WO2020026068A1 - Composition et procédé pour la production de biocarburant à partir de sous-produits et de déchets de raffinerie d'huile comestible - Google Patents

Composition et procédé pour la production de biocarburant à partir de sous-produits et de déchets de raffinerie d'huile comestible Download PDF

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WO2020026068A1
WO2020026068A1 PCT/IB2019/056245 IB2019056245W WO2020026068A1 WO 2020026068 A1 WO2020026068 A1 WO 2020026068A1 IB 2019056245 W IB2019056245 W IB 2019056245W WO 2020026068 A1 WO2020026068 A1 WO 2020026068A1
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Prior art keywords
oil
biofuel
composition
diesel
present
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PCT/IB2019/056245
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English (en)
Inventor
Shweta VIRARAGHAVAN
Radhika VIRARAGHAVAN
S Viraraghavan
Suhas Sadanand DIXIT
Original Assignee
Viraraghavan Shweta
Viraraghavan Radhika
S Viraraghavan
Dixit Suhas Sadanand
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Application filed by Viraraghavan Shweta, Viraraghavan Radhika, S Viraraghavan, Dixit Suhas Sadanand filed Critical Viraraghavan Shweta
Publication of WO2020026068A1 publication Critical patent/WO2020026068A1/fr

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    • 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
    • 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 a field of biofuel production and in particular to a composition and method for the production of biofuel from edible oil refinery by-products and wastes.
  • Edible Oils Refining is required for crude vegetable oils & fats or animal oils & fats to be used for cooking and frying food products.
  • crude edible oils are refined either through a process of chemical refining (by using chemicals like caustic soda) or physical refining (by use of high temperature) to form edible oil and by-products.
  • the by-products produced during the process are inedible, some are further processed and others are disposed-off, as they are not seen as commercially valuable.
  • US20160024394A1 relates to a method for producing a fuel or solvent comprising a branched alkane, a branched alkene, or a combination thereof comprising heating a fatty acid in the presence of one or more alkenes to produce fuel.
  • the fatty acid resources include vegetable oil, animal fats, lipids derived from bio solids, spent cooking oil, lipids, phospholipids, soapstock or other sources of triglycerides, diglycerides or monoglycerides.
  • US8100990B2 provides a method of integrated biomass fast pyrolysis and fractionation.
  • the method further comprises production of agglomerated biochar from one or more added binders such as lignosulfonates, vegetable oil, water, whole bio-oil, bio-oil fractions, biomass, clay, bitumen, coal and any combinations thereof.
  • binders such as lignosulfonates, vegetable oil, water, whole bio-oil, bio-oil fractions, biomass, clay, bitumen, coal and any combinations thereof.
  • US8317883B1 provides bio-oil produced from mustard family seeds. Further, the bio-oil is produced by a method involving pyrolyzing the feedstock to produce bio-oil, bio-char and non-condensable gases, removing the bio-char from the bio-oil, condensing the bio-oil and precipitating the bio-oil.
  • WO2014209973A1 provides a catalyst useful for biomass pyrolysis and bio-oil upgrading. Further, the catalysts are especially useful for microwave- and induction-heating based pyrolysis of biomass, solid waste and other carbon containing materials into bio-oil.
  • alkali catalysts such as sodium or potassium hydroxides, carbonates or alkoxides, which are very sensitive to the presence of water, free fatty acids and require more amount of carbinol. Since, the alkali catalysts must be neutralized, giving rise to wastewaters, they cannot be reutilized and glycerol is obtained as an aqueous solution of relatively low purity.
  • An object of the present invention is to provide a composition of biofuel that can be prepared from the edible oil refinery waste and by products.
  • Another object of the present invention is to provide a method for the production of biofuel from processing edible oil waste and by-products that requires no external energy source to manufacture after process initiation.
  • Another object of the present invention is to provide a method for the production of biofuel which possess properties similar to that of High Speed Diesel (HSD).
  • HSD High Speed Diesel
  • Another object of the present invention is to provide a composition of biofuel that can be put to various fuel related uses, such as a direct fuel for use in vehicles, a component of a biofuel or blend, a fuel additive, a fuel supplement, as fuel for generation of power and for use in boilers, heat generators, furnaces etc.
  • Another object of the present invention is the generation of a high- energy gaseous product that has energy properties similar to natural gas or Liquefied Petroleum Gas (LPG).
  • LPG Liquefied Petroleum Gas
  • Another object of this invention is the production of a solid by product, such as biochar, which is high in essential nutrients required by plants such as potassium and phosphorous.
  • a method for the production of biofuel comprises steps of, but not limited to, providing a plurality of raw materials from edible oil refinery, performing pyrolysis of the plurality of raw materials in a reactor at a bed temperature of 500 - 550 Q C to obtain vapors or a liquid on rapid cooling of the vapors by performing step wise cooling of the vapors to obtain liquid fractions of different properties or distillation of the obtained liquid from rapid cooling of the vapors to make fractions.
  • the pyrolysis is performed in the presence of a catalyst which is derived from the plurality of raw materials.
  • the edible oil is selected from, but not limited to, a group comprising, sunflower oil, rice bran oil, soybean oil, peanut oil, palm oil, mustard oil and other soft oils.
  • the other soft oils are selected from, but not limited to, a group comprising, rapeseed oil, sesame oil, safflower oil, canola oil, mustard oil and corn oil.
  • the plurality of raw materials are obtained from, but not limited to, edible oil refinery by-products, co-products and effluent.
  • the plurality of raw materials are selected from, but not limited to, a group comprising, spent clay, soap stock, spent wax and Effluent Treatment Plant (ETP) Waste.
  • ETP Effluent Treatment Plant
  • the pyrolysis produces products selected from, but not limited to, a group comprising, a high calorific value liquid, a high calorific value gas, a solid by-product. Further, high calorific value gas produced during pyrolysis is further used in the process itself to provide the heat energy for pyrolysis.
  • the high calorific value gas produced during pyrolysis is further recycled in the process or can be sold as a fuel gas which has more than 3 times the calorific value of methane.
  • the solid by-product is char, which on oxidation can be reused in the Vegetable oil refinery as a Bleaching clay or as an ingredient for de waxing.
  • the step of providing comprising the steps of drying the plurality of raw materials by using a double drum dryer and delivering the dried raw material in the reactor for pyrolysis.
  • the heat energy produced during the step wise cooling of the vapors is used as input energy for the step of providing.
  • the heat energy is used to generate stem which eventually heat the double drum dryer.
  • a biofuel composition comprises an olefins present in a range of, but not limited to, 18%- 20% by weight, a paraffin present in a range of, but not limited to, 67.5% - 69.5% by weight, an aromatic compound present in a range of, but not limited to, 1 %-1.5% by weight, an aqueous phase present in a range of, but not limited to, 0.5%-1 % by weight, a residual oil coke present in a range of, but not limited to, 8%-10% by weight and other compounds present in a range of, but not limited to, 5%- 7%by weight.
  • the composition has gross calorific value in a range of, but not limited to, 10,000 Kcal/Kg - 10,810 Kcal/Kg.
  • the composition has density in a range of, but not limited to, 0.825 g/ml -0.90 g/ml.
  • the composition has a cetane index in the range of 46 - 60.
  • the composition has Sulphur content in an amount of ⁇ 10 ppm.
  • Fig. 1 is a flow chart illustrating a method for the preparation of biofuel composition, in accordance with an embodiment of the present invention
  • Fig. 2 illustrates a heavy-duty multi-cylinder engine setup, for testing of the heavy fraction of the biofuel, in accordance with an embodiment of the present invention
  • Fig. 3 illustrates a graph showing comparison of dynamic fuel injection timings of diesel, neat heavy fraction biofuel and heavy fraction biofuel-diesel blends (25%, 50%, 75% and 100%) at varying loads, with a biofuel of Cetane Index 46, in accordance with an embodiment of the present invention
  • Fig. 4 illustrates a graph showing comparison of ignition delay between diesel, neat heavy fraction biofuel and heavy fraction biofuel- diesel blends at varying loads, with the biofuel of Cetane Index 46, in accordance with an embodiment of the present invention
  • Fig. 5A illustrates a graph showing comparison of cylinder pressure histories at 20% between diesel, neat heavy fraction biofuel and heavy fraction biofuel-diesel blends, with the heavy fraction biofuel of cetane index 46, in accordance with an embodiment of the present invention
  • Fig. 5B illustrates a graph showing comparison of cylinder pressure histories at 80% load between diesel, neat heavy fraction biofuel and heavy fraction biofuel-diesel blends, with the heavy fraction biofuel of cetane index 46, in accordance with an embodiment of the present invention
  • Fig. 5C illustrates a graph showing comparison of peak pressures at varying loads between diesel, neat heavy fraction biofuel and heavy fraction biofuel-diesel blends, with the heavy fraction biofuel of cetane index 46, in accordance with an embodiment of the present invention
  • Fig. 6 illustrates a graph showing comparison of maximum rate of pressure rise between diesel, neat heavy fraction biofuel and heavy fraction biofuel-diesel blends at varying loads, with the heavy fraction biofuel of cetane index 46, in accordance with an embodiment of the present invention
  • Fig. 7A illustrates a graph showing comparison of heat release rates at 20% load at varying loads between diesel, neat heavy fraction biofuel and heavy fraction biofuel-diesel blends, with a heavy fraction biofuel of cetane index 46, in accordance with an embodiment of the present invention
  • Fig. 7B illustrates a graph showing comparison of heat release rates at 80% load at varying loads between diesel, neat heavy fraction biofuel and heavy fraction biofuel-diesel blends, with a heavy fraction biofuel of cetane index 46, in accordance with an embodiment of the present invention
  • Fig. 7C illustrates a graph showing comparison of combustion duration at varying loads between diesel, neat heavy fraction biofuel and heavy fraction biofuel-diesel blends, with the heavy fraction biofuel of cetane index 46, in accordance with an embodiment of the present invention
  • Fig. 8A illustrates a graph showing comparison of Brake Specific Fuel Consumption (BSFC) of the engine with diesel, neat heavy fraction biofuels and heavy fraction biofuels-diesel blends at varying loads, with the heavy fraction biofuel of cetane index 46, in accordance with an embodiment of the present invention
  • Fig. 8B illustrates a graph showing comparison of Brake Specific Energy Consumption (BSEC) of the engine with diesel, neat heavy fraction biofuels and heavy fraction biofuels-diesel blends at varying loads, with the heavy fraction biofuel of cetane index 46, in accordance with an embodiment of the present invention
  • Fig. 8C illustrates a graph showing comparison of brake thermal efficiency of the engine with diesel, neat heavy fraction biofuels and heavy fraction biofuels-diesel blends at varying loads, with the heavy fraction biofuel of cetane index 46, in accordance with an embodiment of the present invention
  • Fig. 9 illustrates a graph showing comparison of NOx emissions with diesel, neat heavy fraction biofuel and heavy fraction biofuel-diesel blends are compared at varying loads, with the heavy fraction biofuel of cetane index 46, in accordance with an embodiment of the present invention
  • Fig. 10 illustrates a graph showing comparison of exhaust smoke emissions with diesel, neat heavy fraction biofuel and heavy fraction biofuel-diesel blends at varying loads, with the heavy fraction biofuel of cetane index 46, in accordance with an embodiment of the present invention
  • Fig. 1 1 illustrates a graph showing comparison of unburned hydrocarbon (FIC) emissions between diesel, neat heavy fraction biofuel and heavy fraction biofuel-diesel blends, with the heavy fraction biofuel of cetane index 46, in accordance with an embodiment of the present invention
  • Fig. 12 illustrates a graph showing comparison of Carbon Monoxide (CO) emissions with diesel, neat heavy fraction biofuel, heavy fraction biofuel-diesel blends, with the heavy fraction biofuel of cetane index 46, in accordance with an embodiment of the present invention
  • Fig. 13 illustrates the process of drying of wet stock generated from edible oil refinery in form of waste using the double drum dryer in accordance with an embodiment of the present invention.
  • CO Carbon Monoxide
  • compositions or an element or a group of elements are preceded with the transitional phrase“comprising”, it is understood that we also contemplate the same composition, element or group of elements with transitional phrases“consisting of”, “consisting”, “selected from the group of consisting of,“including”, or“is” preceding the recitation of the composition, element or group of elements and vice versa.
  • a composition for the preparation of a biofuel from edible oil refinery waste and by-products comprises olefins present in a range of, but not limited to,18%-20%, paraffin present in a range of, but not limited to, 63%-70%, aromatic compounds present in a range of, but not limited to, 1 %-1.5%, aqueous phase present in a range of, but not limited to, 0.5%-1 %, others present in a range of, but not limited to, 9.50%-1 1.50% and coke residual oil present in a range of, but not limited to, 8%-10%.
  • the amount of aromatic compound is about 1.05% approximately, and consequently have even lower percentage of Polycyclic Aromatic Hydrocarbon (PAH) in the final biofuel composition, much lower than the 10% limit of Polycyclic Aromatic Hydrocarbon (PAH) allowed in High Speed Diesel (HSD). Since, Polycyclic Aromatic Hydrocarbon (PAH) are suspected carcinogens, such an ultra-low value in this biofuel will make the use of biofuel composition safe and will further mitigate health and environmental risks.
  • the composition possesses fuel efficiency similar to that of diesel oil.
  • the biofuel of present invention can replace diesel either in pure form or in blended form as biofuel-diesel blend.
  • any of the form there is no significant changes in the engine combustion and performance.
  • the exhaust smoke emissions are reduced as from use of High Speed Diesel (HSD).
  • HSD High Speed Diesel
  • the Sulphur content is less than 10 ppm, the SOx emissions are lower than even the ones specified for Bharat IV HSD.
  • FIG 1 illustrates method for the production of biofuel from edible oil refinery waste and by-products, in accordance with an embodiment of the present invention.
  • a plurality of raw materials are provided from edible oil refinery waste and by-products.
  • the edible oil is selected from a group comprising, sunflower oil, rice bran oil, soybean oil, peanut oil, palm oil, mustard oil and other soft oils.
  • the other soft oils are selected from a group comprising, rapeseed oil, sesame oil, safflower oil, canola oil, mustard oil and corn oil.
  • the plurality of raw materials are obtained from edible oil refinery waste, by-products and effluent.
  • the plurality of raw materials are selected from a group comprising, spent clay, soap stock and spent wax and Effluent Treatment Plant (ETP) waste.
  • the spent wax and spent clay inherently has clay that acts as a catalyst. Additionally, some lime at 0.1 % of feed may be added to keep acidity of the final product low. Whereas, soap stock is dried at low moisture level prior to further processing for the production of biofuel. Additionally, an external catalyst like Bentonite or FIZSM - 5 is added in-situ.
  • the step of providing (102) comprising the steps of drying the plurality of raw materials by using a double drum dryer and delivering the dried raw material in the reactor for pyrolysis.
  • the raw material is soap stock.
  • pyrolysis is performed on the plurality of raw materials in a reactor at a bed temperature in the range of 500 Q C - 550 Q C to obtain vapors or a liquid.
  • the step of pyrolysis there are critical features such as presence of the right catalyst and process conditions like feed rate, bed temperature, temperature of cooling water etc.
  • the pyrolysis produces products selected from a group comprising, a high calorific value liquid, a high calorific value gas and a solid by-product.
  • a vapor temperature in the range of 375 Q C - 390 Q C is achieved.
  • the feeding rate is maintained at a ratio of Kgs/hr of feed to volume of the reactor at 0.06 - 0.2.
  • a liquid is recovered from the pyrolysis process before distillation process by having a series of condensers for the pyrolysis vapors and cooling them selectively to obtain the fractions.
  • the obtained liquid may be directly used in boilers, furnaces and other heat generating equipment to replace High Speed Diesel (FISD) or Light Diesel Oil (LDO) as it gives the same heat and energy efficiencies with reduced smoke and particulate emissions.
  • FISD High Speed Diesel
  • LDO Light Diesel Oil
  • step of performing (104) further comprising preforming step wise cooling of the vapors to obtain liquid fractions of different properties or distillation of the obtained liquid from rapid cooling of the vapors to make fractions.
  • the heat energy produced during the step wise cooling of the vapors is used as input energy for the step of providing (102).
  • distillation of the obtained vapors or liquid is performed to obtain fractions.
  • the critical parameters involved in distillation are the initial and final temperatures of the fraction cut taken to form a liquid component. Further, this liquid component may be distilled to obtain a Fligh-Speed Diesel (HSD) like fuel to be used in automobiles.
  • HSD Fligh-Speed Diesel
  • the resulting liquid from pyrolysis may be passed through a straight path distillation up to a temperature of 190 Q C and heavy fractions of temperature between 191 e C and 390 Q C. Further, this liquid component may be distilled to obtain a High-Speed Diesel (HSD) like fuel to be used in automobiles.
  • HSD High-Speed Diesel
  • the high calorific value gas produced during pyrolysis is further recycled in the process to provide heat needed for the process. Additionally, the high calorific value gas produced during pyrolysis may be separated and further used as a biofuel alternative to natural gas or Liquefied petroleum gas (LPG) as it has equivalent calorific values.
  • LPG Liquefied petroleum gas
  • the raw stock as transferred to the soap crutcher (1304) normally has a moisture content in the range of 35% to 45%.
  • the stock is transferred by a transfer pump to a drum dryer, where it continuously accumulates in a pool between two rolls (1312) and (1314).
  • the rolls (1312) and (1314) are driven by a drive so as to move inwardly in the direction of the arrows and are adjusted for clearance so as to permit a thin layer of stock to be deposited on each roll.
  • Room air is introduced by blower (1322) through the line (1324) into the top portion of a cooling header (1326) having ports (1328) in its upper side so as to lift the dried stock sheet from the perforated cooling header surfaces and convey the sheet from the knife blade edge.
  • Refrigerated air is introduced into the bottom section of the cooling header and discharged through the perforations (1330) in the outer side thereof to make the sheet prior to its introduction to the screw conveyor (1332).
  • the air flows from an air cooler (1324). It is also preferred to introduce an added quantity of refrigerated air through the outlets (1334) into the screw conveyors to further cool the stock sheet and to dehumidify its surrounding air.
  • the ground stock may be combined with a conditioning agent from the storage tank (1336), from which it is discharged through feeder (1338), the combination being formed in a paddle mixer (1340). From the mixer (1340), the finished-product goes to a surge bin (1342) and appropriate conveying and packaging equipment for packaging the product for use.
  • a heavy-duty multi cylinder engine was used for the engine test as shown in figure 2.
  • the heavy-duty multi cylinder engine was connected further with an eddy current dynamometer (212) to act as a load absorber and provide a quick load change rate for rapid load settling.
  • the eddy current dynamometer (212) was provided with a water inlet (230) and water outlet (231 ) supported by a thermocouple.
  • the eddy current dynamometer was then connected with a load cell (210) and one dynamometer controller (214). Consequently, the load cell (210) provides the thermocouple signals to the dynamometer controller (214).
  • An air supply (228) provided, which was further configured to attach with the air filter (202), air flow meter (204) and surge tank (206) respectively. From surge tank (206) it was then attached with the heavy-duty multi cylinder engine (208) and controlled by a thermocouple (229). The surge tank (206) is provided to control the sudden rise in the pressure of the liquid flow.
  • One end of the heavy-duty multi cylinder engine (208) was connected with an exhaust (224) that comprises a valve system (226) adapted to dispense the exhaust gases.
  • the exhaust (224) was further connected with an exhaust gas analyzer (222) to measure the combustion rate.
  • the sensitivity of the pressure sensor ranges between! 0.5% over a temperature range of 200 ⁇ 50 °C.
  • HSD High Speed diesel
  • the in-cylinder gas pressure history is a cardiogram of engine combustion analysis from which various combustion parameters are deduced such as heat release rate, peak cylinder pressure, maximum rate of pressure rises and duration of combustion.
  • a comparison of cylinder pressure histories at 20% and 80% load and peak pressures at varying loads between Diesel, B25, B50, B75 and B100 at varying loads are shown in figures 5A, 5B and 5C.
  • the engine performance is evaluated in terms of Brake Specific Fuel Consumption (BSFC), Brake Specific Energy Consumption (BSEC) and brake thermal efficiency.
  • BSFC defined as the total fuel consumed by the engine to produce unit brake power output is evaluated on mass basis and thus, is an indicator of engine fuel economy.
  • the BSEC is evaluated on energy basis, which is defined as the ratio of total energy consumed by the engine to the brake power output.
  • the engine brake thermal efficiency is a measure of ability of the engine to convert fuel chemical energy into brake power output.
  • a comparison of BSFC, BSEC and brake thermal efficiency of the engine with Diesel, B25, B50, B75 and B100 at varying loads is shown in figure 8A, 8B and 8C.
  • the regulated emissions from diesel engine viz. oxides of nitrogen (NOx), smoke, carbon monoxide (CO) and unburned hydrocarbon (FIC) are analyzed to examine the emission reduction potential with the heavy fraction biofuel of the present invention.
  • NOx emissions with Diesel, B25, B50, B75 and B100 are compared at varying loads in figure 9.
  • the exhaust smoke emissions with Diesel, B25, B50, B75 and B100 at varying loads are compared in figure 10.
  • the smoke emissions are relatively more dependent on the extent of fuel-air mixing and the magnitude of heat release rates during the diffusion phase combustion.
  • the smoke emissions with both the fuels remain considerably lower at all the loads except at full load.
  • the lower smoke emissions with all the fuels at part loads could be attributed to turbocharged operation, which increases oxygen availability.
  • the differences in smoke emissions between diesel and heavy fraction biofuel are not significant at part load conditions, however, at higher loads, the smoke emissions are reduced with neat heavy fraction biofuel and heavy fraction biofuel-diesel blends.
  • the lower smoke emissions with heavy fraction biofuel signify its better mixing characteristics as compared to diesel.
  • HC emissions are products of incomplete combustion, which are found to increase with less oxygen availability, crevice flow and flame quenching mechanisms.
  • a higher HC emission signifies lower energy release during combustion and thereby, lowers combustion efficiency.
  • CO emissions with Diesel, B25, B50, B75 and B100 are compared at varying loads in Figure 12.
  • the CO emissions are products of incomplete combustion, which are highly sensitive to changes in fuel-air equivalence ratio.
  • a fuel-rich mixture increases the tendency of CO formation.
  • the oxidation of CO requires higher temperatures and thus the changes in in-cylinder gas temperature influences CO emissions.
  • the combustion duration was taken as the time interval between 10% and 90% of cumulative heat release.
  • B25, B50, B75 and B100 show a delayed start of combustion and somewhat higher peak heat release rate.
  • the occurrence of peak heat release rate is also delayed with B25, B50, B75 and B100 owing to a longer ignition delay compared to diesel due to cetane index of 46 which can be raised and even the small difference nullified.
  • the NOx emissions were found to increase with an increase in cylinder gas temperatures, longer residence time and oxygen availability.
  • the trends of NOx emissions were similar with all the fuels, as shown in figure 9, wherein it increases with an increase in load owing to higher cylinder gas temperatures at higher loads.
  • the changes in NOx emissions between diesel, B25, B50, B75 and B100 were insignificant at lower loads, there was a slight increase in NOx emissions with B25, B50 and B75 at higher loads.
  • These trends were due to the fact that the ignition delay was longer with B25, B50 and B75 leading to more intense premixed combustion, higher cylinder gas temperatures and thereby, higher NOx emissions. This can be nullified by using a Bio fuel of higher cetane index than 46 used for this experiment.
  • the exhaust smoke emissions with diesel, B25, B50, B75 and B100 at varying loads were compared as shown in Fig. 10.
  • the smoke emissions with both the fuels remain considerably lower at all the loads except at full load.
  • the lower smoke emissions with all the fuels at part loads could be attributed to turbocharged operation that increases oxygen availability.
  • the differences in smoke emissions between diesel and heavy fraction biofuel as disclosed in the present invention were not significant at part load conditions, however, at higher loads, the smoke emissions were reduced with B100 and B25 , B50 & B75.
  • the lower smoke emission with heavy fraction biofuel as disclosed in present invention signifies its better mixing characteristics as compared to diesel.
  • CO emissions with diesel, B25, B50, B75 and B100 were compared at varying loads in figure 12. It was observed that the trends of CO emissions with changes in engine load were similar with all the fuels. The CO emissions were higher at lower and higher loads due to lower in-cylinder gas temperatures and locally fuel-rich regions respectively. Although, the differences in CO emissions between diesel and heavy fraction biofuel as disclosed in present invention were not significant at intermediate load conditions, they were higher at lower and higher loads with heavy fraction biofuel.
  • table 3 table 4, table 5, table 6 and table 7 shows the engine combustion, performance and emission data with diesel, B25, B50, B75 and B100.
  • Table 4 An Engine Combustion, Performance and Emission Data with B25
  • Table 5 An Engine Combustion, Performance and Emission Data with B50
  • Table 7 An Engine Combustion, Performance and Emission Data with B100
  • a composition of biofuel from edible oil refinery by-products and wastes has been successfully obtained.
  • the experiment shows that the heavy fraction biofuel can replace diesel with B100 or B25, B50, B75 and that there are no significant changes in the engine combustion and performance, the exhaust smoke emissions were reduced.
  • Bio oil yield was about 67% from Pyrolysis of Spent wax and the char yield was about 15% - 18% with the rest being the high calorific value gas, which could replace natural gas and Liquefied Petroleum Gas (LPG) as it has similar calorific value.
  • Heavy fraction biofuel yield after distillation is over 85% and the fuel properties of obtained, as disclosed in present invention, fraction are exactly in the range required for vehicular diesel.
  • the Char thus obtained is rich in important nutrients like potassium and phosphorous which may be further used as a soil nutrient to improve crop yield and soil quality, as a precursor for extraction of silica or in the making of adsorbents to be used in water purification, removal of heavy metals etc.
  • composition and method as described above could be fabricated in various other ways and could include various other materials, to provide a biofuel.

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Abstract

La présente invention concerne un procédé de production de biocarburant, le procédé comprenant les étapes consistant à fournir une pluralité de matières premières à partir d'une raffinerie d'huile comestible, réaliser une pyrolyse de la pluralité de matières premières dans un réacteur à une température de lit de 500 à 550 °C pour obtenir un liquide et réaliser une distillation du liquide obtenu pour préparer des fractions. En outre, la pyrolyse est effectuée en présence d'un catalyseur. De plus, le sous-produit solide produit est un produit de carbonisation qui a une quantité élevée de nutriments essentiels comme le potassium et le phosphore qui sont essentiels pour les plantes. Le gaz à valeur calorifique élevée produit pendant la pyrolyse est capturé séparément et utilisé en outre comme biocarburant alternatif. FIG 1 :
PCT/IB2019/056245 2018-07-31 2019-07-22 Composition et procédé pour la production de biocarburant à partir de sous-produits et de déchets de raffinerie d'huile comestible WO2020026068A1 (fr)

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