US20130131408A1

Movatterモバイル変換

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Publication number: US20130131408A1
Application number: US13/742,991
Authority: US
Inventors: Ramin Abhari; H. Lynn Tomlinson; Vladimir Gruver
Original assignee: Syntroleum Corp
Current assignee: REG Synthetic Fuels LLC
Priority date: 2008-12-10
Filing date: 2013-01-16
Publication date: 2013-05-23
Also published as: US20120238791A1; US20100145114A1; US20200299210A1; US11623899B2; US20230219867A1; US20180290946A1; US20250051247A1; US10717687B2; US20210371356A1; US12049434B2; US20160264491A1; US8231804B2; US20140081057A1; US9963401B2; US11097994B2

Abstract

Paraffin compositions including mainly even carbon number paraffins, and a method for manufacturing the same, is disclosed herein. In one embodiment, the method involves contacting naturally occurring fatty acid/glycerides with hydrogen in a slurry bubble column reactor containing bimetallic catalysts with equivalent particle diameters from about 10 to about 400 micron. The even carbon number compositions are particularly useful as phase change material.

Description

CROSS-REFERENCE TO RELATED PATENT APPLICATIONS

This application is a Continuation of U.S. application Ser. No. 13/466,813, filed May 8, 2012, which is a Divisional of U.S. application Ser. No. 12/331,906, now U.S. Pat. No. 8,231,804, filed Dec. 10, 2008, all of which are incorporated herein by reference, in their entireties, for any and all purposes.

BACKGROUND OF THE INVENTION

1. Field of the Invention

The present invention relates to producing specialty materials and chemical intermediates from bio-renewable feedstocks such as animal fats, plant oils, algal oils, bio-derived greases, and tall oil fatty acid (hereafter referred to as biological feedstocks, or alternatively, fatty acids and/or glycerides depending upon the composition of the feedstock). Specifically, the present invention relates to predominantly even carbon number paraffin compositions in the C₁₂-C₂₄range, and the catalytic hydrogenation/hydrogenolysis method used for its manufacture.

Paraffins in the C₁₂-C₂₄range have useful applications as phase change material (PCM). The paraffins undergo solid-liquid phase transition in the about −9° C. (15° F.) to about 50° C. (120° F.). Heat is absorbed as the PCM paraffin melts and heat is released later when the PCM freezes. Fabricated systems that use PCM's as such are referred to as passive thermal storage devices. Due to relatively high latent heats of solid-liquid phase transition (referred to simply as latent heats hereafter), as well as compatibility with common material of construction and high stability, paraffins are considered particularly well-suited for PCM applications. Wall boards of a house impregnated with a PCM are an example of a passive thermal storage device. During a hot day, the PCM will absorb heat as it melts. Since there is no temperature change during phase transition, the surface in contact with the thermal storage device stays at constant temperature until all PCM therein has melted. The heat that would have made the house hot has thus been stored in the molten PCM. At night, as the temperatures get cooler, the molten PCM freezes and releases the heat thus preventing the home from getting cold. The melting-freezing cycles moderate the temperature of the space enclosed within the passive thermal storage device despite extreme night-day temperature swings outside. In general, PCMs are an effective way of storing thermal energy (e.g. solar, off-peak electricity, industrial waste heat), and reducing energy demand (e.g. for heating and air-conditioning).

The thermal storage capacity of the PCM is dictated by its latent heat. The higher the latent heat, the higher the thermal storage capacity of the PCM, and the smaller the required thermal storage device size/cost.

Table 1 provides the latent heats and melting points of paraffins. As observed therein, the latent heat for even carbon number paraffins is higher than the latent heat for odd carbon number paraffins of similar transition temperature. For example, n-heptadecane (carbon number 17) and n-octadecane (carbon number 18) melt in the 22-28° C. range. Whereas the latent heat of n-heptadecane is 215 kJ/kg and the latent heat for n-octadecane is 245 kJ/kg or 14% higher. In general, the even carbon number paraffin heats of fusion in the C₁₄-C₂₄range are 10-16% higher than odd carbon number paraffins.

TABLE 1

Latent Heats and Solid-Liquid Transition
Temperatures of Selected Paraffins

	Carbon	Melting Point	Latent Heat
Name	Number	(° C.)	(kJ/kg)

n-Tetradecane	14	4.5-5.6	231
n-Pentadecane	15	10	207
n-Hexadecane	16	18.2	238
n-Heptadecane	17	22	215
n-Octadecane	18	28.2	245
n-Nonadecane	19	31.9	222
n-Eicosane	20	37	247
n-Heneicosane	21	41	215
n-Docosane	22	44	249
n-Tricosane	23	47	234
n-Tetracosane	24	51	255

In addition to PCM applications, even carbon number C₁₂-C₂₄paraffins are also used as chemical intermediates for linear alkyl benzene (C₁₂, C₁₄) and alkyenyl succinate (C₁₆, C₁₈), as well as lubricant/wax additives.

2. Brief Description of the Related Art

The commercially practiced synthesis of even carbon number n-paraffins involves ethylene oligomerization. Depending on the catalyst and reactor operating conditions, this process produces a distribution of linear alpha olefins in the C₄to C₂₀+ range. Linear alpha olefins in the C_4-C8range are the main products of this process and are separated. These olefins are in high demand, mainly as comonomers for film-grade polyethylene. The C₁₀+ even carbon number olefins are sold as intermediates for specialty chemicals, or hydrogenated to produce even carbon number n-paraffins.

This ethylene oligomerization process for producing even carbon number paraffins is highly dependent on crude oil and natural gas prices. Furthermore, n-paraffins have to be sold at a premium to the olefins to justify the added cost of hydrogenating. These factors make the price and availability of n-paraffins thus produced highly variable.

Another method of producing n-paraffins is Fischer-Tropsch synthesis. The liquid product of this reaction is a broad distribution of even and odd carbon number paraffins, from C₅to C₅₀+.

Naturally occurring fatty acids and esters may be hydrotreated to produce a hydrocarbon composition including even and odd carbon number paraffins as reported in prior art, namely: Wong, et. al. “Technical and Economic Aspects of Manufacturing Cetane-Enhanced Diesel Fuel from Canola Oil”; Bio-Oils Symposium, Saskatoon, Saskatchewan, Canada; March 1994. FIG. 2 of Wong et. al. includes typical gas chromatography/mass spectrometry (GC/MS) trace of hydrotreated canola oil wherein the relative heights of even and odd carbon number paraffins are similar, indicating presence of comparable concentrations of each. The prior art method for converting triglycerides and fatty acids to paraffins employs a fixed-bed catalytic reactor, packed with commercially available hydrotreating catalysts. These catalysts are cylindrical or three-fluted extrudates of alumina with nickel molybdenum or cobalt molybdenum sulfided metal activity. The typical equivalent diameter of these catalysts is from about 1.5 mm to about 2.0 mm.

The equivalent diameter is used to characterize non-spherical particles by size. Equivalent particle diameter of a non-spherical particle is defined as the diameter of a sphere having the same volume as the non-spherical particle. For a cylindrical catalyst of diameter D and length L, the equivalent particle diameter D_pis expressed as D_p=6(4/L+4/D)⁻¹. For a three-fluted extrudate, the equivalent particle diameter expression is D_p=6[2/L+5π/(D(sin(60°)+1.25π)]⁻¹.

The fatty acid/glyceride feed is hydrogenated and deoxygenated in the fixed bed reactor packed with commercial hydrotreating catalysts. As illustrated by

Equations

1 and 2 for the example of triolein (oleic acid triglyceride), the deoxygenation is achieved by oxygen hydrogenolysis, decarboxylation (removal of CO₂), and decarbonylation (loss of CO).

In both reactions, the glycerol backbone is converted to propane and double bonds are saturated. Since one carbon is removed from the fatty acids during decarboxylation and decarbonylation reactions (as illustrated in Equation 2), odd carbon number paraffins are formed from even carbon number naturally occurring fatty acids.
To this end, there is a need for even carbon number paraffin compositions and a selective process for producing even carbon number paraffins. In particular, the present invention is a process for converting biological feedstocks into even carbon number paraffin compositions.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a schematic diagram of an embodiment of an operation of a continuous process in accordance with the present invention.

FIG. 2 is a schematic diagram of an embodiment of an operation of a series-reactor process in accordance with the present invention.

FIG. 3 is a schematic diagram of an alternative embodiment of an operation of a series-reactor process in accordance with the present invention.

FIG. 4 is a schematic diagram of an embodiment of an operation of a batch process in accordance with the present invention.

FIG. 5 is a bar graph summarizing the results of Example 1.

FIG. 6 is a bar graph summarizing the results of Example 2.

FIG. 7 is a McCabe-Thiele diagram for C₁₆-C₁₈paraffin separation.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

The present invention relates to even carbon number paraffin compositions and a method for producing such even carbon number paraffin compositions from biological feedstocks. Paraffin compositions of the present invention have superior properties as phase PCM material.

It has been discovered that hydrocarbon compositions with very high concentrations of even carbon number paraffins can be obtained from biological feedstocks. The products are produced by a single-step hydrogenation/hydrogenolysis process of biological feedstocks. One embodiment of the process is carried out using a bimetallic catalyst of about 10 to about 500 micron equivalent particle diameter. The shorter diffusion path length, more accessible pores, and lower intra-catalyst temperature gradients in the smaller catalyst system of the present invention reduce thermal decarboxylation and consequent co-production of odd number paraffins.

One embodiment of the process of the present invention is preferably carried out with the catalyst in the slurry phase. Commercially available catalyst extrudates may be ground and sieved to reduce the catalyst size to the preferred range of the present invention, from about 10 microns to about 400 microns, most preferably from about 30 microns to about 80 microns. Examples of the catalyst include but are not limited to nickel-molybdenum (NiMo), cobalt-molybdenum (CoMo), or nickel-tungsten (NiW) on alumina or alumina phosphate supports. Pre-ground catalyst extrudates are commercially available in both oxide and active sulfide forms. The metal oxide catalysts are activated by sulfiding.

Commercial bimetallic catalysts are also available as slurry grades and well-suited for the invention disclosed herein. Preferred examples include sponge metal catalysts such as Mo promoted Raney® Ni and Co (Raney® is the trade name of the Grace Davison sponge metal catalyst). Sponge metal catalysts are formed by leaching nickel-aluminum or cobalt-aluminum alloys with concentrated caustic (sodium hydroxide) solution to form hydrogen active metal of high surface area. These slurry catalysts are active as received, but may be sulfided to achieve the desired selectivity.

Supported slurry catalysts suitable for the process of this invention may be prepared by impregnating spray-dried alumina or modified alumina supports with solutions containing nickel, cobalt, molybdenum and/or tungsten compounds before calcining.

It should be understood by one of ordinary skill in the art that any such catalyst may be utilized in the present invention so long as the catalyst operates as described herein.

Referring now to the drawings and more particular toFIG. 1, shown therein is one embodiment of an operation of a process utilizing a continuous flow reactor constructed in accordance with the present invention. Abiological feedstock101 is pressurized to reactor pressure of about 200 psig to about 2,000 psig viapump102. Preferred operating pressures for the slurry bubble column reactor are from about 400 to about 1,000 psig. Thefeed101 comprises of vegetable oils, animal fats/greases, plant oils, tall oil fatty acid, and algal oils. Algal oils can be naturally occurring or produced in bioreactors. Pressurizedliquid stream103 enters areactor104.

Theslurry reactor104 is preferably a bubble column. The reactor catalyst loading is between about 1% and about 30% (dry bulk catalyst volume per total slurry volume), preferably between about 2% and about 20%. The catalyst particle size is from about 10 to about 400 microns, preferably from about 30 to about 80 microns. The throughput of the pressurizedbiological feed stock103, is between about 0.1 and about 10 LHSV (volume feed per volume catalyst per hour), preferably between about 0.5 and about 5 LHSV. These parameters set theslurry reactor104 volume for the design feed rate.

The pressurizedliquid stream103 reacts therein withhydrogen105 which is optionally preheated throughheater116. The hydrogen-rich gas105 preferably has a hydrogen concentration between 70 and 100 mol %, preferably between 80 and 99 mol %. The hydrogen-rich gas105 is supplied at a rate of about 3,000 to about 10,000 SCF/bbl (volume gas per volume biological feedstock). The gas to feedstock ratio is preferably from about 4,000 SCF/bbl to about 8,000 SCF/bbl. The diameter of bubblecolumn reactor vessel104 is selected such that the gas flow rate is in the churn-turbulent regime from about 7 cm/s to about 40 cm/s, preferably from about 8 cm/s to about 12 cm/s. A heated hydrogen-rich gas105A is dispersed through asparger119. The sparger may be of various configurations including but not limited to a ring-type sparger with multiple orifices, a sintered metal plate or sintered metal distributing pipe(s) or co-fed with the biological feedstock via a simple pipe distributor. In some embodiments the catalyst is dispersed in the slurry phase by mechanical agitation. The gas flow through thereactor104 produces auniform catalyst slurry106. Alternatively, a side arm/downcomer (not shown) can also be deployed to recirculate de-gassed slurry to thereactor104 which also aides catalyst distribution in thereactor104. The biological feedstock converts into mainly even carbon number paraffins as it is diluted within the catalyst-paraffin slurry106.

The heat of reaction is in part removed by evaporation of aboiler feed water117 in cooling tubes/coils120, producingsteam118. At the hydrodynamic regimes described herein, high heat removal may be achieved with coolingcoil device120 immersed in thereactor104. Typical heat transfer coefficient for a steam-generating cooling coil is in the 40 to 200

Btu/hr-ft²-° F. range. The reactor temperature is thus controlled between about 450° F. (232° C.) to about 750° F. (399° C.), preferably between about 600° F. (315° C.) and about 650° F. (343° C.). At these preferred temperatures, high pressure steam (greater than about 400 psig, and preferably greater than about 600 psig) may be produced and used for driving motors, generating electricity, and/or supplying process heat.

The extent of back-mixing within the bubble column depends to a large extent on the height-to-diameter ratio of the reactor. Typical columns have successfully been modeled as 1.1-1.9 ideal CSTR's in series. At the preferred reactor design conditions, the reactor liquid composition is mainly the paraffin, and the temperature very close to uniform.

Thevapor product107 frombubble column reactor104 is cooled in air cooler108 wherein byproduct water and light hydrocarbons condense. At operating pressures below 500 psig and temperatures above about 315° C. (600° F.), more than about 50% of the C₁₈— paraffin reaction product will vaporize and is condensed overhead with water and light hydrocarbons.

A threephase composition109 is separated inseparator drum110. Thewater stream111B andhydrocarbon111A are thus separated from recycle hydrogen-rich gas111C. In some embodiments, the hydrogen-rich gas111C may be purified to remove some or all of the minor reaction byproducts such as ammonia, hydrogen sulfide, and carbon oxides. Recycle hydrogen-rich gas may then be combined with makeup hydrogen to form the reactor hydrogen-rich gas105.

Theslurry106 is transported throughconduit112 to filter113 to separate the catalyst from the reactor product. In some embodiments filter113 is a cross-flow filter. In other embodiments, a hydrocyclone followed by a filter is used. It should be understood by one of ordinary skill in the art that any device capable of separating suspended solids from liquid may be used in the present invention. The catalystslurry concentrate stream114 returns toreactor104, while the filteredparaffin product115 exits the reactor system. Product streams115 and111B include equal to or greater than about 75 wt % even carbon number paraffins in the C₁₂-C₂₄range. Preferably, the product streams comprise of equal to or greater than about 80 wt % even carbon number paraffins. In some embodiments, the product stream may undergo further processing such as distillation to recover the even carbon number paraffin products.

In other embodiments of the present invention, a plurality of reactors are employed to divide the hydrogenation/hydrogenolysis load over two or more reactors. Those skilled in the art will recognize that the reactors-in-series configuration is used in back-mixed reactor systems to achieve higher conversion at same or lower total reactor volume.

Referring now toFIG. 2,biological feedstock201 is pressurized to the reactor system pressure inpump202. The reactor system pressures are in the same range previously specified herein. The reactor system further contains catalyst of type and size specified in the detailed description of the invention. Thepressurized feed203 is optionally heated inheater240. Thepreheated feed203A enters thefirst stage reactor204 wherein partial conversion occurs in the catalyst slurry phase. Hydrogen-rich gas205 is introduced into slurrybubble column reactor204 through a sparger device (not shown) at the rates previously specified herein.Reactor204 is equipped with coolingcoils210 to maintain the reactor at the desired temperature range previously specified. The extent of feed conversion inreactor204 is about 10% to about 90%, preferably about 30% to about 60%.Stream206, the partially converted product including paraffin, biological feedstock, and reaction intermediates such as fatty alcohols, fatty acids, and olefins, is filtered throughfilter207 to separate the catalyst. The catalystrich slurry209 is returned to thereactor204 while the filtered, partially convertedproduct208 flows tosecond stage reactor211.

Typically, areactor211 operates under the same temperature and gas-to-oil ratio as thereactor204. In some embodiments thereactor211 operates at a higher temperature than thereactor204. In some embodiments, the pressure in

reactors

211 and239 are lower than thereactor204 to facilitate filtrate flow from thereactor204 to thereactor211, and from thereactor211 to thereactor239. After undergoing reaction with hydrogen provided bygas stream212, a partially convertedslurry213 undergoes solid-liquid separation in afilter214. A catalystrich slurry216 is returned to thereactor211 while the partially convertedstream215 is transferred to thereactor239. The total extent of feed conversion in thereactor211 is about 30% to about 95%, preferably between about 50% and about 80%.

Hydrogen is supplied to thereactor239 from thegas stream217. The total feed conversion achieved in this slurry bubble column reactor is between about 80% and about 100%, preferably at or very near about 100% feed conversion. The temperature, pressure, and gas-to-oil ratio are in the same range described previously. However in some embodiments, thereactor239 is operated at a higher temperature than the

reactors

204 and211. A paraffin-catalyst slurry stream218 is filtered in afilter219 to supply aproduct stream221 and returning high-solids slurry stream220 to thereactor239. Theproduct221 includes equal to or greater than about 75 wt % even carbon number paraffins in the C₁₂-C₂₄range. Preferably, theproduct stream221 comprises of equal to or greater than about 80 wt % even carbon number paraffins in the C₁₂-C₂₄range.

The off gas from the three slurry bubble column reactors in series, streams222,223 and224, are combined to form avapor stream225. Thevapor stream225 is cooled in acondenser226 to a temperature from about 60° F. (15.5° C.) to about 160° F. (71° C.), preferably from about 80° F. (27° C.) to about 140° F. (60° C.). A threephase stream227 entersdrum228 where thestream227 is separated into awater phase229, alight hydrocarbon phase230 and agas phase231. Thegas phase231 is rich in hydrogen. The other components of thegas phase231 include propane, other light hydrocarbons, and minor byproducts described previously. The hydrogen-rich gas stream may be partially purged (stream232) with the rest recycled asstream233. The aforementioned impurities may be removed in ahydrogen purification unit234. Thehydrogen purification unit234 is typically a scrubber used to remove ammonia and hydrogen sulfide. A purified hydrogen-rich stream235 is then combined withmakeup hydrogen238 inrecycle compressor236. A recompressed hydrogen-rich gas237 is used to supply each of the slurry bubble column reactors.

In an alternative embodiment of an operation of a reactors-in-series process of the present invention, a slurry bubble column reactor containing catalyst of the type and size previously described herein may be followed by a fixed-bed reactor. Referring toFIG. 3, thebiological feedstock251 is pressurized bypump252 to the reactor system pressure previously specified herein. The pressurized biological feedstock is heated by the reactor feed-effluent exchanger254. Aheated stream255 enters a slurrybubble column reactor257 where a catalyst of the type and size-range previously described herein is suspended in the slurry phase by sparging of hydrogen-rich gas258.Reactor257 is equipped with coolingcoils256 to control the temperature at target value within the range previously specified herein. A partially convertedeffluent slurry259 is processed throughfilter260. A catalystrich slurry262 is returned to thereactor257 while a filtered partially convertedproduct261 is transferred to a fixed-bed reactor264 for achieving full conversion. Before entering thereactor264, the liquid feed is mixed with optionallypreheated hydrogen286. A combinedfeed263 trickles through the fixed-bed reactor264 wherein the partially converted feedstock and reaction intermediates are fully converted to a predominately even carbon number paraffin composition. The fixed-bed reactor264 is operated adiabatically and the temperature is allowed to rise within the preferred range previously specified herein. Areactor effluent265 is partially cooled inexchanger254. A partially cooledproduct266 entershigh pressure separator267 wherein the hydrogen-rich vapor stream270 is separated from a mainly even carbon number paraffinicliquid product268. Theliquid product268 may be further processed through distillation to recover the desired even carbon number paraffin composition previously specified herein.

The hydrogen-

rich gas streams

270 and269, from thehigh pressure separator267 and the slurrybubble column reactor257 respectively, are combined to formvapor stream271.Water271A is added tovapor stream271 to wash any deposits that may form upon condensation in acondenser272. A cooledstream273 is a three phase composition which is separated indrum274. The liquid fractions includebyproduct water275 andlight hydrocarbons276. A hydrogen-rich gas277 is partially purged asstream278. The rest of the gas,stream279 is optionally treated in purification unit290 to remove ammonia, hydrogen sulfide, and other byproducts of the hydrogenation/hydrogenolysis reaction. A purified hydrogen-rich gas280 is combined withmakeup hydrogen282 inrecycle compressor281. A recompressed hydrogen-rich gas283 is optionally heated inheater284 before supplying theslurry bubble column257 and the fixed-bed reactor264.

The slurry catalyst reaction may also be conducted in batch mode. This may be a preferable embodiment when large volume production is not sought, or when the paraffin products from different feed stocks need to be segregated.

Referring toFIG. 4, abiological feedstock301 is charged to a batch stirredreactor302. Thereactor302 is equipped with anagitator assembly303 for suspending solids and dispersing gas, and ajacket304 for heat transfer. Aslurry catalyst306 is then added to thereactor302. The catalyst is of the type and size-range previously described herein. The reactor is then purged and pressurized withhydrogen307 to the target operating pressure. Pressure ranges described previously for the continuous flow reactor embodiments are applicable to the batch reactor embodiment as well. These preferred pressures are from about 400 psig to about 1,000 psig.

Thereactor302 is then heated to a target operating temperature in the range previously described for the continuous reactor embodiments, preferably between 450° F. (232° C.) and 650° F. (343° C.). The operating temperatures may be achieved by circulation of aheat transfer fluid308 through thereactor jacket304. Once at target temperature, theheat transfer fluid308 is used for cooling. Thehydrogen307 supply rate is used to limit the release of reaction heat through atemperature control loop309. In some embodiments, the hydrogen flow rate is maintained constant and the reactor pressure is controlled through a backpressure control loop310, while temperature is controlled through circulation rate of the heat transfer fluid. In some embodiments,reactor302 is equipped with a cooling coil (not shown) to increase heat removal and shorten batch cycle.

The batch reactor is equipped with piping312,312A, andcondenser318. Condensable byproducts of the hydrogenation/hydrogenolysis reaction which occurred inreactor302, light hydrocarbons and water, are thus collected indrum314 after cool-down withcoolant316 incondenser318. Upon completion of the reaction, when no more H₂consumption is observed, thereactor302 is cooled to about 140° F. (60° C.) to about 160° F. (71° C.) and the products and byproducts are drained out through conduits320 (water, followed by light hydrocarbons) and322 (main paraffin product). Most of the catalyst settles to the bottom ofreactor302 after agitation has been turned off, for reuse in the next batch. The suspended catalyst fines are removed from the n-paraffin product throughfilter324. Sintered metal or cartridge elements may be used forcatalyst filter324. A filteredproduct326 has the same even carbon number paraffin composition previously described in the continuous flow reactor embodiments of the present invention.

In order to further illustrate the present invention, the following examples are given. However, it is to be understood that the examples are for illustrative purposes and are not to be construed as limiting the scope of the subject invention.

EXAMPLESExample 1Hydrogenation/Hydrogenolysis of Canola Oil with 1/16″ Trilobe Catalyst Extrudates (D_p˜1.2 mm) in a Fixed-Bed Reactor

The present example demonstrates the conversion of a biological feedstock, canola oils, into paraffinic compositions using standard-size catalyst extrudates. A 100 cc isothermal tubular reactor was filled with 80 cc of a commercially available NiMo catalyst (purchased from Catalyst Trading Corporation, Houston, Tex.) of 1.2 mm equivalent particle diameter, and 70-100 mesh glass beads. The catalyst was sulfided in the presence of hydrogen with dimethyl disulfide at two hold temperatures: 6 hours at 400° F. and 12 hrs at 650° F. Hydrogen sulfide break-through was confirmed before the temperature was raised from 400° F. (204° C.) to 650° F. (343° C.) at 50° F./hr. After sulfiding, the reactor was cooled to 400° F. (204° C.).

Next a fatty triglyceride feed was introduced to the isothermal reactor. The reactor was slowly heated to 650° F. to achieve full conversion of the triglyceride feed to a paraffin composition. The reactor temperature was further increased to 700° F. (371° C.) to maintain good catalyst activity at 80 cc/hr feed rate (1.0 hr⁻¹LHSV). Canola oil feedstock was then introduced at these reactor conditions.

The product was analyzed using a gas chromatography (GC) method involving calibration with n-paraffin standards. The results of feed conversion to paraffins are summarized inFIG. 5. As observed therein, a significant percent of C₁₇paraffins was produced from decarbonylation/decarboxylation of C₁₈fatty acids. The overall concentration of even carbon number paraffins was only 61 wt %.

Example 2Hydrogenation/Hydrogenolysis of Canola Oil with Crushed and Sieved Catalyst (D_p=30-80 micron) in Slurry Reactor

The catalyst used in Example 1 was discharged from the reactor, crushed, and sieved into a 30-80 micron particle-size cut. Ten (10) grams of the 30-80 micron cut of the ground catalyst was combined with 300 g of canola oil in a 1 liter Autoclave stirred-reactor. The agitation was set at 1000 rpm. The reactor was purged with N₂before starting H₂flow at 3 L/min. The reactor was controlled at 500 psig pressure. The temperature was ramped at 1° F./min to hold temperatures of 450° F. (232° C.), 500° F. (260° C.), 550° F. (288° C.), and 600° F. (316° C.). Liquid samples were obtained at each hold temperature and analyzed by GC. The hold times were 20 hrs at 450° F. (232° C.), 5 hrs at 500° F. (260° C.), 23 hrs at 550° F. (288° C.), and 19 hrs at 600° F. (316° C.).

The results of the slurry catalyst conversion reaction are summarized inFIG. 6. It is thus observed that most of the C₁₈and C₁₆fatty acids in the canola oil were converted to C₁₈and C₁₆paraffins, suggesting a high selectivity for the oxygen hydrogenolysis mechanism and low decarboxylation/decarbonylation. The overall concentration of even carbon number paraffins was 80 wt %.

Example 3Even Carbon Number Paraffin Composition from Rapeseed Oil

Rapeseed oil was the third largest source of vegetable oil in the world (USDA year 2000 statistics), behind palm and soybean oils. The oil yield from rapeseed is 40-50%, compared to only 20 percent for soybeans. Table 2 summarizes the fatty acid profile of representative biological feedstocks.

TABLE 2

Fatty Acid Composition of Several Common Biological Feedstocks^(1-5)

Saturated Acids

Mono-Unsaturated Acids

Eicosenic/

Poly-Unsaturated Acids

Animal fats
Chicken Fat	—	—	—	—	7	2	—	—	69	—	17	—
Beef Tallow	—	—	0.2	2-3	24-30	21-26	0.4-1	—	39-43	0.3	2-3	1
Yellow Grease	—	3	3	1-11	23-27	10-12	—	1	29-50	—	2-15	1
Choice White	—	7	3	9	25	12	—	—	27	—	1-3	1
Grease
Lard (pork fat)	—	—	—	1-2	25-30	12-16	—	2-5	41-51	2-3	4-22	0.2
Vegetable Oils
Soybean Oil	—	—	—	0.3	7-11	3-6	5-10	0-1	22-34	—	50-60	2-10
Corn Oil	—	—	—	0-2	8-11	1-4	—	1-2	28-50	0-2	34-58	1
Cottonseed Oil	—	—	—	0-3	17-23	1-3	—	—	23-41	2-3	34-55	1
Canola Oil	—	—	—	—	4	2	—	—	62	—	22	10
Coconut Oil	5-9	4-10	44-51	13-18	7-10	1-4	—	—	5-8	—	1-3	—
Sunflower Oil	—	—	—	—	6-7	4-5	1.4	—	19		68-69	0.3-1
Palm Oil	—	—	—	1-6	32-47	1-6	—	—	40-52	—	2-11	—
Palm Kernel	2-4	3-7	45-52	14-19	6-9	1-3	1-2	0-1	10-18	—	1-2	—
Oil
Rapeseed	—	—	—	—	2-5	1-2	0.9	0.2	10-15	50-60	10-20	5-10
(High Eurcic)

(1) http://www.scientificpsychic.com/fitness/fattyacids.html
(2) Kinast, J. A. March 2003, “Production of Biodiesel from Multiple Feedstocks and Properties of Biodiesel/Diesel Blends, NREL/AR-510-31460
(3) Tyson, K. S., NREL Presentation “Biodiesel for New England” Mar. 26, 2003
(4) Food Fats and Oils, Institute of Shortening and Edible Oils, Ninth Edition 2006
(5) a“—” in a cell means that this constituent is not present

As observed therein, rapeseed oil consists of 50-60 wt % C₂₂fatty acids with the balance mainly C₁₈fatty acids. According to the inventive conversion process disclosed herein, rapeseed oil will produce an even carbon number composition comprising of a ratio of about 1:1 to 1.5:1 C₂₂:C₁₈n-paraffins. This composition is useful as a PCM in construction or textile/clothing application for high temperatures, including desert climates when day times can surpass 44° C. (melt point of C₂₂paraffin), and night times below 28° C. (freeze point of C₁₈paraffin). The high temperature phase transition makes this PCM composition well suited for computer cooling applications (i.e. heat sink or cooling pad under the computer) as well.

Example 4Even Carbon Number Paraffin Compositions from Palm Oil and Palm Kernel Oil

Palm oil recently surpassed soybean oil as the largest volume plant oil produced in the world. Whereas palm oil itself is derived from the fruit of the palm tree, the palm kernel oil is extracted from the fruit's seeds. Referring to Table 2, palm oil consists of about 40 wt % C₁₆fatty acids, with the balance mainly C₁₈fatty acids. According to the method of the present invention, the palm oil is converted to a mainly even carbon number paraffin composition in the C₁₆-C₁₈range with C_1-18:C₁₆weight ratio of about 1.5:1. The composition is useful as a PCM for construction and textile/clothing applications in the 18° C. to 28° C. range.

Referring to Table 2, palm kernel oil has a fatty acid composition of about 45-52 wt % C₁₂, 14-19 wt % C₁₄, 6-9 wt % C₁₆, and 11-17 wt % C₁₈. According to the present invention, the biological feedstock is converted to a mainly even carbon number n-paraffin composition including C₁₂, C₁₄, C₁₆, and C₁₈components. The n-paraffin composition may be distilled to yield a C₁₂/C₁₄composition suitable for very low temperature PCM applications (such as for bridge warmers and dive suites) or as chemical intermediates (such as for producing linear alkyl benzenes).

Example 5Separation of Even Carbon Number Paraffins Derived from the Method of the Present Invention

The method of the present invention may be used to convert most animal fats into a composition with approximately 30 mol % C₁₆n-paraffins and the balance mainly C₁₈paraffin. Vacuum distillation is a well understood and broadly practiced separation technology. At 20 torr pressure, the vapor-liquid equilibrium (VLE) constants (“K-values”) for n-octadecane and n-hexadecane are 1.34 and 0.82 respectively (computed using HYSYS simulation software's Peng-Robinson thermodynamic model). These K-values may be used to generate the equilibrium curve ofFIG. 7. Distillation column operating lines have been added according to the McCabe-Thiele methodology as disclosed in prior art, namely, Foust et. al.Principles of Unit Operations,2^ndEd.; John Wiley & Sons: New York, 1980; Chapter 7. According to McCabe-Thiele procedure for distillation column design, with a reflux ratio of 6.5, or 30% higher than minimum reflux, a separation yielding 90 mol % purity C₁₈and C₁₆n-paraffin products requires 14.5 theoretical stages. Assuming 73% tray efficiency, the vacuum tower requires 20 actual trays.

While the C₁₈product of the separation can be sold as a PCM for narrow temperature control applications, the C₁₆n-paraffin (n-hexadecane or cetane) has other markets. One large volume application is diesel fuel additive. Another use of linear C₁₆hydrocarbons is as intermediates for specialty chemicals including alkenyl succinates for paper coatings.

The analysis of this example shows that the even carbon number compositions of the present invention, such as those derived from animal fats/greases, are well suited for producing chemicals using conventional separation techniques.

While the compositions and methods of this invention have been described in terms of preferred embodiments, it will be apparent to those of skill in the art that variations may be applied to the process described herein without departing from the concept and scope of the invention. All such similar substitutes and modifications apparent to those skilled in the art are deemed to be within the scope and concept of the invention as it is set out in the following claims.