activity and selectivity were measured. The reaction activity was measured at about 300° C., after which changes in the reaction activity were checked depending on changes in the reaction temperature and pressure. The stabilized product pattern results, observed two days after changes in the reaction conditions, were adopted, taking reaction stability into consideration. The conversion efficiency of the product was measured via SimDist analysis. The product selectivity and the presence or absence of side reactions were measured via GC-MS and SimDist analysis. The results are shown in Table 3 below.

(55) TABLE-US-00003 TABLE 3 CuCr/Al.sub.2O.sub.3 Sample ID 47 39 28 58 Reaction conditions Temp. (° C.) 320 320 360 320 H.sub.2 pressure (bar) 50 40 40 40 H.sub.2 flow rate (sccm) 200 200 200 100 Product pattern (%) C17, C18 Paraffin 0 0 0 0 C18 Alcohol 83 79 46 67 C18 Acid 4 13 21 11 C18 α-olefin 0 0 0 4 C18 Acid-ethyl ester 13 8 7 19 Others 0 0 25 0

(56) As is apparent from Table 3, the CuCr/Al.sub.2O.sub.3 catalyst exhibited high conversion efficiency of C18 fatty acid and high selectivity of C18 alcohol. The yield of C18 alcohol was 80% or more under conditions of a reaction temperature of about 320° C., H.sub.2 pressure of 50 bar, and H.sub.2 flow rate of 200 sccm. As such, side reactions did not occur. However, as the reaction temperature was increased (to 360° C. or higher), side reactions such as the formation of heavy hydrocarbons occurred, and the conversion efficiency was somewhat decreased. Furthermore, when the H.sub.2 flow rate was lowered and thus the catalyst retention time of the reaction feed was increased, a small amount of C18 linear α-olefin was produced. However, this amount was very low, about 4%, thus making it possible to apply the above product industrially.

(57) Evaluation of Dehydration Activity of Stearyl Alcohol

(58) Stearyl alcohol was evaluated for dehydration activity in the presence of an alumina catalyst using a fixed-bed reactor. Specifically, 6 g of an alumina catalyst was placed in a fixed-bed reactor, the top and bottom of the catalyst were closed with glass wool, the remaining portion of the reactor was filled with silica beads, and a thermocouple was disposed so as to be in contact with the catalyst. The alumina had a surface area of about 260 m.sup.2/g, an average pore size of about 10 nm, and a total pore volume of about 0.83 cc/g. The reactor was heated at a rate of 5° C./min under conditions of N.sub.2 pressure of about 5 bar and N.sub.2 flow rate of about 100 sccm, and was maintained at about 500° C. for 3 hr, whereby water was removed from the surface of the catalyst or the adsorbed gas was removed. Thereafter, the temperature was lowered to about 300° C., and a mixture comprising C18 fatty alcohol and n-heptane at a molar ratio of 6:4 was fed at 0.13 sccm, and the reactor was operated at a space velocity (WHSV) of about 1 hr.sup.−1. Draining for the first 16 hr and then sampling at 8-hr intervals were performed, and the conversion activity of linear internal olefins and the selectivity thereof were measured. The C18 linear internal olefin was prepared at 400° C. and the properties thereof were measured. The stabilized product pattern results, observed two days after changes in the reaction conditions, were adopted, taking reaction stability into consideration. The conversion efficiency of the produced linear internal olefin was measured through SimDist analysis.

(59) Based on the dehydration results, it was possible to convert the stearyl alcohol into C18 linear internal olefin at a high conversion efficiency of 95% or more. The remainder, comprising less than 5%, was determined to be an ester intermediate via GC-MS.

(60) The results of SimDist analysis of the stearyl alcohol feed, obtained through the experiment, and the C18 linear internal olefin, obtained using the r-Al.sub.2O.sub.3 catalyst, are shown in FIGS. 4 and 5.

(61) The purchased C18 linear α-olefin and the C18 linear internal olefin obtained in Example 1 were analyzed to determine the pour point and cloud point. The results are shown in Table 4 below.

(62) TABLE-US-00004 TABLE 4 Pour point/Cloud point (° C./° C.) C18 linear α-olefin 18/20 C18 linear internal olefin −14/−13

(63) Production of Estolide

(64) 100.3 g of the C18 linear internal olefin thus obtained and 82.2 g of palmitic acid were placed in a 500 cc flask, after which a stirring rod, a thermometer, and a cooling trap were connected thereto, and the mixture was stirred at 800 rpm and then heated to 210° C. When the reaction temperature reached 210° C., 9.2 g of sulfuric acid was added in droplets to the reaction system of the reactor. The sulfuric acid used was purchased from Across, and had a purity of 96% (in water). 3 hr after the addition of H.sub.2SO.sub.4, the operation was terminated and the reaction product was allowed to stand until it reached room temperature.

(65) After termination of the reaction, the product was filtered, and unreacted palmitic acid was separated. The amount of the separated palmitic acid was 60.7 g. 119.8 g of the remaining solution was placed in a 4 L reactor, and a mixture comprising 963 g of methanol and 27.5 g of sulfuric acid was added. The above sulfuric acid product, made by Across, was used, and methanol made by SamChun Chemical, having a purity of 99.8%, was used. Thereafter, the temperature of the reactor was raised to 75° C. and maintained for 3 hr. Thereafter, the reaction was terminated, and the reaction product was allowed to stand until it reached room temperature.

(66) In order to obtain a final product, the product was recovered, and the acidity thereof was checked using a mixed aqueous solution of KOH/ethanol (KOH/EtOH/DI water=0.1 g/30 g/1975 g). The mixed solution having no remaining acid was placed in a separatory funnel and allowed to stand. When the organic layer and the water layer containing salt and alcohol were separated in the separatory funnel, the water layer was removed, and the organic layer was isolated, from which the remaining salt and acid were then removed using 2 L of DI water. The amount of the organic layer was 120.5 g.

(67) The yield of the product was measured through SimDist analysis of the organic layer. The results are shown in Table 5 below.

(68) TABLE-US-00005 TABLE 5 Product Wt % C18:1 Linear internal olefin 42 C16:0 Palmitic acid 34 Estolide (ester) 21 Estolide (acid) 3

(69) The obtained organic layer was further treated using a fractional distillation unit (Spaltrohr HMS 300 C; Fischer technology), and was cut on the basis of the boiling point, thereby separating the final product in estolide ester form. The amount of the finally obtained estolide ester material was 34.8 g.

(70) Analysis of Properties of Estolide

(71) In order to evaluate the applicability of the estolide produced in Example 1 as a lubricating oil, the properties thereof were analyzed for PP, viscosity (40° C., 100° C.), and iodine value, from which viscosity index (VI) was then calculated. The analyzed and calculated properties of estolide as lubricating oil are shown in Table 6 below.

(72) TABLE-US-00006 TABLE 6 Viscosity Viscosity at 40° C. at 100° C. Pour point Iodine value Estolide (Cst) (Cst) VI (° C.) (cg/g) Example 1 22.25 4.93 153.2 −23 0.01

(73) The estolide produced through the experiment exhibited very high VI, and had almost none of the remaining unsaturated double bonds. The pour point thereof was about −23° C., which made it suitable for use as lubricating oil. However, such estolide has very high VI compared to typical Group III base oil, and is thus regarded as good lubricating base oil.

EXAMPLE 2

(74) Conversion of Fatty Acid Into Estolide

(75) 450.9 g of PFAD was placed in a 2 L reactor, stirred at 800 rpm, and heated to 210° C. When the reaction temperature reached 210° C., 22.5 g of sulfuric acid was added in droplets to the reaction system of the reactor. 3 hr after the addition of sulfuric acid, the operation was terminated. When the reaction temperature reached 70° C., the reaction product was placed in a 1 L glass bottle.

(76) The product was cut on the basis of 400° C. using a fractional distillation unit (Spaltrohr HMS 300 C; Fischer technology), so that the estolide product was separated from the unreacted material and sulfuric acid.

(77) The amount of the unreacted material, which was separated through fractional distillation from the product, was 186.1 g, and the amount of the product recovered as a material having a boiling point of 400° C. or higher was 250.4 g.

(78) 250.4 g of the recovered product was subjected to hydrodeoxygenation, yielding a final estolide product. The NiMo/ZrO.sub.2 catalyst of Example 1 was loaded and pretreated in the same manner as in Example 1, followed by hydrodeoxygenation. The reaction conditions were the same as in Example 1, with the exception that the reaction temperature was set to 280° C. 8-hr sampling was performed, and the obtained product was recovered, and cut on the basis of 490° C. using a fractional distillation unit (Spaltrohr HMS 300 C; Fischer technology), thereby separating a final product having no carboxyl functional group from the unreacted estolide feed.

(79) The amount of the final product obtained through fractional distillation was 135.8 g, and the amount of the unreacted estolide feed recovered as the material having a boiling point of 490° C. or higher was 62.1 g.

(80) Based on the results of SimDist analysis, the final product was composed of a total of five components, wherein the amount of the material having a boiling point of 450° C. or less, regarded as the dimer of C16 and C18 fatty acids, was 68 wt % (21% and 47%), and the amount of the material having a boiling point of 450° C. or more, regarded as the trimer or higher, was 32 wt % (16%, 4%, 5%, remainder of 7%).

(81) Analysis of Properties of Estolide

(82) In order to evaluate the applicability of the estolide produced in Example 2 as a lubricating oil, the properties thereof were analyzed for PP, viscosity (40° C., 100° C.), and iodine value, from which the VI was then calculated. The analyzed and calculated properties of the estolide as lubricating oil are shown in Table 7 below.

(83) TABLE-US-00007 TABLE 7 Viscosity Viscosity at 40° C. at 100° C. Pour point Iodine value Estolide (Cst) (Cst) VI (° C.) (cg/g) Example 2 31.79 5.85 129.1 −29 0.01

(84) The estolide produced in Example 2 had improved pour point compared to the estolide product of Example 1, but the viscosity index thereof was significantly decreased. As for the properties as lubricating oil, the estolide of Example 2 exhibits higher VI and pour point than those of typical Group III base oil, and is thus regarded as good lubricating base oil.

(85) The reason why the product is different from that produced in Example 1 is that the viscosity at 100° C. is greatly increased to 5.85, and thus the mixture of trimers or higher is produced, and C18:2 and C18:3 may participate in the estolide reaction, so that the estolide reaction is carried out not at the center position but at the unsaturated double bond adjacent to the center position, thus reducing the structure regularity. For this reason, the viscosity at 100° C. was further increased, and the viscosity index was remarkably decreased. Due to the effect of the material comprising trimers or higher, the pour point is considered to be much lower.

(86) Although the embodiments of the present invention have been disclosed for illustrative purposes, those skilled in the art will appreciate that the present invention may be embodied in other specific ways without changing the technical spirit or essential features thereof. Therefore, the embodiments disclosed in the present invention are not restrictive but are illustrative.