Classifications

• • C—CHEMISTRY; METALLURGY
  • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
  • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
  • C11B3/00—Refining fats or fatty oils
  • C11B3/008—Refining fats or fatty oils by filtration, e.g. including ultra filtration, dialysis
• • 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
  • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
• • 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
  • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
  • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
  • C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
  • C10G45/08—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
• • C—CHEMISTRY; METALLURGY
  • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
  • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
  • C11B3/00—Refining fats or fatty oils
  • C11B3/001—Refining fats or fatty oils by a combination of two or more of the means hereafter
• • C—CHEMISTRY; METALLURGY
  • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
  • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
  • C11B3/00—Refining fats or fatty oils
  • C11B3/02—Refining fats or fatty oils by chemical reaction
  • C11B3/04—Refining fats or fatty oils by chemical reaction with acids
• • 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
  • C10G2300/1014—Biomass of vegetal origin
• • 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
  • C10G2300/1018—Biomass of animal origin
• • 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
  • C10G2300/201—Impurities
• • 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
  • C10G2300/201—Impurities
  • C10G2300/202—Heteroatoms content, i.e. S, N, O, P
• • 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
  • C10G2300/201—Impurities
  • C10G2300/205—Metal content
• • 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
  • C10G2300/40—Characteristics of the process deviating from typical ways of processing
  • C10G2300/4081—Recycling aspects
• • 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
  • C10G2300/40—Characteristics of the process deviating from typical ways of processing
  • C10G2300/44—Solvents
• • 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
  • C10G2300/80—Additives
  • C10G2300/805—Water
• • 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
  • C10G2400/04—Diesel oil
• • 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 present invention relates generally to the process for removing impurities from triglycerides, especially prior to the conversion of triglycerides to fuel range hydrocarbons.
• One possible alternative source of hydrocarbons for producing fuels and chemicals is the natural carbon found in plants and animals, such as for example, oils and fats.
• oils and fats such as those contained in vegetable oil
• Bio Diesel is one such product and may be produced by subjecting a base vegetable oil to a transesterification process using methanol in order to convert the base oil to methyl esters. After processing, the products produced have some what similar combustion properties as compared to petroleum-derived hydrocarbons.
• Bio-Diesel as an alternative fuel has not yet been proven to be cost effective.
• Bio-Diesel often exhibits "gelling” thus making it unable to flow, which limits its use in pure form in cold climates.
• Unmodified vegetable oils and fats have also been used as additives in diesel fuel to improve the qualities of the diesel fuel, such as for example, the lubricity.
• problems such as injector coking and the degradation of combustion chamber conditions have been associated with these unmodified additives.
• cetane (C 16 H 34 ), heptadecane (C 17 H 36 ) and octadecane (C 18 H 38 ) by definition have very good ignition properties (expressed as cetane rating), it is often desired to add paraffmic hydrocarbons in the C 16 -C 18 range, provided that other properties of the additive (such as for example, viscosity, pour point, cloud point, etc.,) are congruent with those of the diesel fuel.
• the final treated triglyceride containing feedstock may be converted to fuel range hydrocarbons via hydrotreating processes.
• a process comprising (a) providing a feedstock comprising at least one triglyceride and one type of impurities; (b) admixing an organic solvent with the feedstock for a contacting time to form a mixture; (c) settling the mixture for a retention time to form a layer of treated feedstock, a layer of impurities, and a layer of organic solvent; and (d) recovering the layer of treated feedstock from the mixture, wherein the treated feedstock comprises less than 50% of the amount of the impurities than which is in the feedstock.
• a process comprising contacting the treated feedstock from the first embodiment of the invention with a hydrotreating catalyst in a reaction zone under a condition sufficient to produce a reaction product containing diesel boiling range hydrocarbons, such condition includes a pressure of less than about 2000 psig and a temperature in the range of from about 260°C to about 430°C.
• a process comprising (a) providing a feedstock comprising at least one triglyceride and one type of impurities; (b) subjecting the feedstock to a first separation device to remove at least 25 % of the impurities from the feedstock and to produce a first effluent stream; (c) admixing an acid or acid anhydride with the first effluent stream for a first contact time to form a first mixture; (d) admixing water with the first mixture for a second contact time to form a second mixture; (e) subjecting the second mixture to a second separation device to form an aqueous phase and oil phase; and (f) subjecting the oil phase to a third separation device to remove another portion of the impurities from the oil phase to produce a treated feedstock.
• a process comprising contacting the treated feedstock from the third embodiment of the invention with a hydrotreating catalyst in a reaction zone under a condition sufficient to produce a reaction product containing diesel boiling range hydrocarbons, such condition includes a pressure of less than about 2000 psig and a temperature in the range of from about 260°C to about 430°C.
• triglycerides or fatty acids of triglycerides, or mixtures thereof may be converted to form a hydrocarbon mixture useful for liquid fuels and chemicals.
• the term, "triglyceride,” is used generally to refer to any naturally occurring ester of a fatty acid and/or glycerol having the general formula CH 2 (OCOR 1 )CH(OCOR 2 )CH 2 (OCOR 3 ), where R 1 , R 2 , and R 3 are the same or different, and may vary in chain length.
• triglycerides useful in the present invention include, but are not limited to, animal fats (e.g.
• poultry grease edible or inedible beef fat also referred as tallow, milk fat, and the like
• vegetable oils e.g. soybean, corn oil, peanut oil, sunflower seed oil, coconut oil, babassu oil, grape seed oil, poppy seed oil, almond oil, hazelnut oil, walnut oil, olive oil, avocado oil, sesame, oil, tall oil, cottonseed oil, palm oil, ricebran oil, canola oil, cocoa butter, shea butter, butyrospermum, wheat germ oil, illipe butter, meadowfoam, seed oil, rapeseed oil, borage seed oil, linseed oil, castor oil, vernoia oil, tung oil, jojoba oil, ongokea oil, algae oil, jatropha oil, yellow grease such as those derived from used cooking oils, and the like), and mixtures and combinations thereof.
• vegetable oils e.g. soybean, corn oil, peanut oil, sunflower seed oil, coconut oil, babassu oil, grape seed oil, poppy seed
• the triglyceride comes with impurities such as phosphorus, metals (e.g. Alkali metals, alkali earth metals, or etc), solids, proteins and bone materials, or any combinations thereof.
• impurities such as phosphorus, metals (e.g. Alkali metals, alkali earth metals, or etc), solids, proteins and bone materials, or any combinations thereof.
• the amounts of these elements/compounds are generally in the range of from about 0 ppmw to about 10,000 ppmw.
• the feedstock is generally kept in the range of the lowest temperature at which the feedstock remains as a liquid to 15O 0 C for at least lminute.
• an organic solvent is added to this feedstock. Any organic solvent may be used, in one embodiment of the invention, any type of a polar organic solvent, such as ethylene glycol, may be used.
• the amount of organic solvent added to the feedstock may vary depend upon the amount of the feedstock to be mixed. According to the present invention, the amount of the organic solvent added is in the range from 0.1 to 50 wt%, calculated on the weight of triglyceride containing feedstock.
• the organic solvent added to the feedstock is given sufficient contacting time to mix with the feedstock to thereby forming a mixture.
• the contacting time required for mixing the organic solvent with the feedstock may be affected by temperature of the feedstock as well as the types of device for mixing. In one embodiment, such contacting time is at least lminute under dynamic mixing action provided by devices such as such as stirrer or high shear mixers.
• the temperature of the mixture is maintained in the range of from the lowest temperature at which the mixture remains as a liquid to 150 0 C during the mixing of organic solvent with the feedstock.
• the mixture is allowed to set for a sufficient retention time, usually without any mixing action, to thereby form a layer of treated feedstock, a layer of impurities, and a layer of organic solvent.
• the retention time required in this step may be affected by the temperature of the mixture. In one embodiment, such retention time is at least lminute.
• the temperature of the mixture is maintained in the range of from the lowest temperature at which the mixture remains as a liquid to 150 0 C during the setting of the mixture.
• the layer of the treated feedstock is recovered but not limited by separation funnel.
• the treated feedstock after the inventive process comprises less than 50% of the amount of the impurities than it is in the feedstock prior to the inventive process.
• a polar organic solvent e.g. ethylene glycol
• the treated feedstock after the inventive process comprises less than 80% of the amount of the impurities than it is in the feedstock prior to the inventive process.
• the layer of organic solvent may also be recycled for using in the treating of additional feedstock.
• a feedstock comprising triglyceride and impurities is subject to a first separation device where in at least 25% of the impurities may be removed from the feedstock.
• Any suitable separation device capable of separating the solid from an oil phase feed may be used.
• a first separation device according to one embodiment of the current invention is a commercially available bag or cartridge filter with a pore size of at least 0.1 ⁇ m.
• the first separation device of choice is a commercially available bag or cartridge filter with a pore size anywhere from 2 to 7 ⁇ m, which removes at least 50% of the impurities from the inedible tallow feedstock to produce the first effluent stream.
• the acid or acid anhydride in principle all inorganic and organic acids having a pH of from 0-6 as measured at 2O 0 C in a one molar aqueous solution, may be used.
• phosphoric acid, sulfuric acid, nitric acid, acetic acid, citric acid, tartaric acid, succinic acid, etc. or mixtures of such acids.
• the acids or acid anhydride may be added in any concentration, in one embodiment of this invention, an aqueous solution of the acid added contains 0.1 to 99.9% of the acid in H 2 O.
• the acid or acid anhydride after the acid or acid anhydride being added to the first effluent stream, it is given a sufficient contacting time to mix with the first effluent stream to form the first mixture.
• the contacting time required for homogeneously mixing the acid or acid anhydride with the first effluent stream may be affected by temperature of the first effluent stream as well as the types of device for mixing. In one embodiment, such contacting time is at least 0.1 minute under dynamic mixing action provided by devices such as stirrer or high shear mixers. In another embodiment, such contacting time is about 0.1 to 60 minutes under dynamic mixing action provided by devices such as stirrer or high shear mixers.
• the temperature of the first mixture is maintained in the range of from the lowest temperature at which the first effluent stream remains as a liquid to 150 0 C during contacting time mentioned above.
• a small amount of water is added.
• the amount of water added is in the range from 0.1 to 10 wt%, calculated on the oil.
• such contacting time is at least 1 minute under dynamic mixing action provided by devices such as stirrer or high shear mixers. In another embodiment, such contacting time is about 1-1000 minutes under dynamic mixing action provided by devices such as stirrer or high shear mixers.
• the second mixture is then subject to a second separation device by which an aqueous phase and oil phase are separated.
• a second separation device capable of separating an aqueous from an oil phase may be used.
• a second separation device according to one embodiment of the current invention is a commercially available centrifugation unit.
• the oil phase separated from the second mixture is subject to a third separation device wherein another portion of the impurities may be removed from the feedstock.
• Any suitable separation device capable of separating solids from an oil phase feed may be used.
• the third separation device according to one embodiment of the current invention is a commercially available bag or cartridge filter with a pore size of at least 0.1 ⁇ m.
• the third separation device of choice is a commercially available bag or cartridge filter with a pore size between from 0.1 to 0.5 ⁇ m.
• the useful catalyst compositions in the present invention include catalysts effective in the conversion of triglycerides to hydrocarbons when contacted under suitable reaction conditions.
• suitable catalysts include hydrotreating catalysts.
• the term "hydrotreating” as used herein, generally describes a catalyst that is capable of utilizing hydrogen to accomplish saturation of unsaturated materials, such as aromatic compounds.
• hydrotreating catalysts useful in the present invention include, but are not limited to, materials containing compounds selected from Group VI and Group VIII metals, and their oxides and sulfides.
• Examples of hydrotreating catalysts include but are not limited to alumina supported cobalt-molybdenum, nickel sulfide, nickel-tungsten, cobalt-tungsten and nickel-molybdenum.
• the metal of the catalyst useful in the present invention is usually distributed over the surface of a support in a manner than maximizes the surface area of the metal.
• suitable support materials for the hydrogenation catalysts include, but are not limited to, silica, silica-alumina, aluminum oxide (Al 2 O 3 ), silica-magnesia, silica-titania and acidic zeolites of natural or synthetic origin.
• the metal catalyst may be prepared by any method known in the art, including combining the metal with the support using conventional means including but not limited to impregnation, ion exchange and vapor deposition.
• the catalyst contains molybdenum and cobalt supported on alumina or molybdenum and nickel supported on alumina.
• this process in accordance with an embodiment of the present invention can be carried out in any suitable reaction zone that enables intimate contact of the treated feed and control of the operating conditions under a set of reaction conditions that include total pressure, temperature, liquid hourly space velocity, and hydrogen flow rate.
• the catalyst can be added first to the reactants and thereafter, fed with hydrogen.
• fluidized bed reactor denotes a reactor wherein a fluid feed can be contacted with solid particles in a manner such that the solid particles are at least partly suspended within the reaction zone by the flow of the fluid feed through the reaction zone and the solid particles are substantially free to move about within the reaction zone as driven by the flow of the fluid feed through the reaction zone.
• fluid denotes gas, liquid, vapor and combinations thereof.
• the reaction conditions at which the reaction zone is maintained generally include a temperature in the range of from about 260°C to about 430°C. Preferably, the temperature is in the range of from about 310°C to about 370°C.
• the pressure is generally in the range of from about 100 pounds per square inch gauge (psig) to about 2000 psig. Generally, in a fixed bed reactor, the pressure is in the range of from about 100 psig to about 1500 psig. In a fixed bed reactor, the pressure can also be about 600 psig. In a fluidized bed reactor, the pressure is generally in the range of from about 400 psig to about 750 psig, and can also be about 500 psig.
• An inedible tallow feed stock is provided. Such feedstock was subject to a commercially available sintered metal filter with a pore size of 2 ⁇ m to remove solids from the feedstock. The filtered feedstock was then mixed with phosphoric acid at the concentration of 75-85% for about 3minutes followed by the addition of 5wt% H 2 O. The tallow/phosphoric acid/water was further mixed for 60 minutes followed by a centrifugal step in which an aqueous phase and oil phase were separated. Sample of feedstock at the various stages were obtained and measured. As shown in Table 1, the results of this experiment indicates that there are a significant (more than 50%) reduction of the metals, phosphorus and solids concentration achieved by just after passing the feedstock through a sintered metal filter with pore size of 2 ⁇ m alone.
• the oil phase feed is further subject to a commercially available sintered metal filter with a pore size of 0.5 ⁇ m to remove some solids from the feedstock. Thereby, significantly purified inedible tallow is obtained.

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• Chemical & Material Sciences (AREA)
• Life Sciences & Earth Sciences (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Engineering & Computer Science (AREA)
• Organic Chemistry (AREA)
• Microbiology (AREA)
• General Chemical & Material Sciences (AREA)
• Wood Science & Technology (AREA)
• Fats And Perfumes (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

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• 2010
  • 2010-07-20 US US12/840,033 patent/US20110047866A1/en not_active Abandoned
  • 2010-07-27 EP EP10739790A patent/EP2473464A2/de not_active Withdrawn
  • 2010-07-27 WO PCT/US2010/043405 patent/WO2011025616A2/en not_active Ceased
  • 2010-07-27 CA CA2769716A patent/CA2769716A1/en not_active Abandoned
  • 2010-07-27 BR BR112012004530A patent/BR112012004530A2/pt not_active Application Discontinuation
  • 2010-07-27 AU AU2010286909A patent/AU2010286909A1/en not_active Abandoned

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