EP1877355A1 - Procede de conversion en biocarburant - Google Patents

Procede de conversion en biocarburant

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Publication number
EP1877355A1
EP1877355A1 EP06745799A EP06745799A EP1877355A1 EP 1877355 A1 EP1877355 A1 EP 1877355A1 EP 06745799 A EP06745799 A EP 06745799A EP 06745799 A EP06745799 A EP 06745799A EP 1877355 A1 EP1877355 A1 EP 1877355A1
Authority
EP
European Patent Office
Prior art keywords
powder
weight percent
absorption
powders
catalyst
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP06745799A
Other languages
German (de)
English (en)
Inventor
Norikazu Nakamura
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Individual
Original Assignee
Individual
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Publication of EP1877355A1 publication Critical patent/EP1877355A1/fr
Withdrawn legal-status Critical Current

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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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • 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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • C10G1/086—Characterised by the catalyst used
    • 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, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
    • C10L1/026—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only for compression ignition
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • 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 is directed to a process, method, apparatus and materials for efficient conversion of waste vegetable oils into biofuel that does not use methanol as a reactant or catalyst.
  • Biofuel is a type of fuel made using non-petroleum based oils converted to allow combustion within power plants and engines as a replacement for heavy oils and diesel fuel.
  • Biofuels have desirable burning characteristics and are derived from renewable resources.
  • biofuels may be derived from vegetable oils processed from crops.
  • Vegetable oils are used extensively in food preparation in restaurants, hotels, hospitals and other large institutions.
  • the use of vegetable oils in food preparation generates substantial waste product that must be appropriately disposed of. Processing of these waste • vegetable oils into biofuel thus serves two beneficial purposes, creation of a clean and environmentally friendly fuel source and the elimination of waste disposal requirements .
  • waste vegetable oils are gathered and stored in large drums, for example 55 gallon drums.
  • the waste vegetable oils are allowed to sit for thirty days so that the sediments in the waste oil settle to the bottom of the container.
  • the top clarified oil is removed for processing in a column catalytic reaction chamber while the bottom layer of oil having retained sediments and oil are sent for disposal.
  • This process is inefficient as it requires extensive storage periods and there is still a significant amount of sediment contaminated waste oil that is sent for disposal. It is also a common process in the conversion of vegetable oils, whether virgin or waste oils, to use methanol as a reactant or catalyst.
  • the methanol based processes have as an advantage that the resulting biofuel can be used in engines without being mixed with other fuels.
  • a volume of vegetable oil is mixed with a solution of Methanol and Sodium hydroxide. Approximately 80% of the oil volume becomes fuel, and byproducts are glycerin, fatty acids.
  • NO x Nitrous Oxide
  • the range of increasing in NO x emissions resulting from biodiesel can be anywhere between 1-15% but is generally around 5%.
  • the complete lack of sulfur in biodiesel fuel allows the use of powerful NO x breaking catalysts that had been unusable.
  • the present invention is directed to a process, method, apparatus and materials for efficient conversion of waste vegetable oils into biofuel that does not use methanol as a reactant or catalyst.
  • Engines running on biofuel register a decrease in Nitrous Oxide (NO x ) emissions .
  • NO x Nitrous Oxide
  • methanol based processes result in a biofuel that does not mix well with other fuels, such as diesel fuel, so a small quantity of methanol derived biofuels must be mixed with other fuels, such as diesel fuel for automobiles.
  • the present invention is directed to a process, method, apparatus and materials for efficient conversion of waste vegetable oils into biofuel that does not use methanol as a reactant or catalyst.
  • the resulting biofuel is mixed with kerosene or heavy oil to form a stable diesel fuel grade fuel that is mixable with diesel fuel.
  • the process and apparatus are also applicable to the conversion of virgin vegetable oils and other waste or virgin oils, such as used motor oil, into fuels or fuel additives.
  • the waste oils are mixed with a blend of catalyst and absorption powders in a tank and heated to about 80 degrees centigrade for 40 to 60 minutes.
  • composition is then passed through a filter to remove the added powders, any sediments and certain contaminates in the oil including most carbon solids, as well as certain fatty acids and constituents of the waste oil.
  • the mixing and filtering process clarifies the resulting biofuel and enhances the energy content from 4,000 to 5,000 calories/gram to 9,000 to 10,000 calories/gram.
  • the clarified biofuel resulting from vegetable oils may then be blended with kerosene and filtered through the filter bed containing the removed sediments from the first filtering process or a powder mixture of absorption powders is added to the blended biofuel and kerosene, mixed for 40 to 60 minutes and then filtered.
  • a similar process can be used to recover and generate fuel grade oil from used or waste motor oil, with a resulting product that can be mixed with the biofuel derived from vegetable oils as a replacement for the kerosene additive to produce a light grade or heavy grade fuel oil.
  • FIG. 1 schematically depicts the processing apparatus of the present invention.
  • Figure 2 schematically depicts ' an alternate configuration of the processing apparatus of the present invention.
  • Figure 3 schematically depicts the fuel blending filter assembly and process used with the apparatus of Figure 2.
  • FIG. 1 schematically depicts a basic biofuel conversion apparatus 10 according to a first aspect of the present invention.
  • the apparatus 10 includes an oil tank 20 that is either a large storage tank or plurality of storage drums. Oil from tank 20 is routed via pipe 22 and pump 24 to a catalyst tank 30.
  • the catalyst tank 30 includes a mixing apparatus 32, for example a motor 34, shaft 36 and impeller 38.
  • the lower section of the catalyst tank 30 includes a heating assembly 40, for example a steam heat exchange system.
  • the catalyst tank 30 also includes a temperature sensor 42 and may include a level sensor 44.
  • the temperature sensor 42 is connected to a controller 46 that controls the pump 24 and the timing of the process as well as the temperature control for the heating assembly 40.
  • the mixture Upon completion of a reaction period in the catalyst tank 30, the mixture is delivered via a pipe 50 to pump 52.
  • the output of pump 52 is directed to a pipe 54.
  • Pipe 54 delivers the mixture to a high pressure filter assembly 60.
  • An air compressor 56 provides compressed air via pipe 50 to a junction valve 58 in pipe 54 upstream of the filter assembly 60.
  • the operations of the pump 52 and the compressor 56 are controlled by the controller 46.
  • the air compressor 56 is used at the end of a filtering process step to force oils in the pipes and falter assembly 60 through the filter in assembly 60.
  • the high pressure filter 60 filters the mixture from the catalytic tank 30 through a filter media 62.
  • the high pressure filter 60 may include a plurality of filter chambers assembled in series and fed via an axial flow path aligned with the inlet connection to pipe 54.
  • the filter media 62 has a 150 mesh fiberglass filter although a range about this mesh size is potentially applicable.
  • the primary output of high pressure filter 62 is provided to pipe 70.
  • a secondary output of high pressure filter 60 caused by leakage along the edges of the filter media 62 is captured in a tray 64 and delivered via pipe 66 to pump 68 which preferably directs the secondary output back to the inlet of the high pressure filter 60.
  • Pipe 70 from the high pressure filter 62 is connected to a valve 72 that directs the flow to a pipe 74 or recirculation pipe 76.
  • the output of pipe 74 is a fuel combination tank 80.
  • the output from recirculation pipe 76 is a return into the catalyst tank 30.
  • the fuel combination tank 80 includes a mixing assembly 82, including a motor 84 driving a shaft 86 having an impeller 88.
  • the reacted and filtered oil from the high pressure filter 60 is blended with a base fuel, either kerosene or light oil (heating oil) .
  • a base fuel either kerosene or light oil (heating oil) .
  • An absorption powder composition may also be added to the blend to enhance the chemical bonding of the blend and to remove additional contaminants such as ash and carbon particles.
  • FIG. 1 schematically depicts a second more advanced biofuel conversion apparatus 100 according to a second aspect of present invention.
  • Apparatus 100 includes oil tank 110 that is a large oil tank or plurality of storage drums. Oil from tank 110 is routed via pipe 112 to a pump 114 and the output of pump 114 is directed to pipe 116 having a control valve 118. Pipe 116 directs oil to a centrifugal separator 120.
  • the separator 120 has an outlet to pipe 122 and waste outlet to waste 124.
  • the separator 120 includes a motor 126 driving a centrifugal impeller assembly 128, to separate particulate matter from the oil in the centrifugal separator 120.
  • Pipe 122 delivers the cleaned oil to a holding tank 130. Oil from the holding tank 130 is pumped via pump 132 and pipe 134 into a catalytic mixing tank 140.
  • the catalytic mixing tank 140 includes a motor driven mixing assembly 142 with temperature sensor 144 and level sensor 146 similar to that described above for Figure 1. Further, the catalytic mixing tank 40 includes a heating assembly 148, for example a steam heat exchange system, to heat materials in the catalytic mixing tank 140.
  • Catalytic mixing tank 140 is also configured to receive powders from powder tank 150 via pipe 152 and auger screw feed 154. The output of mixing tank 140 is directed to a pipe 160 to a high pressure pump 170. The high pressure pump delivers the mixture via pipe 172 to a high pressure filter assembly 180.
  • Pipe 172 preferably also includes pressure sensor 174 and a junction valve 176 with junction valve 176 also being connected to an air compressor 178 for cleaning the pipes and filters at the end of a batch.
  • the high pressure filter assembly 180 is configured similar to that of high pressure filter assembly 60 of Figure 1. Accordingly, the high pressure filter assembly 180 includes a plurality of filter chambers 182 and filter media 184 to separate particulates and powder materials from the mixed oil composition passing therethrough.
  • the outlet product from high pressure filter assembly 180 is delivered via pipe 190 to a secondary filter assembly 194.
  • the secondary filter assembly 194 includes a directional valve 196 to separate the flow to one of two filters 198.
  • Each of the filters 198 includes a paper filter having a 250 to 300 mesh filter ' media.
  • the output side of each of filters 198 is directed to a pipe 200 to deliver the filtered fuel to a storage tank 220.
  • the high pressure assembly 180 also produces a secondary output to a tray 202.
  • the flow from the tray 202 is directed through pipe 204 to a pump 206.
  • the output of pump 206 is directed to pipe 208.
  • Pipe 208 terminates in a directional valve 210 which separate the flow into one of two pipes 212 each having a filter 214.
  • Each filter 214 includes a paper filter media having a mesh size of 250 to 300.
  • the output of the filters 214 is directed to a pipe 216 which delivers the output to the storage tank 220.
  • Figure 3 depicts the blending system for blending the processed oil with a base fuel such as kerosene or light oil.
  • the process starts with the storage tank 220 having filtered processed oil from the system of Figure 2.
  • the system also includes a fuel tank 222 for containing kerosene or light oil.
  • Each of the tanks 220 and 222 are configured to deliver oil or fuel via pipes 224 and 226, respectively, to a catalytic blending tank 230.
  • a high pressure filter may be included in pipe 224 to filter out any retained particulate matter.
  • the blending tank 230 includes a mixing assembly 232 having a motor 234 having a shaft 236 driving impeller 238.
  • the blending tank 230 may also include level sensor 240 and ' temperature sensor 242 to provide signals to a system controller 244 that monitors the level and temperature of the blending composition.
  • the blending tank 230 may also receive powdered materials from the powder tank 246, delivering powders via a pipe 248 to the catalytic blending tank 230.
  • the blended output from the blending tank 230 is delivered via a pipe 250 to a high pressure pump 260.
  • the output of the high pressure pump 260 is delivered via a pipe 262 to a high pressure filter assembly 270.
  • the pipe 262 preferably includes a pressure sensor 264 and a junction valve 266, the junction valve 266 also being connected to receive pressurized air from a compressor 268 used to clean out the pipes and high pressure filter assembly 270.
  • the blended composition is delivered to the high pressure filter assembly 270 to remove powder composition and particulate matter from the blend.
  • the output of the high pressure filter assembly 270 is directed to a pipe 280 which delivers the output to a filter assembly 290.
  • the filter assembly 290 includes a pair of filters 292 that may be used sequentially as discussed above with respect to the filter assembly 198.
  • the filters 292 include paper filter media having a 250 to 300 mesh filter media.
  • the output of the filter assembly 290 is directed to a biofuel tank 300.
  • the high pressure filter tank assembly 270 may also have a secondary output captured by a tray 272 and delivered to a pump 274 via a pipe 276.
  • the output from pump 274 is directed to filter assembly 278 having a pair of filters 282, operated sequentially.
  • Filter assembly 278 has an output pipe 284 delivering the filtered fuel ' mixture to biofuel tank 300.
  • the biofuel conversion process utilizing either the apparatus of Figure 1 or Figure 2 relies on the use of a catalytic material and absorption material composition.
  • the catalytic materials are blended and grounded to fine or super fine powder having a particle size less than 500 ⁇ m and preferably having a particle size of less than 100 ⁇ m.
  • the powdered catalytic materials are mixed with vegetable oil or waste vegetable oil in the catalytic tanks.
  • the catalytic powders are preferably:
  • an aluminum sludge zeolite material Na 2 O, SiO 2 , H 2 O
  • the powder composition added to the catalytic mixing tank includes powdered absorption materials, preferably selected from the group consisting of one or more of the following materials, with the preferred composition including each of the materials in the relative weight percentages indicated below:
  • SiO 2 Silicon Dioxide
  • AI 2 O 3 Aluminum Oxide
  • Fe 2 O 3 Iron Oxide
  • MgO Magnesium Oxide
  • CaO Calcium Oxide
  • an appropriate range for each of the component materials is 75 to 85 weight percent of silicon dioxide (Si ⁇ 2 ) r 10 to 14 weight percent of aluminum oxide (AI 2 O 3 ) , 2 to 4 weight percent of iron oxide (Fe 2 Oa) , 2 to 5 weight percent of magnesium oxide (MgO), and 0.5 to 2 weight percent of calcium oxide (CaO) .
  • a preferred composition contains a catalyst composition powder • consisting of: thirty weight percent of the aluminum sludge zeolite material, and 70 weight percent of Na 2 O, nSiO 2 , xH 2 0, or 70 weight percent of 0.75CaO, 0.2Na 2 O Al 2 O 3 , 2SiO 2 ,
  • the powders forming the ionic exchange or catalytic materials include an aluminum sludge zeolite. This aluminum sludge zeolite material may be processed to increase surface porosity by known methods such as an acid wash, and then cleaned with a calcium wash to leave a deposit of calcium within the porosity of the zeolite .
  • the amount of catalytic powder for processing each 100 liters of vegetable oil is 250 to 750 grams with a preferred range of 450 to 550 grams. For most processes, however, it has been found that an adequate amount of catalytic powder without excess or waste is 500 grams for 100 liters of vegetable oil.
  • the amount of the absorption powder for 100 liters of vegetable oil is in a range of 1 to 2 kilograms for a resulting dark oil or a range up to 3 kilograms -to produce a light or more clarified oil.
  • a preferred range for the amount powders to yield a dark oil having a higher carbon content would be 1.5 kilograms of absorption powder to 100 liters of process oil to 3 kilograms of absorption powder used to produce ' a very clear or clarified oil. Adding in excess of 3 kilograms is not necessary and leads to excess usage and waste of the absorption powders.
  • the powders in the amounts described above are blended into the waste or virgin vegetable oils and mixed for a period of 40 to 60 minutes as the mixture is heated to a reaction temperature of 60° C to 80° C and, preferably, at the upper end of this range such that the temperature is controlled to between 78° to 80° C by the heat exchange assembly and the controller. It is also preferred that the material be maintained at the reaction temperature for at least 20 minutes within the 40 to 60 minute interval.
  • the materials are processed at a pressure of approximately 0.5 MPa through the filter media.
  • the materials are processed at an initial flow rate of approximately 90 liter per minute in a fresh filter media although the processing rate will be reduced with the build up of a filter cake on the filter media.
  • materials be recirculated at the beginning of any filtering process, in particular if a new filter media has been installed in the high pressure filter assembly.
  • the recirculation of the initial processed product is beneficial to wet the filter media and to build a cake of powder including catalytic powder and absorption powder on the surface of the filter media. It is preferred that the thickness of the cake be 2 to 3 mm before the filter oil is routed to the fuel combination tank 80 or tank 220.
  • the filter media can be used to process 2 to 3 batches of waste oil before the filter requires cleaning, so the cake build up on the surface of the filter media and within the high pressure filter may be substantial. A cake buildup of 2 to 4 cm in thickness thus may increase the effectiveness of the filter process.
  • the absorption materials may allow fatty acids to combine to be of a size that can be retained either by the cake or by the filter media in the filtering step.
  • the absorption powders as discussed above may be added to and mixed with the blend in a range of approximately 1 kilogram of absorption powder to 200 liters of combined base oil and kerosene.
  • the range of absorption powders to 200 liters of fuel would be from 1 to 3 kilograms.
  • the preferred range of absorption powder would be 0 to 3 kilograms per 200 liters of combined processed oil or kerosene. It has been found that waste vegetable oil processed according to the foregoing assembly and method provides a biofuel component having the following properties: pH 7.0
  • the biofuel produced from waste vegetable oil utilizing the foregoing technology is stable and, when once mixed with the kerosene or light oil it can be combined with other diesel fuels or light oils to be burned in an engine or combustion process without chemical separation or decomposition.
  • the pH of the biofuel is neutral and the biofuel has an energy content that is consistent with the energy content of other fuels which leads to the biofuel being stable when combined with other fuels .
  • the blended composition may not require absorption powder if the high pressure filter assembly includes substantial cake deposits on the surface of the filter media.
  • the waste oil can be processed to remove particulates, substantially all, if not all carbon, certain fatty acids, and other contaminates.
  • the pH of a waste oil is neutralized to a pH of approximately 7.0, which occurs because of compounds both within the catalytic powders and the first three absorption powders.
  • the catalytic function of the catalytic powders increases or ionizes oils to increase energy content and combustibility and allow blending with kerosene or light oils.
  • the steps necessary to process waste oil into biofuel are combined and the processing time for a batch to pass through the entire process and system of the present invention may take less than two hours to per batch.
  • Each batch can be scalable within the foregoing system so that a small facility could process a batch 100 liters while a large facility could process a batch of several thousand liters in each of the tanks.
  • the process is equally applicable to virgin vegetable oils to convert these virgin oils to biofuels or biofuel additives.
  • the apparatus described above may be used to process petroleum based oil, such as used motor oil, to convert the petroleum oil into a fuel grade oil or fuel additive.
  • the powdered catalytic materials for petroleum based oils include 65 to 75 weight percent sodium monoxide, silicon dioxide and water in the formula: Na 2 O, nSi ⁇ 2, XH2O, mixed with 25 to 35 weight percent aluminum sludge zeolite for processing mineral or petroleum based oils.
  • the filter media may be cleaned to remove the cake build up.
  • the byproduct material in the cake build up primarily consists of the catalytic powders and the absorption powders as well as carbon, particulates, fatty acids, and other contaminants as well as small amounts of oil.
  • This byproduct material may be mixed with cement powder and water and molded to form bricks or other configurations which may be used for paving and construction materials. It has been found that a mixture of 75% byproduct and 25% cement powder is sufficient to form a stable and hardened brick. Other blends and ratios of byproduct to cement or byproduct and binder materials can be used so as to form useful construction materials.
  • all products and byproducts of the process according to this invention are either useful biofuels or used as construction products, Alternatively, the byproduct from the filter media may be used as a fertilizer and soil conditioner, as opposed to being formed into hardened materials, as the materials contained in the byporoduct materials are primarily mineral compositions and organic materials.

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

Abstract

L’invention concerne un processus, un procédé, un appareil et des matériaux permettant de convertir efficacement les déchets d’huiles végétales en biocarburant n’utilisant pas de méthanol en tant que réactif ou catalyseur. Le biocarburant obtenu est mélangé avec du kérosène ou de l’huile lourde afin de parvenir à un carburant de type diesel stable qui peut être mélangé avec un carburant diesel. De plus, lesdits procédé et appareil peuvent également être utilisés lors de la conversion d’huiles vierges végétales ainsi que d’autres déchets ou huiles vierges, telle l’huile de moteur usée, en carburants ou additifs pour carburant.
EP06745799A 2005-04-22 2006-04-21 Procede de conversion en biocarburant Withdrawn EP1877355A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US11/112,600 US20060236595A1 (en) 2005-04-22 2005-04-22 Biofuel conversion process
PCT/JP2006/308918 WO2006115284A1 (fr) 2005-04-22 2006-04-21 Procede de conversion en biocarburant

Publications (1)

Publication Number Publication Date
EP1877355A1 true EP1877355A1 (fr) 2008-01-16

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EP06745799A Withdrawn EP1877355A1 (fr) 2005-04-22 2006-04-21 Procede de conversion en biocarburant

Country Status (8)

Country Link
US (1) US20060236595A1 (fr)
EP (1) EP1877355A1 (fr)
JP (1) JP2008536952A (fr)
CN (1) CN101163655A (fr)
BR (1) BRPI0608492A2 (fr)
CA (1) CA2606208A1 (fr)
TW (1) TW200702433A (fr)
WO (1) WO2006115284A1 (fr)

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CA2606208A1 (fr) 2006-11-02
JP2008536952A (ja) 2008-09-11
CN101163655A (zh) 2008-04-16
WO2006115284A1 (fr) 2006-11-02
BRPI0608492A2 (pt) 2010-11-30
US20060236595A1 (en) 2006-10-26
TW200702433A (en) 2007-01-16

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