Classifications

• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
  • C10G3/42—Catalytic treatment
  • C10G3/44—Catalytic treatment characterised by the catalyst used
  • C10G3/47—Catalytic treatment characterised by the catalyst used containing platinum group metals or compounds thereof
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
  • C10G3/42—Catalytic treatment
  • C10G3/44—Catalytic treatment characterised by the catalyst used
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
  • C10G3/42—Catalytic treatment
  • C10G3/44—Catalytic treatment characterised by the catalyst used
  • C10G3/45—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
  • C10G3/42—Catalytic treatment
  • C10G3/44—Catalytic treatment characterised by the catalyst used
  • C10G3/45—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof
  • C10G3/46—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof in combination with chromium, molybdenum, tungsten metals or compounds thereof
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
  • C10G3/42—Catalytic treatment
  • C10G3/44—Catalytic treatment characterised by the catalyst used
  • C10G3/48—Catalytic treatment characterised by the catalyst used further characterised by the catalyst support
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
  • C10G3/42—Catalytic treatment
  • C10G3/44—Catalytic treatment characterised by the catalyst used
  • C10G3/48—Catalytic treatment characterised by the catalyst used further characterised by the catalyst support
  • C10G3/49—Catalytic treatment characterised by the catalyst used further characterised by the catalyst support containing crystalline aluminosilicates, e.g. molecular sieves
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
  • C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
  • C10L1/00—Liquid carbonaceous fuels
  • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
  • C10L1/00—Liquid carbonaceous fuels
  • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
  • C10L1/06—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for spark ignition
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
  • C10G2300/10—Feedstock materials
  • C10G2300/1011—Biomass
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
  • C10G2300/20—Characteristics of the feedstock or the products
  • C10G2300/30—Physical properties of feedstocks or products
  • C10G2300/301—Boiling range
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
  • C10G2400/02—Gasoline
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
  • C10G2400/08—Jet fuel
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P30/00—Technologies relating to oil refining and petrochemical industry
  • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Definitions

• the invention relates to the conversion of carboxylic acids obtained from biomass and other natural or industrial sources into paraffinic and olefinic hydrocarbons suitable for use as other hydrocarbon products, including but not limited to fuels, solvents, and other derivatives and products.
• Hydrocarbons are an energy source for internal combustion engines, for turbines in jet aircraft, and for other kinds of engines, as well as for other applications that require a source of fuel.
• Some hydrocarbon fuels such as diesel fuels, are linear, paraffmic hydrocarbons.
• Some hydrocarbon products such as, for example, kerosene, some jet fuels, and some solvents, have branched-chain hydrocarbons and number 10-to-15 carbon atoms in their molecular structure. By comparison, diesel fuels are typically straight-chained and have between 15-to-22 carbon atoms.
• Hydrocarbon fuels and other petrochemical products typically are obtained from crude petroleum oil through a series of conventional steps. These steps include, but are not necessarily limited to, distillation followed by additional refining. Attempts are being made, however, to produce hydrocarbon fuels, solvents, and other hydrocarbon products from alternative, renewable sources, including but not limited to feedstocks of biological origin. A common objective of such attempts has been to develop hydrocarbon fuels with similar chemical and functional properties to the fuels and other products that are obtained from crude petroleum, but made from alternative sources and without having to utilize the conventional steps such as those mentioned above.
• hydrocarbon fuels from alternative, renewable sources are compatible with and, therefore, acceptable for use with, the kinds of engines for which petroleum-derived hydrocarbon fuels are intended. The same is true in regards to other hydrocarbon products as noted above.
• hydrocarbon fuels and other hydrocarbon products from alternative, renewable sources other than petroleum include those products which are obtained from a process according to multiple embodiments and alternatives as described and claimed herein.
• such products are capable of being stored and transported through existing infrastructure (e.g., storage tanks and pipelines) as with petroleum-derived hydrocarbon fuels. This increases the feasibility of using such products as replacements for petroleum-derived hydrocarbon products in applications such as transportation fuels, as well as other applications.
• carboxylic acids are obtained from biomass raw materials, and are used as starting materials in the conversion to linear, paraffinic hydrocarbons.
• stearic acid with a chemical formula of C 17 H 35 COOH (or, C 18 H 36 O 2 )
• C 17 H 35 COOH or, C 18 H 36 O 2
• hydrodeoxygenation accomplishes this but requires the use of hydrogen as a reactant.
• An alternative approach is decarboxylation, which involves removal of the carboxylate group as carbon dioxide. In this approach, the alkane product has one carbon atom less than the carboxylic acid starting material.
• a decarboxylation reaction does not require the consumption of hydrogen as a reactant.
• decarboxylation produces hydrocarbons with a linear structure in which the alkyl group of the carboxylic acid is preserved, and the carboxylate group (i.e., one carbon atom and two oxygen atoms) is removed as carbon dioxide.
• carboxylate group i.e., one carbon atom and two oxygen atoms
• Decarboxylation of carboxylic acids is generally less expensive than hydrodeoxygenation, which requires a large supply of hydrogen as a necessary reactant.
• Decarboxylation yields normal, linear, hydrocarbons, without having to use hydrogen as a reactant. These hydrocarbons then may be isolated and separated by fractional distillation or other methods known to persons of ordinary skill in the art into appropriate fractions for use as kerosene, jet fuel, diesel fuel, automobile fuel or other kinds of fuel, solvents, and/or other kinds of hydrocarbon products as desired by an end user.
• a process for producing linear, paraffinic hydrocarbons converts fatty acids (a.k.a. carboxylic acids) containing 6-to-24 carbon atoms into linear, paraffinic hydrocarbons, which can be used as fuels and other hydrocarbon products.
• the linear, paraffinic hydrocarbons contain one less carbon atom than the starting carboxylic acids.
• decarboxylation of stearic acid (18 carbons) produces heptadecane (17 carbons, C17H36).
• a process for producing linear, olefinic hydrocarbons converts fatty acids containing 6-to-24 carbon atoms into linear, olefinic hydrocarbons.
• the linear, olefinic hydrocarbons contain one less carbon atom than the starting carboxylic acids.
• surface basicity of the catalyst and its dispersibility over the support are factors for selecting a reaction catalyst.
• Porosity and/or mesoporosity, as well hydrophobicity, are factors for selecting a support.
• Processes disclosed and claimed herein are for producing linear hydrocarbons which can be used in various ways. In some applications, these products are used as hydrocarbon fuels. Alternatively, these products are starting materials, which are converted to branched-chain paraffinic hydrocarbons through processes known to persons of ordinary skill in the art, and which are suitable for use as hydrocarbon fuels. Alternatively, these products are starting materials for the production of various petrochemicals, through methods which are known to persons of ordinary skill in the art. Non-limiting examples of such petrochemicals include linear alpha olefins, alpha olefin sulfonates, and linear alkyl benzenes. Such petrochemicals are used in the manufacture of various end products.
• linear alkyl benzenes are used in the manufacture of detergents.
• petrochemicals used in the manufacture of various end products include high viscosity index star polymers. The forgoing are non-limiting examples of a broad scope in which products of the subject process are used.
• a process for producing linear hydrocarbons comprises (1) obtaining a supply of at least one carboxylic acid; (2) selecting a reaction catalyst and a support as described herein; and (3) contacting the at least one carboxylic acid with the catalyst over the support, under conditions as described herein, resulting in the decarboxylation reaction:
• linear, paraffinic hydrocarbons are then isolated from the end products of the reaction.
• the linear, paraffinic hydrocarbons obtained as the end products of the decarboxylation reaction are fully saturated hydrocarbons, which are appropriate to be used in the various applications described above.
• the at least one carboxylic acid is a carboxylic acid having 6-to-24 carbon atoms.
• the at least one carboxylic acid is a mixture of at least two carboxylic acids, each having 6-to-24 carbon atoms.
• triglyceride esters contained in various sources as described below are converted to carboxylic acids through methods known to persons of ordinary skill in the art.
• the at least one carboxylic acid is obtained from a renewable feedstock of biological origin (i.e., biomass raw materials), such as, for example, plant oils; animal fats and oils; algae oils; waste vegetable oils; or oils from heterotrophic microbes.
• heterotrophic microbes are heterotrophic algae, oleaginous yeasts, and various bacteria.
• the source of the at least one carboxylic acid consists of a mixture of two or more members of this group.
• the at least one carboxylic acid is obtained from an industrial or other non-biological source, such as, for example industrial greases, and waxes obtained from solid wastes, and paper mills.
• the renewable feedstock includes, but is not necessarily limited to, plant oils from a non-food oil crop such as jatropha oil, camelina oil, pennycress oil, pongamia oil, and carinata oil.
• a non-food oil crop such as jatropha oil, camelina oil, pennycress oil, pongamia oil, and carinata oil.
• Such non-food oil crops are generally less expensive to produce or obtain, are more sustainable, and are significantly lower in lifecycle greenhouse gas emissions than, for example, soybean oil, rapeseed oil, or beef tallow.
• the use of such lower-cost, more sustainable oils for decarboxylation processes as described herein, according to multiple embodiments and alternatives provides increased production flexibility and cost-effectiveness for hydrocarbon fuels, chemicals, and other products because production facilities can be distributed and in closer proximity to locations where these oil crops are grown.
• known hydrodeoxygenation techniques and processes generally require significantly greater economies of scale, and are largely limited to being carried out at or near existing oil refineries with large supplies of hydrogen.
• starting materials used in a process for producing linear, paraffinic hydrocarbons are saturated carboxylic acids.
• the starting materials are unsaturated carboxylic acids.
• a catalyst is chosen from the group platinum, palladium, nickel, nickel- molybdenum, nickel-tungsten, and platinum-copper.
• surface basicity is considered in selecting a catalyst. It will be noted that the presence or absence of various functional groups at the surface of a catalyst influences its surface basicity.
• a support's basicity or acidity influences the kinds of hydrocarbon products resulting from decarboxylation of the carboxylic acids.
• the presence of acidic sites in the support tend to catalyze certain side reactions, such as cracking, isomerization, polymerization, and cyclisation of the primary decarboxylation product, i.e., the linear hydrocarbon.
• Some products of such side reactions tend to diminish the long-term life and activity of the catalyst.
• a solid material with known, basicity properties is chosen as a support.
• the surface basicity of the catalyst is determined by measuring the amount of acetic acid adsorbed from a 0.1 N solution of acetic acid in normal hexane, at room temperature, on a sample of the solid catalyst treated previously at high temperatures to remove impurities (e.g., water, carbon dioxide), and is expressed as equivalents of acetic acid adsorbed by the solid.
• impurities e.g., water, carbon dioxide
• the extent to which the metal catalyst is dispersed over the support influences the yield of the decarboxylation reaction. Stated differently, the hydrocarbon product yield increases as the level of metal dispersion increases.
• the dispersion of the metal catalyst over the support is at least about 50%.
• a support which is a porous or mesoporous structure formed from basic oxide materials, which are chosen from the group hydrotalcite, magnesium oxide, calcium oxide, a mixed oxide of ceria-zirconia, and lanthanum oxide.
• hydrophobicity is considered in selecting a support for the catalyst. Hydrophobicity of the support is determined by measuring adsorption of water vapor by the support under ambient conditions. Preferably, the support adsorbs no more than about 0.5%wt water vapor under ambient conditions. Optionally, hydrophobicity is determined by exposing the support to water vapor at 25° C and corresponding equilibrium pressures, and measuring the percentage of water vapor adsorbed by the support in relation to the weight of the catalyst to be used.
• carboxylic acid starting materials are diluted in a suitable solvent before commencing the decarboxylation reaction.
• a suitable solvent would include hydrocarbons, such as, for example dodecane or hexadecane.
• hydrocarbons such as, for example dodecane or hexadecane.
• a mixture of two or more hydrocarbons is used as a solvent.
• decarboxylation is carried out in a suitable solvent.
• decarboxylation is carried out in a solvent-free reaction chamber.
• a process for production of paraffmic hydrocarbons is carried out in a reactor.
• the reactor is a batch reactor.
• the reactor is a semi-batch reactor.
• the reactor is a continuous flow reactor.
• the carboxylic acid starting materials are passed over a supported catalyst in a reaction zone contained within the reactor.
• decarboxylation is carried out at a temperature in a range of about 200° C - 400 ° C.
• the temperature is in a range of about 250° C - 350 ° C.
• decarboxylation is carried out at a pressure in a range of about 1 bar - 60 bar.
• decarboxylation produces hydrocarbon products consisting of linear, paraffinic hydrocarbons, which are isolated and separated using techniques known to persons of ordinary skill in the art (e.g., distillation).
• decarboxylation produces hydrocarbon products consisting of linear, olefinic hydrocarbons, which are isolated and separated using such techniques. In this way, the separated reaction products can be put to use according to their intended purpose as selected by a user.
• decarboxylation produces only linear, paraffinic hydrocarbons, and carbon dioxide.
• the lack of cracking, branching, or other side reactions in the decarboxylation reactor may be desirable for the production of certain products, such as, for example, high-cetane diesel blendstock or aromatic-free solvents.
• the lack of side reactions may also be desirable for increasing the conversion yield of the desired products.
• the lack of side reactions may help to reduce the complexity and cost of downstream separations.
• the combination of certain catalysts and certain supports may help to reduce unwanted side reactions, including cracking and branching. Further, certain combinations as well as reaction conditions may help to increase single-pass conversion yields.
• the cracked or branched hydrocarbons are expected to be less than about 5% by mass of the total reaction products.
• the degree of cracking can be indicated by the ratio of the weighted average carbon chain length of the hydrocarbon products to that of the carboxylic acid feedstock, after accounting for the difference of a single carbon resulting from the decarboxylation itself.
• a weighted average chain length of hydrocarbon products greater than 80% of the weighted average chain length of the carboxylic acid feedstock is expected to be a finding indicative of minimal cracking during the decarboxylation reaction.
• a process for producing linear hydrocarbons is used for the conversion of unsaturated carboxylic acids to olefinic (unsaturated), linear hydrocarbons.
• This alternative embodiments comprises (1) obtaining a supply of at least one carboxylic acid; (2) selecting a reaction catalyst and a support as described herein; and (3) contacting the at least one carboxylic acid with the catalyst over the support, under conditions as described herein, resulting in the decarboxylation reaction:
• R contains six-to-twenty-four carbons, and has at least one carbon-carbon double bond.
• both paraffinic and olefinic carboxylic acids are together converted to paraffinic and olefinic linear hydrocarbons in a single reaction chamber, using a catalyst, support, and reaction conditions according to alternative embodiments as set forth herein.
• the process converts at least a portion of olefinic carboxylic acids to linear, olefinic hydrocarbons by decarboxylation, which are then converted through hydrogenation, which optionally can be performed in the same reaction chamber or in a separate reaction chamber.
• reaction conditions and catalyst/support combinations can also be varied in order to favor particular levels of cracking and/or so that the paraffinic hydrocarbons that are produced will meet the specifications of, among other products, high cetane diesel and feedstocks for the downstream production of chlorinated paraffins, alpha olefins, and olefin sulfonates.
• the paraffinic hydrocarbon products of the decarboxylation reaction are subsequently passed over a hydroisomerization catalyst to favor particular levels of cracking and/or branching that meet the specifications of a variety of commercially desirable products, such as, for example various solvents, diesel fuel, aviation turbine fuel, gasoline, and aviation gas.
• a hydroisomerization catalyst to favor particular levels of cracking and/or branching that meet the specifications of a variety of commercially desirable products, such as, for example various solvents, diesel fuel, aviation turbine fuel, gasoline, and aviation gas.
• solvents may offer improved health and safety conditions during use in the workplace and elsewhere given the significantly lower levels of volatile organic compounds ("VOCs”) and of aromatics, while still meeting other key specifications for degreasing solvents and cleaning fluids, such as flash point and drying time.
• VOCs volatile organic compounds
• the paraffinic hydrocarbons produced from decarboxylation, or, alternatively, decarboxylation followed by isomerization have a flash point above about 140°F, have a VOC content at or below 25 g/L, and meet the specifications of MIL-PRF-32295, the military specification for environmentally friendly cleaning fluids, which is now being required in order to protect workers' health and safety.
• olefmic hydrocarbons such products can be used as base stock for lubricants.
• base stock for lubricants.
• mid-chain olefins with internal double bonds can be used as base stock for lubricants with desired levels of viscosity index, lubricity, and oxidative stability.
• the paraffinic hydrocarbon products of decarboxylation undergo subsequent hydroisomerization to form branched paraffinic hydrocarbons, which are useful as aviation turbine fuel and which meet the specifications of ASTM D7566, the standard for Jet-A aviation turbine fuel produced from renewable sources.
• ASTM D7566 the standard for Jet-A aviation turbine fuel produced from renewable sources.
• One of the key specifications of that standard is the boiling point range of 180°C-300°C, which can be achieved with the correct balance of cracking and isomerization.
• the process for the production of these hydrocarbons, as described herein according to multiple embodiments and alternatives, can be tuned as selectably desired by a user to achieve the same boiling point range and other specifications using different feedstock sources with different carbon chain length distributions, and varying degrees of cracking and branching.
• the paraffinic hydrocarbon products of decarboxylation and subsequent hydroisomerization are useful as a high-octane motor gasoline meeting the specifications of ASTM D4814-1 IB, including a boiling point range of about 35°C-200°C, and these products will also have an octane rating greater than about 90.
• the decarboxylation process described herein allows for higher-octane gasoline because it can be tuned to convert the (linear) carboxylic acid feedstocks preferentially into specific paraffinic hydrocarbons, with a minimum of side reactions.
• some branched paraffinic hydrocarbons have higher octane values than multicyclic paraffinic hydrocarbons with similar volatility.
• some C9 napthenes have an octane rating of approximately 35
• some types of C12 branched paraffins have an octane rating of approximately 85
• both molecules have boiling points within about 5°C - 10°C of one another.
• the paraffinic hydrocarbon products of decarboxylation and subsequent hydroisomerization are useful as aviation gasoline after the addition of monocyclic aromatics, such as benzene, toluene, and xylene, which can be used to increase the octane to 100 or more.
• monocyclic aromatics such as benzene, toluene, and xylene
• One advantage of this process for producing aviation gas is that the branched paraffinic hydrocarbons resulting from decarboxylation and subsequent hydroisomerization will be very similar species and may have a significantly higher starting octane, as described above - before the addition of any aromatics or tetraethyl lead - compared to paraffinic hydrocarbons obtained from petroleum.
• the aviation gasoline specifications of ASTM D7719 including the requirement of an octane rating of 100 and a boiling point range of 20°C-175°C, can be met without the use of tetraethyl lead, which is prohibited by ASTM D7719 (the standard for lead- free test aviation gas), with the use of less or no aromatics.
• ASTM D7719 the standard for lead- free test aviation gas
• D910 the standard for leaded aviation gas
• the paraffinic hydrocarbon products of decarboxylation are used as feedstocks for downstream processes to produce mid-chain or long-chain chlorinated paraffins.
• Mid-chain chlorinated paraffins have carbon chain lengths of between 14 and 18 carbons and long-chain chlorinated paraffins have carbon chain lengths greater than 20 carbons.
• the paraffinic hydrocarbon products of decarboxylation are capable of being distinguished from paraffinic hydrocarbons produced by petroleum refineries or by hydrodeoxygenation of triglycerides.
• the products of decarboxylation are expected to be very low in sulfur, are expected to significantly exceed the Ultra Low Sulfur Diesel (ULSD) specification of no more than 15 ppm sulfur, and actually are expected to have less than about 5 ppm sulfur.
• ULSD Ultra Low Sulfur Diesel
• the hydrocarbon products of decarboxylation followed by subsequent hydroisomerization are expected to have less than about 5 ppm sulfur.
• hydrocarbon products of decarboxylation and/or of subsequent hydroisomerization are also possible to distinguish_the hydrocarbon products of decarboxylation and/or of subsequent hydroisomerization, according to multiple embodiments and alternatives described herein, from those of hydrocarbon products produced using conventional techniques at a petroleum refinery based on the molar ratio of linear hydrocarbons to branched or cyclic hydrocarbons.
• this molar ratio is expected to be higher for products obtained by decarboxylation according to embodiments and alternatives described herein.
• this molar ratio is expected to be greater than about five, and in some embodiments greater than about ten, compared to a molar ratio of about less than five and possibly less than one for hydrocarbons from petroleum refining.
• these embodiments would lead to higher octane gasoline or aviation gas because of the higher ratio of linear or branched to cyclic hydrocarbons.
• the Carbon- 14 to Carbon- 12 ratio in contemporary carbon sources is about 10 "12
• the Carbon- 14 to Carbon- 12 ratio in petroleum is 100 times lower, at a value of about 10 "14 .
• renewable triglycerides which are in large supply and which are generally of the kind that can be subjected to either decarboxylation (according to present embodiments and alternatives) or hydrodeoxygenation, routinely have even-numbered carbon chain lengths in nature.
• Decarboxylation removes one carbon from each carboxylic acid, such that the products of decarboxylation will typically have odd-numbered carbon chain lengths.
• Hydrodeoxygenation does not remove carbon from the carboxylic acid, so the products of hydrodeoxygenation typically will have even-numbered carbon chain lengths, although allowing for some cracking, they may not be exclusively even-numbered.
• the hydrocarbon products of decarboxylation are expected to have a ratio of odd-numbered to even-numbered carbon chain lengths significantly above one to one (i.e., 1 : 1), and generally above about four to one (i.e., 4: 1), whereas the hydrocarbon products of hydrodeoxygenation are expected to have a ratio significantly below one.
• the ratio of odd- numbered to even-numbered chain lengths can be estimated by analyzing the hydrocarbon products of these processes using a Gas Chromatograph-Mass Spectrometer (GC-MS), which will show the proportion by mass of the hydrocarbons at different chain lengths. This mass proportion can then be converted to a molar proportion.
• GC-MS Gas Chromatograph-Mass Spectrometer
• the decarboxylation of stearic acid, C18H36O2 yields predominantly heptadecane, C17H36, a linear paraffinic hydrocarbon containing only 17 carbon atoms.
• hydrodeoxygenation of stearic acid yields predominantly octadecane, C18H38, containing the same number of carbon atoms (18) as the starting carboxylic acid (stearic acid), with the oxygen atoms being removed as water.
• the presence of heptadecane, having an odd number of carbon atoms is a factor indicative of decarboxylation of the stearic acid feedstock.
• the predominance of odd-numbered carbons over even-numbered carbons, at a ratio of about 4: 1 indicates that decarboxylation is the predominant reaction occurring.
• Examples 1, 3, 4, 5, 6, 7, 10, 11, 12 and 13, which are described below, are alternative embodiments of a process for producing linear, paraffinic hydrocarbons.
• Examples 2, 8, and 9 are offered as comparative examples.
• Example 14 illustrates one application for the products of the subject process, namely as starting materials for conversion of paraffinic hydrocarbons to aviation turbine fuel (i.e., jet fuel).
• the catalytic run was carried out continuously over 150 hours.
• the liquid products contained two layers: a hydrocarbon top layer and a bottom layer containing unconverted carboxylic acids, which were condensed and collected in a product receiver at the end of 50 and 150 hours.
• the identity of the hydrocarbon products was determined by gas chromatography using a Hewlett Packard 4890 gas chromatograph.
• the acid number of the products of the hydrocarbon layer were determined, and compared to the acid number of the carboxylic acid feedstock. Based upon that comparison, the conversion of the carboxylic acid feedstock to paraffinic hydrocarbons was determined, as further described below. Iodine number is an indicator of unsaturation and presence of carbon-carbon double bonds, which serves as indicator of process effects on saturation of carbon-carbon double bonds.
• a palladium metal catalyst supported on a basic hydrotalcite oxide support [00044] The surface area of the support was approximately 99.5 m 2 per gram; the pore volume of the support was approximately 0.3 ml per gram of catalyst. The support was dried overnight at 150° C. The average pore width of the catalyst was approximately 9.5 nm (nanometers); basicity of the catalyst, as determined by titration with 0.1 normal acetic acid, was approximately 0.15 mEq (milliequivalent) acetic acid per gram.
• An aqueous solution of palladium nitrate containing a sufficient amount of palladium metal for 5 wt% of palladium in the final catalyst was prepared.
• a suspension of the hydrotalcite support in the palladium nitrate solution was prepared.
• the palladium compound was reduced to the metallic state by addition of a sufficient amount of sodium borohydride.
• the catalyst was dried in a flow of nitrogen at 200° C for 5 hours.
• the reduced catalyst was loaded in a downflow, fixed bed reactor.
• a feedstock consisting of a mixture of oleic acid and normal hexadecane in equal weight proportions was passed over the catalyst with a HPLC pump at a temperature of 330° C, hydrogen pressure of 20 bar, a hydrogen to oleic acid ratio of 600 (V/V) and a weight hourly space velocity of oleic acid of 1.0.
• the gaseous product of the reaction was carbon dioxide.
• a palladium metal catalyst supported on a non-basic support material i.e., activated carbon
• the surface area of the support was approximately 778 m 2 per gram; the pore volume of the support was approximately 0.45 ml per gram of catalyst.
• the support was dried overnight at 150° C.
• the average pore width of the catalyst was approximately 3.3 nm; basicity of the catalyst, as determined by titration with 0.1 normal acetic acid, was approximately 0.02 mEq acetic acid per gram.
• An aqueous solution of palladium chloride containing a sufficient amount of palladium metal for 5 wt% of palladium in the final catalyst was prepared and deposited on the carbon by incipient deposition.
• the catalyst was dried in a flow of nitrogen at 200° C for 5 hours.
• the dried catalyst was loaded in a downflow, fixed bed reactor and reduced in flowing hydrogen at 250° C, 20 bar pressure for 6 hours.
• a feedstock consisting of a mixture of oleic acid and normal hexadecane in equal weight proportions was passed over the catalyst with a HPLC pump at a temperature of 330° C, hydrogen pressure of 20 bar, a hydrogen to oleic acid ratio of 600(V/V) and a weight hourly space velocity of oleic acid of 1.0.
• the gaseous product of the reaction was carbon dioxide.
• a palladium metal catalyst supported on a basic hydrotalcite oxide support reaction not carried out under hydrogen pressure
• Process conditions were the same as for Example 1, except that the reaction was not carried out under hydrogen; the pressure within the reactor remained at 20 bar of nitrogen throughout the reaction. The gaseous product of the reaction was carbon dioxide.
• the hydrocarbon layer contained penta-, hexa-, hepta- and octa decanes.
• the iodine number of these products was negligible, indicating that the product contained only saturated paraffinic hydrocarbons.
• the conversion of the oleic acid to hydrocarbon products was 94 wt% at the end of 50 hours. From the ratio of heptadecane to (heptadecane + octadecane), the selectivity for decarboxylation was calculated to be 93%.
• a palladium metal catalyst supported on a magnesium oxide support [00053] The surface area of the support was approximately 99.5 m 2 per gram; the pore volume of the support was approximately 0.23 ml per gram of catalyst. The support was dried overnight at 250° C. The average pore width of the catalyst was approximately 3.4 nm; basicity of the catalyst, as determined by titration with 0.1 normal acetic acid, was approximately 0.11 mEq acetic acid per gram.
• An aqueous solution of palladium nitrate containing a sufficient amount of palladium metal for 5 wt% of palladium in the final catalyst was prepared.
• a suspension of the magnesium oxide support in the palladium nitrate solution was prepared.
• the palladium compound was reduced to the metallic state by addition of a sufficient amount of sodium borohydride.
• the catalyst was dried in a flow of nitrogen at 200° C for 5 hours.
• the reduced catalyst was loaded in a downflow, fixed bed reactor.
• a feedstock consisting of a mixture of oleic acid and normal hexadecane in equal weight proportions was passed over the catalyst with a HPLC pump at a temperature of 330° C , hydrogen pressure of 30 bar, a hydrogen to oleic acid ratio of 600 (V/V) and a weight hourly space velocity of oleic acid of 1.0.
• the gaseous product of the reaction was carbon dioxide.
• the conversion of the oleic acid to hydrocarbon products was 95 wt% at the end of 50 hours and 94 wt% after 150 hours.
• the hydrocarbon layer contained penta-, hexa-, hepta- and octa-decanes.
• the selectivity for decarboxylation was calculated to be 86% after 50 hours and 90% after 150 hours.
• the catalyst was evaluated according to conventional methods and determined not to have been deactivated.
• a palladium metal catalyst supported on a basic hydrotalcite oxide support reaction carried out under nitrogen pressure
• a nickel metal catalyst supported on a mixed oxide support of ceria-zirconia was prepared by coprecipitation of the mixed hydroxides of cerium and zirconium from an aqueous solution of the nitrates using sodium hydroxide as the precipitating agent.
• the support had a surface area of approximately 163 m 2 per gram; the pore volume of the support was approximately 0.165 ml per gram of catalyst.
• the support was then impregnated with a nickel nitrate solution by the incipient wetness method to yield 41.54 wt% of nickel oxide in the final catalyst.
• the material was dried in air at 120° C for 12 hours and calcined in air at 400° C for 12 hours.
• Basicity of this catalyst as determined by titration with 0.1 normal acetic acid, was approximately 0.21 mEq acetic acid per gram.
• the contents of cerium and zirconium oxides in the final catalyst were 25.6 wt% and 32.8 wt%, respectively.
• Surface area of the final catalyst was 134 m 2 per gram, and its pore volume was 0.12 ml per gram.
• a palladium metal catalyst supported on basic hydrotalcite catalyst as in Example 1 from a mixture of dodecanoic acid and oleic acid
• This example used the catalyst and support of Example 1 with the same process conditions as Example 1, except as noted with respect to temperature and pressure.
• the conversion of dodecanoic acid (as determined by gas chromatography) was 90%>, and the conversion of oleic acid (as determined by gas chromatography) was 96%.
• the selectivity in the conversion of dodecanoic acid (CI 1/(C11+C12)) value was 86%>, and the corresponding value for the selectivity in the conversion of oleic acid (C17/(C17+C18) was 91%.
• a palladium metal catalyst supported on a non-basic support material i.e., activated acidic aluminum oxide [00062]
• the surface area of the support was approximately 178 m 2 per gram; the pore volume of the support was approximately 0.35 ml per gram of catalyst.
• the support was dried overnight at 150° C.
• the average pore width of the catalyst was approximately 2.3 nm; basicity of the catalyst, as determined by titration with 0.1 normal acetic acid, was approximately 0.03 mEq acetic acid per gram.
• An aqueous solution of palladium chloride containing a sufficient amount of palladium metal for 5 wt% of palladium in the final catalyst was prepared and deposited on the support by incipient deposition. The catalyst was dried in a flow of nitrogen at 200° C for 5 hours.
• the dried catalyst was loaded in a downflow, fixed bed reactor and the palladium metal was reduced in flowing hydrogen at 350° C, 20 bar pressure for 6 hours.
• a feedstock consisting of a mixture of oleic acid and normal hexadecane in equal weight proportions was passed over the catalyst with a HPLC pump at a temperature of 350° C, hydrogen pressure of 30 bar, a hydrogen to oleic acid ratio of 600 (V/V) and a weight hourly space velocity of oleic acid of 1.0.
• the gaseous products of the reaction were carbon dioxide, ethane, propane, butane, as well as propylene and butane.
• the conversion of the palmitic acid to hydrocarbon products was 78 wt% at the end of 50 hours and 39 wt% after 150 hours.
• the hydrocarbon layer contained penta-, hexa-, hepta- and octa-decanes as well as olefins.
• the iodine number of the product, an indicator of unsaturation and presence of carbon-carbon double bonds, was 35 indicating that the product contained some olefins in addition to the saturated paraffinic hydrocarbons. From the ratio of heptadecane to octadecane, the selectivity for decarboxylation was calculated as 42% at the end of 50 hours.
• the catalyst was evaluated according to conventional methods, and was found to have sustained severe catalytic deactivation. Thus, even though this catalyst was active for the deoxygenation reaction, it deactivated fast and most of the oxygen of the carboxylate group was removed as H 2 0 rather than as C0 2 . As a consequence, hydrogen consumption during the process was relatively high.
• the surface area of the support was approximately 212 m 2 per gram; the pore volume of the support was approximately 0.23 ml per gram of catalyst.
• the catalyst was prepared by the deposition of ammonium molybdate and nickel nitrate on aluminum oxide, drying at 120° C and calcining it further in air at 500° C.
• the average pore width of the catalyst was approximately 2.5 nm; basicity of the catalyst, as determined by titration with 0.1 normal acetic acid, was approximately 0.03 mEq acetic acid per gram.
• the catalyst was loaded in a downflow, fixed bed reactor and dried overnight at 150° C to remove adsorbed matter like water and carbon dioxide. The catalyst was then sulfided for 24 hours at 200° C in a stream of hexadecane containing 100 ppm of dimethyl disulfide.
• a feedstock consisting of a mixture of oleic acid and normal hexadecane in equal weight proportions was then passed over the catalyst with a HPLC pump at a temperature of 330° C, hydrogen pressure of 45 bar, a hydrogen to oleic acid ratio of 1200 (V/V) and a weight hourly space velocity of oleic acid of 1.5.
• the gaseous product of the reaction was carbon dioxide.
• the conversion of the oleic acid to hydrocarbon products was 90 wt% at the end of 50 hours and 85 wt% after 150 hours.
• the hydrocarbon layer contained penta-, hexa-, hepta- and octa-decanes.
• the iodine number of these products indicating that the product contained only saturated paraffinic hydrocarbons and no olefins. From the ratio of heptadecane to octadecane, the selectivity for decarboxylation was calculated to be 60%.
• the support was prepared by the decomposition of calcium carbonate at 650° C in air.
• the surface area of the support was approximately 76.8 m 2 per gram; the pore volume of the support was approximately 0.28 ml per gram of catalyst.
• the support was dried overnight at 200° C.
• the average pore width of the catalyst was approximately 2.5 nm; basicity of the catalyst, as determined by titration with 0.1 normal acetic acid, was approximately 0.23 mEq acetic acid per gram.
• An aqueous solution of palladium nitrate containing a sufficient amount of palladium metal for 5 wt% of palladium in the final catalyst was prepared.
• a suspension of the calcium oxide support in the palladium solution was prepared.
• the palladium compound was reduced to the metallic state by addition of a sufficient amount of sodium borohydride.
• the catalyst was dried in a flow of nitrogen at 200° C for 5 hours.
• the reduced catalyst was loaded in a downflow, fixed bed reactor.
• a feedstock consisting of a mixture of palmitic acid and normal dodecane in equal weight proportions was passed over the catalyst with a HPLC pump at a temperature of 335° C, hydrogen pressure of 20 bar, a hydrogen to palmitic acid ratio of 600 (V/V) and a weight hourly space velocity of palmitic acid of 1.0.
• the gaseous product of the reaction was carbon dioxide.
• the conversion of the palmitic acid to hydrocarbon products was 88 wt% at the end of 50 hours and 85 wt% after 150 hours.
• the hydrocarbon layer contained dodecane, penta-and hexa decanes.
• the support was prepared by the decomposition of lanthanum carbonate at 700° C in air.
• the surface area of the support was approximately 85.7 m 2 per gram; the pore volume of the support was approximately 0.19 ml per gram of catalyst.
• the support was dried overnight at 300° C.
• the average pore width of the catalyst was approximately 3.6 nm; basicity of the catalyst, as determined by titration with 0.1 normal acetic acid, was approximately 0.21 mEq acetic acid per gram.
• An aqueous solution of palladium nitrate containing a sufficient amount of palladium metal for 5 wt% of palladium in the final catalyst was prepared.
• a suspension of the lanthanum oxide support in the palladium nitrate solution was prepared.
• the palladium compound was reduced to the metallic state by addition of sufficient amount of sodium borohydride.
• the catalyst was dried in a flow of nitrogen at 200° C for 5 hours.
• the reduced catalyst was loaded in a downflow, fixed bed reactor.
• a feedstock consisting of a mixture of palmitic acid and normal dodecane in equal weight proportions was passed over the catalyst with a HPLC pump at a temperature of 335° C , hydrogen pressure of 20 bar, a hydrogen to palmitic acid ratio of 600 (V/V) and a weight hourly space velocity of palmitic acid of 1.0.
• the gaseous product of the reaction was carbon dioxide.
• the conversion of the palmitic acid to hydrocarbon products was 90 wt% at the end of 50 hours and 85 wt% after 150 hours.
• the hydrocarbon layer contained dodecane, penta-and hexa-decanes.
• the iodine number of these products was negligible, indicating that the product contained mainly saturated paraffinic hydrocarbons. From the ratio of pentadecane to (pentadecane + hexadecane), the selectivity for decarboxylation was calculated to be 85% after 50 hours and 87% after 150 hours. The catalyst was evaluated according to conventional methods and determined not to have been deactivated.
• a palladium metal catalyst supported on basic hydrotalcite catalyst - fatty acids obtained from beef tallow
• Example 1 The catalyst and support of Example 1 were used, along with the process conditions of Example 1, except as noted with respect to temperature and pressure.
• Feedstock was a 50:50 wt. % mixture of n-hexadecane and C14-C18 fatty acids, the latter being obtained by hydrolyzing beef tallow supplied by Emery Oleochemicals LLC, Cincinnati,
• the beef tallow was black in color, with a density of 0.86 g/cc; flash point of 185° C; acid number of 198.5; iodine number of 56.9.
• Fatty acid content of feedstock was 3%> C14:0,
• the hydrocarbon chain length distribution (in wt%) in the liquid product obtained by gas chromatography was as follows: 9.3% C8, 10.5% C9, 11.9% CIO, 11.8% Cl l, 9.3% C12, 8.1% C13, 5.8% C14, 5.9$ C15, 17.3% CI 6, 4.1% CI 7, 3.5% CI 8, and 2.4% CI 9.
• Example 12 mixture of fatty acids from beef tallow and n- hexadecane
• catalyst of Example 11 over support of Example 11, by heating in an autoclave with 4 gm of the aforementioned palladium metal catalyst supported on a basic lanthanum oxide support catalyst at 350° C and 40 bar pressure of nitrogen for 3 hrs.
• the yield of liquid product was 78 wt%>, with the gaseous product being mainly carbon dioxide with 2% of methane.
• the product was colorless.
• the acid number of the liquid product was 1.1 and its iodine number was 1.7.
• the freezing point of the liquid product was
• Example 14 Production of aviation turbine fuel [00082]
• the liquid product of Example 13 was reacted with a hydroisomerization catalyst known in the art at 350° C and a hydrogen pressure of 40 bars for 3 hrs.
• the product had a freezing point of -64 C, a total sulfur content of 4 ppm (per ASTM D-1266), a smoke point of 26.7 mm (ASTM D-1322), net heat of combustion of 43.8 MJ/Kg (ASTM D-4809); approximately 10% of the products boiled at a temperature of less than about 254° C and about 90% boiled in a range between about 254° C - 300° C; and the elemental composition by %wt of 85%o carbon, 15% hydrogen, and 0%> oxygen.
• the liquid sample obtained by hydro isomerization of linear paraffins obtained in Example 13 meets ASTM D-1655, the standard specification for jet fuel.

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