WO2015093991A1 - Un procedimiento industrial continuo para producir combustible biodiesel - Google Patents
Un procedimiento industrial continuo para producir combustible biodiesel Download PDFInfo
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- WO2015093991A1 WO2015093991A1 PCT/PA2013/000003 PA2013000003W WO2015093991A1 WO 2015093991 A1 WO2015093991 A1 WO 2015093991A1 PA 2013000003 W PA2013000003 W PA 2013000003W WO 2015093991 A1 WO2015093991 A1 WO 2015093991A1
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- biodiesel
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- methyl
- triglycerides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
- B01J19/10—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing sonic or ultrasonic vibrations
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/008—Processes for carrying out reactions under cavitation conditions
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- 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
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- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
- C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
- C11C3/003—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fatty acids with alcohols
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- 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
- C10L2270/00—Specifically adapted fuels
- C10L2270/02—Specifically adapted fuels for internal combustion engines
- C10L2270/026—Specifically adapted fuels for internal combustion engines for diesel engines, e.g. automobiles, stationary, marine
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- 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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/24—Mixing, stirring of fuel components
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- 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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/34—Applying ultrasonic energy
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- 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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/543—Distillation, fractionation or rectification for separating fractions, components or impurities during preparation or upgrading of a fuel
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- 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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/547—Filtration for separating fractions, components or impurities during preparation or upgrading of a fuel
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- 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
Definitions
- the present invention relates to a continuous industrial process for obtaining biodiesel fuel.
- Said process for the production of biodiesel from vegetable oils or animal fats essentially comprises three stages, which are the following: Stage 1: the interesterification reaction;
- Stage 2 recovery of excess ethyl acetate (or methyl); Y
- Stage 3 the separation of biodiesel.
- Biodiesel is a type of fuel, of semi-synthetic origin, that is used in pure form or in admixture with diesel fuel (also called diesel or diesel) for the operation of diesel cycle engines.
- Biodiesel decreases carbon dioxide emissions into the atmosphere, the main cause of the greenhouse effect caused by global warming, such as This also reduces sulfur emissions and carcinogenic aromatic components.
- biodiesel is biodegradable, with the advantages that this entails for the environment, and it can be mixed perfectly with diesel oil: it does not ignite or explode easily, because it has a high flash point or ignition temperature.
- Biodiesel is produced from oils and fats, virgin or used, of vegetable and animal origin.
- biodiesel can be obtained from animal fats
- conventional procedures generally refer to the transformation of triglycerides from vegetable oils into the methyl esters of their fatty acids, which constitute biodiesel and are suitable for use as fuels in diesel engines.
- a process which comprises a transesterification stage of very high conversion of triglycerides in the methyl esters of fatty acids under ultrasonic cavitation conditions in a tubular ultrasonic cavitation reactor with 2 to 8 Cavitation series cells.
- the triglycerides present in oils or fats of vegetable and animal origin are constituted by glycerin molecules (1,2,3-propanediol) esterified with saturated and unsaturated fatty acids, predominantly with 16 to 20 carbon atoms.
- Soy, sunflower, rapeseed, palm and even cotton oils are representative of vegetable oils that contain this type of triglycerides.
- the fuel commonly referred to as biodiesel is a diesel engine fuel that is generally prepared from vegetable oils that contain the aforementioned triglycerides.
- diesel fuel produced from fractional distillation of oil, is a fraction of linear and branched hydrocarbons (paraffins and olefins) containing approximately 15 to 25 carbon atoms per molecule.
- the biodiesel fuel is constituted by the methyl (and possibly ethyl) esters of fatty acids containing mainly 16 to 20 carbon atoms.
- the biodiesel fuel is constituted by the methyl (and possibly ethyl) esters of fatty acids containing mainly 16 to 20 carbon atoms.
- industrial chemical processes have been developed to prepare the biodiesel fuel by transforming, by substitution, the triglycerides contained in vegetable oils into the methyl esters of fatty acids.
- This reaction is currently carried out in the presence of sodium or potassium hydroxide, as a catalyst.
- the ultrasound waves are those with a frequency greater than 20,000 Hz, and, therefore, inaudible to humans.
- cavitation The phenomenon of gas bubble formation within a liquid as a result of the formation of a low pressure zone (below the vapor pressure of the liquid) is called cavitation, and when cavitation is the result of application of an ultrasonic wave train, the phenomenon is known as ultrasonic or ultrasonic cavitation.
- the liquid is a mixture of two reagents, such as a triglyceride and methanol, and the catalytic and temperature and pressure conditions are appropriate, then the result of the application of the ultrasound cavitation phenomenon is the chemical reaction between both reagents. a very high reaction rate behavior.
- the known equipment which can be implemented on an industrial scale, basically consists of two tanks containing respectively the oil and the mixture of methanol with the catalyst (sodium or potassium hydroxide).
- Both solutions are fed, in approximately the appropriate stoichiometric molar proportions (1 mole of triglyceride per 3 moles of methanol) to a tubular ultrasonic cavitation reactor, where a pressure of 1 to 3 atm and a temperature of about 66 to 70 ° C reigns.
- the glycerin / biodiesel mixture is pumped to the glycerin separation train, methanol recovery and biodiesel washing and drying.
- European standard EN 14214 represents an international standard that describes the minimum technical requirements of biodiesel.
- Biodiesel, as fuel, is comparable to diesel fuel, which is produced from petroleum, but has the advantage of being a fuel obtainable from a renewable source such as oilseed crops (soybeans, corn, etc. .).
- Pure biodiesel which is known as B100, consists of the fatty acid methyl esters of 14/15 at 24 carbon atoms (palmitic, oleic, linoleic, etc.) from glycerin.
- Biodiesel blends with diesel fuel are designated with a "B” followed by a number that represents the biodiesel content of the mixture.
- B80 is 80% biodiesel in mixture with 20% diesel fuel.
- the EN 14214 standard establishes, among other requirements, that biodiesel must have a minimum content of methyl esters of 96.5% by weight and a combined glycerin content (mono-, di- and triglycerides) of at most 1, 2% in weigh.
- stage of the chemical transesterification reaction is of particular importance in the manufacture of biodiesel fuel since a maximum conversion of triglycerides into biodiesel represents an optimal use of raw materials (oil and methanol), with the consequent decrease in the price of fuel per ton of plant material used, and a significantly lower cost in the following stages of separation of free glycerin, combined glycerin, methanol, catalyst and traces of soaps and other impurities.
- ultrasound cavitation is a known process for the production of biodiesel, significantly improved by the procedure described in WO 2011/070445 A2.
- Catalyst concentration 0.6% by weight of sodium or potassium hydroxide
- Type of cavitation reactor tubular, of an ultrasonic cavitation cell
- WO 2011/070445 A2 describes a process for preparing biodiesel by means of ultrasonic cavitation technology, which allows to obtain a triglyceride conversion greater than 99.0% by weight in the transesterification stage preferably between 99.90% and 99.95%.
- This conversion value of triglycerides into biodiesel is achieved by allowing the chemical reaction initiated in the reactor Cavitation end in a stirred tank reactor disposed downstream of the cavitation reactor.
- Reaction temperature in both reactors 45 to 60 ° C; preferably
- Pressure in the cavitation reactor 1.5-2 MPa (15 to 20 atm); preferably 6.6 atm (250 psi);
- Catalyst concentration 0.7 to 1% by weight of sodium or potassium hydroxide; preferably 0.95% sodium hydroxide;
- Residence time in the cavitation reactor 15 to 30 seconds
- Concentration of triglycerides from the triglyceride source greater than 99.0% by weight
- Type of cavitation reactor tubular, with 2 to 8 cells in series of ultrasonic cavitation.
- an energy is generated that causes vapor bubbles to form and collapse.
- the pressure reaches 40,000 psi and the temperature reaches 10,000 ° C, because the phenomenon occurs at the molecular level, since the outside temperature is only 3 to 5 degrees above the product inlet temperature and pressure It practically does not vary.
- the decrease in the reaction temperature below the usual 65 to 70 ° C, at values between 45 and 60 ° C, and preferably around 50 ° C, together with the increase in pressure at he Cavitation reactor from conventional 1 to 3 atm to values between 15 and 20 atm, added to the use of a multi-cell ultrasonic cavitation tubular reactor arranged in series, to obtain such high results in the conversion of triglycerides (for over 99.0% by weight) in biodiesel are really surprising and unexpected results that do not find an easy explanation or technical justification.
- glycerin or glycerol
- glycerol is inappropriate as a fuel while its heat of combustion is low and its viscosity is several orders of magnitude higher than that of triglycerides of origin.
- the process as will be described below comprises a succession of stages that conclude in obtaining biodiesel and, separately, a biofuel formed by low molecular weight glycerides.
- vegetable oils or animal fats are heated to a predetermined temperature and mixed, at the inlet of the reaction system, with ethyl acetate, methyl acetate, or a mixture of both esters (other methyl esters can be used and ethyl with up to 6 carbon atoms), using sodium methylate (sodium methoxide) as catalyst.
- sodium methylate is very hygroscopic and insoluble in ethyl acetate or in vegetable oils or animal fats
- a pre-mixture in ethyl acetate is carried out in a small reactor capable of continuously feeding the catalyst to the main reactor.
- Strong bases such as metallic sodium, sodium or potassium hydroxides, sodium or potassium ethoxides, potassium methoxide, sodamide (or sodium amide) and triphenylmethyl sodium can also be used as catalysts.
- the interesterification reaction is initially carried out inside ultrasonic caviters, according to the known technique, and the reaction product is then fed to two reactors of the tank type with stirring, arranged in series.
- Reagents ie triglycerides and low molecular weight esters, in conjunction with the catalyst, are brought into contact under controlled conditions of temperature, composition and pressure in order to optimize the desired conversion.
- the temperature for the interesterification reaction is between 20 and 120 ° C and the reaction time can vary between 5 and 90 minutes.
- the molecules of vegetable oils or animal fats have been completely converted into biodiesel, that is to say the ethyl esters of fatty acids (also known as FAEE, fatty acid ethyl esters) and low molecular weight triglycerides.
- composition of the reaction product at this point in the process is FAEE, low molecular weight triglycerides, excess ethyl acetate and solid sodium methylate in suspension.
- the reaction product is filtered, for example by a rotary filter.
- the amount of catalyst recovered is continuously recycled to the reactor to make the premix with ethyl acetate and then introduced into the reaction system.
- the product of the filtered reaction, and with the residual content of sodium methylate that was not recovered by the first filter, is neutralized with formic acid inside another reactor tank with continuous stirring.
- a second filtration is carried out, obtaining two phases: (a) a solid phase of sodium formate retained by the filter and which has application in the food industry; and (b) and a clear and homogeneous solution of ethyl acetate, FAEE and low molecular weight triglycerides.
- the clear and homogeneous solution from the second filtration is preheated by heat exchange with the solution hot obtained at the end of the evaporation steps. In this way, energy consumption is optimized.
- the clear and homogeneous reactive medium solution is heated to a predetermined temperature for the start of evaporation in multiple stages.
- the first two evaporation stages are carried out in two heat exchange tubes with an expander tank arranged on the top.
- the steam produced in the first stage is used in the second stage.
- the second stage is carried out under vacuum conditions.
- the vaporized ethyl acetate is then condensed and sent to a storage tank to be recycled to the process.
- the resulting solution still has a low ethyl acetate content that is removed by evaporation by flash distillation in a tank.
- the resulting hot solution is sent to the next stage of the process.
- the biodiesel separation stage The solution from the previous stage is composed of ethyl esters of fatty acids (FAEE or biodiesel) and low molecular weight triglycerides, also referred to, in this representative case, as acetate glycerides.
- Acetate glycerides may be present as mono-, di- or tri-ethyl glycerides.
- the operating conditions can be adjusted to define the composition between these three types of substances.
- the content of tri-ethyl-glycerides is more ' , the greater is the conversion FAEE.
- the hot biodiesel produced is then used to exchange heat in the evaporation stages mentioned above and, finally, is cooled and stored at room temperature.
- the biodiesel obtained by the process of the present invention can be considered as a "premium” biodiesel because of its very low impurity content.
- the ethyl glycerides obtained in this The procedure can be used as an industrial fuel, because it has similar physical-chemical characteristics.
- biodiesel preparation procedure ends in a fuel already approved and defined by international quality specifications and does not require long and expensive approval processes for mass use.
- patent EP 2 113 019 B1 describes the obtaining of a fuel with characteristics similar to diesel, but chemically different from hydrocarbons or biodiesel, which will require a homologation process for its possible use in vehicles.
- the technology that involves the process of the present invention stands out for not producing glycerin as a byproduct, thus avoiding the problems arising from its excess supply.
- the by-products of the process of the present invention are ethyl glycerides that have a low molecular weight and have a much lower viscosity than animal oils and fats, and can thus be easily adapted as industrial fuels for heat and energy generation.
- this technology proposes a pre-mixture of catalyst with ethyl acetate, allowing continuous feed to the reactors and avoiding a batch reaction and its inherent operational difficulties.
- this technology proposes the novel use of an ultrasonic cavitator as the first reactor in an intersterification reaction system, thus overcoming the problems of matter transfer between the reagents (triglycerides and ethyl acetate) and the catalyst.
- This technology reduces the reaction time to at least half, achieving the final results after approximately 30 minutes.
- the industrial advantages of the application of the process of the present invention lie in the use of smaller reactors, less investment, shorter production times, smaller volumes of raw materials and reagents during the process and lower working capital.
- this technology Compared to EP 2 113 019 B1, this technology describes a filtration step before neutralization of the catalyst, in order to recover and recycle this material, reducing the consumption of catalyst and of about 30% to 50%. formic acid and, therefore, reducing operational costs.
- this technology proposes a system for the recovery of excess ethyl acetate in several stages, interspersed with heat regeneration processes, which reduces the use of thermal energy by 30% and its associated operating costs.
- this technology proposes a distillation separation between biodiesel (FAEE) and ethyl glycerides, which allows the production of two high demand products: biodiesel and an industrial fuel of plant origin and / or animal.
- FEE biodiesel
- ethyl glycerides ethyl glycerides
- biodiesel output flow is 3,125 kg / hr to total a nominal production capacity of 25,000 tons per year of biodiesel.
- the average yields (oil - biodiesel) rose to 103.5% by weight, that is, for every 100 tons of oil or grease, an average of 03.5 tons of biodiesel is produced.
- 121 kg / h of ethyl acetate are introduced into the 2R1A reactor where 30 kg / hour of solid sodium methoxide (purity> 99% by weight) is added.
- This premix allows continuous dosing of the solid sodium methylate catalyst in the esterification reaction system.
- the 151 kg / h mixture is added to the raw material at the inlet of the first ultrasonic cavitation reactor.
- the first stage of the reaction occurs in an ultrasonic cavitator in order to overcome the problems of mass transfer between the reagents and the catalyst.
- the results show a 50% saving in reaction time.
- the reaction medium is pumped to the first reactor, 2R2A, of agitated tank type, for the continuity of the reaction. Its feeding is done by the bottom.
- the second stirred tank reactor, 2R2B is received, which receives the transfer reaction medium from the first.
- the residence time for achieving the appropriate conversion was 40 minutes.
- the reactive medium consists of a heterogeneous mixture due to the solid sodium methylate in suspension.
- this reactive medium is subjected to a first filtration step in a continuous vacuum filter, 2F1.
- the recovered solid is transferred and directed to the 2R1 B reactor, where it is fluidized with approximately 120kg / hr of ethyl acetate for reuse in the reaction system. This operation allowed reducing catalyst consumption by at least 30%.
- the filtered solution has an almost homogeneous appearance, but still contains traces of soluble and insoluble catalyst. Then, in the line of this filtered solution, 14 kg / h of formic acid are added in a controlled manner, lowering the pH of the solution to a value between 6.5 and 7.5.
- the neutralization reaction takes place continuously inside the stirred tank reactor 2R3, at a temperature of approximately 45 ° C, which is achieved spontaneously due to the exothermic nature of the neutralization reaction.
- the reaction between formic acid and sodium methylate produces sodium formate, an insoluble salt that is removed from the solution in a second continuous filtration stage, 2F2.
- the separated solid is recovered, transferred and bagged for later commercialization.
- the solution filtered in the 2F2 filter is a solution of yellowish color and absolutely homogeneous appearance and has a continuous flow of 6,045 kg / h. Its approximate composition is 52% ethyl esters of fatty acids; 35% excess ethyl acetate and 13% ethyl glycerides (percentages are given by weight).
- ethyl acetate is added to the set of reactors with a stoichiometric excess in order to promote greater reaction conversion.
- the solution at the end of the inter-esterification system has approximately 35% ethyl acetate, which is not part of the composition of the final product and must, therefore, be recovered and for reuse in order to save unnecessary costs.
- This recovery operation occurs by evaporation in 3 stages.
- the solution from the second filtration is preheated by thermal exchange with the final distilled biodiesel, in the plate-type heat exchanger, 2X2.
- This exchanger works as a heat regenerator and therefore avoids fuel consumption in boilers.
- the temperature of the solution is approximately 50 ° C, and at the outlet, 90 ° C.
- the hot solution is fed to the first evaporator, which consists of a heat exchanger of the vertical layer-tube type, 2X3, vertical, which is heated with thermal oil and which has an expanding head at the top, 2T3.
- This evaporator operates at atmospheric pressure, at a temperature of 110 ° C, and recovers approximately half of the excess ethyl acetate present in the solution.
- the condensed ethyl acetate in the 2X4 hull is sent to the 2T2 - B tank.
- the expanded vapors in the second evaporation stage, 2T4 are condensed in the 2X5A and 2X5B exchangers, which operate in series, using cold water as a refrigerant.
- vacuum is applied in order to form a vacuum gradient between 2T3 and 2T4. This allows 2T3 vapors to be obtained without the 2X4 heating fluid and without the need to use heat exchange.
- the vacuum applied in 2Q4 is 0.8 bar, at a temperature of 110
- the 2T4 solution at the exit has an acetate content of less than 2%, but enough to damage the flash point necessary for the final products.
- the solution from the flash process has a temperature of approximately 110 ° C and consists essentially of a homogeneous mixture of ethyl esters of fatty acids and mono-, di- and tri-ethylglycerides (low molecular weight triglycerides).
- the next stage of the process is the separation of ethyl esters from triglyceride fatty acids.
- the system consists of four distillation columns, the first two being installed in parallel, 3C1A and 3C1 B, the second, 3C2, in series with the first set and the third, 3C3, in series with 3C2.
- This configuration is justified by the high content, around 80% by weight, of the lightest phase constituted by the ethyl esters.
- the light phases of the four columns are collected in parallel in the 3T1 tank. From there they are sent to the storage tank at a flow rate of 3,125 kg / h.
- the biodiesel is cooled in the plate type exchanger, 2X2, by the solution that enters the recovery system of excess ethyl acetate, as previously mentioned, and then cooled with cold water in a battery of heat exchangers, 2X7A, 2X7B, 2X7C and 2X7D, up to a temperature of 40 ° C.
- the heavy phase consisting of low molecular weight triglycerides, is serially distilled in the columns, as previously described, collecting at the end of the last column, 3C3, in the 3T2 tank and then sent to the final storage tank at a flow rate of 780 kg / hour.
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PCT/PA2013/000003 WO2015093991A1 (es) | 2013-12-16 | 2013-12-16 | Un procedimiento industrial continuo para producir combustible biodiesel |
ARP140102465A AR096787A1 (es) | 2013-12-16 | 2014-07-01 | Un procedimiento industrial continuo para producir combustible biodiesel |
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PCT/PA2013/000003 WO2015093991A1 (es) | 2013-12-16 | 2013-12-16 | Un procedimiento industrial continuo para producir combustible biodiesel |
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Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
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EP3674384A1 (en) | 2018-12-28 | 2020-07-01 | Rigas Tehniska Universitate | Biodiesel fuel and method for production thereof |
CN112744883A (zh) * | 2020-11-30 | 2021-05-04 | 安徽金禾实业股份有限公司 | 一种三氯蔗糖生产中废水再利用的方法 |
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WO2011070445A2 (es) * | 2009-12-09 | 2011-06-16 | Blasco Garcia Alfredo Carlos | Un procedimiento continuo para producir combustible biodiesel |
ES2433072T3 (es) * | 2007-02-06 | 2013-12-09 | János Thész | Uso de fueles o aditivos de fuel basados en triglicéridos de estructura modificada |
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Non-Patent Citations (1)
Title |
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MADDIKERI, G. L. ET AL.: "Ultrasound assisted interesterification of waste cooking oil and methyl acetate for biodiesel and triacetin production ''.", FUEL PROCESSING TECHNOLOGY, vol. 116, 7 August 2013 (2013-08-07), pages 241 - 249, Retrieved from the Internet <URL:http://www.sciencedirect.com/science/article/pii/S037838201300235X> [retrieved on 20140819] * |
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EP3674384A1 (en) | 2018-12-28 | 2020-07-01 | Rigas Tehniska Universitate | Biodiesel fuel and method for production thereof |
CN112744883A (zh) * | 2020-11-30 | 2021-05-04 | 安徽金禾实业股份有限公司 | 一种三氯蔗糖生产中废水再利用的方法 |
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