Method and system for extracting and purifying algae oil for low-temperature biofuel production

Abstract

The present invention provides a novel method and system for extracting and purifying algae oil from wet algae slurry or liquid algae, for producing high-performance biofuels suitable for cold-climate applications. The method involves a multi-step process, with the stabilization of algae slurry or liquid algae at controlled flow rates and temperatures between 40°C and 70°C in a stabilization tank. The slurry is then subjected to interference wave extraction using piezoelectric devices operating at frequencies between 11 MHz and 26 MHz, enhancing cavitation energy and causing vaporization of the algae oil mixture. The vaporized mixture is passed through an ion exchange system to remove heavy metals, improving the purity of the extracted oil. A multi-stage condensation process is employed to separate heavy and light fractions of crude algae oil, with a final step involving the restructuring of oil molecules using a magnetic field. The vaporized algae oil is esterified in alcohol to produce a biofuel ester with a pour point below -10°C, suitable for use in aviation, automotive, and other low-temperature applications.

Description

[0001] METHOD AND SYSTEM FOR EXTRACTING AND PURIFYING ALGAE OIL FOR LOW-TEMPERATURE BIOFUEL PRODUCTION

[0002] FIELD OF INVENTION

[0003] The present invention relates to a method and system for extracting oil from algae, particularly focusing on extracting algae oil from wet algae slurry or liquid algae, with temperature control, interference wave extraction, micro cavitation enhancement, ion exchange purification, multi-stage condensation, and magnetic field processing, to efficiently extract algae oil with improved yield and purity.

[0004] BACKGROUND OF THE INVENTION

[0005] The growing global energy demand, coupled with the rapid depletion of fossil fuel reserves and their environmental consequences, has driven the search for sustainable and renewable energy sources. Algal oil has emerged as a promising feedstock for biodiesel production, offering numerous advantages over traditional biofuel sources. Unlike crop-based biofuels, algae do not compete with food production and can thrive in diverse environments, including non-arable land and wastewater. Thus, the extraction of algae oil has gained significant attention due to its potential as a renewable source of biofuel.

[0006] Algal oil is characterized by high lipid content, rapid growth rates, and the ability to sequester carbon dioxide, making it a sustainable and environmentally friendly option. Life-cycle analyses of algal biodiesel have shown significant potential to reduce greenhouse gas emissions and reliance on non-renewable energy resources. Furthermore, algal oil-derived biodiesel is compatible with existing diesel engines and infrastructure, supporting its integration into current energy systems. Given its versatility, renewability, and environmental benefits, algal oil represents a critical component in the transition toward a sustainable energy future. However, the extraction of algal oil using conventional techniques faces several significant challenges that hinder its commercial viability. Traditional methods, such as solvent extraction, mechanical pressing, and enzymatic treatment, often involve high energy consumption, extended processing times, and the use of hazardous chemicals. Solvent-based extraction, though effective in isolating lipids, raises environmental and safety concerns dueto the toxicity and volatility of organic solvents like hexane. Mechanical pressing yields limited oil recovery, particularly for microalgae with rigid cell walls, necessitating additional pre-treatment steps that further increase costs. Enzymatic extraction offers a greener alternative but remains cost-prohibitive due to the high expense of enzymes and their limited reusability. Moreover, many of these methods require drying the algae biomass prior to oil extraction, a step that consumes significant energy and reduces overall efficiency. Thus, traditional algae oil extraction methods suffer from inefficiencies, low yields, and poor purity, especially when working with wet algae slurry. There is a need for a more efficient and scalable technology to extract algae oil, which maintains high quality and purity, and is adaptable to industrial-scale operations.

[0007] Certain alternative approaches from that of the conventional method to obtain algal oil have been used such as in US20100151540A1 which discloses a method for processing an algae medium containing algae microorganisms to produce algal oil and by-products, comprising the steps of: pumping the algae medium through a flowpath in a multi-stage, flow-through, hydrodynamics cavitation device; generating localized zones of reduced fluid pressure in the algae medium as it is pumped through the flowpath; creating cavitational features in the localized zones of reduced fluid pressure in the algae medium; collapsing the cavitational features to expose components of the algae medium in the cavitational features and the surrounding fluid to sudden, localized increases in temperature and pressure; and disintegrating cell walls of and intracellular organelles in the algae microorganisms in the algae medium to produce algal oil and by-products. However, the process only pertains to disruption of various algal microorganisms and does not provide a multi-step extraction method that maximize the recovery and purity of oil from algae.

[0008] Further, US 8329449 B2 discloses use of immobilized anion exchange and lipid binding resins, as the algae flows past the resin, triglycerides adhere while the bulk of the algae flows through. The lipids, useful for generating biofuels are then are eluted off the resin. However, the said application relies solely on immobilized resins for triglyceride extraction, lacking the multi-stage processing that enhances oil quality and yield in the instant application. Moreover, the process does not improve the purity and allow the separation of heavy and light fractions of algal oil.Thus, there is a requirement for a method and system that maximizes the recovery and purity of oil from algae. In view of the deficiency in the art, the present invention provides a method and system for extracting oil from algae, particularly focusing on extracting algae oil from wet algae slurry or liquid algae, with temperature control, interference wave extraction, micro cavitation enhancement, ion exchange purification, multi-stage condensation, and magnetic field processing, to efficiently extract algae oil with improved yield and purity.

[0009] SUMMARY OF THE INVENTION

[0010] As will be realized in the following description, the invention is capable of other and different embodiments and its several details are capable of modifications in various respects, all without departing from the scope of the present invention. This summary is provided to introduce a selection of concepts in a simplified form that are further described below in the Detailed Description. This summary is not intended to identify key features or essential features of the claimed subject matter, nor is it intended to be used as an aid in determining the scope of the claimed subject matter.

[0011] In an aspect, the present invention provides a method for extracting algae oil from wet algae slurry or liquid algae, comprising the steps of:

[0012] (i) providing a stabilization tank (100) configured to stabilize input conditions by controlling the flow and temperature of an algae slurry or liquid algae within the range of 40°C to 70°C and subjecting the algae slurry or liquid algae in the stabilization tank;

[0013] (ii) subjecting the algae slurry or liquid algae of step (i) to interference wave extraction interference (200) using piezoelectric devices operating at frequencies between 11 MHz and 26 MHz to enhance cavitation energy causing the mixture to vaporize;

[0014] (iii) passing the vaporized mixture of step (ii) through an ion exchange system (300) to isolate the heavy metals from vapor to improve the purity of the extracted oil; wherein the ion exchange system further comprises:

[0015] i) copper plates arranged as the first layer, positively charged at 10-30 amps;

[0016] ii) carbon rods as the second layer, negatively charged at 10-30 amps;

[0017] iii)copper plates as the third layer, grounded to zero voltage;

[0018] (iv) condensing the vaporized mixture in a multi-stage condensation process to obtain separated heavy and light fractions of crude algae oil;

[0019] wherein the multi-stage condensation process comprises:i) a first stage condensation (400) wherein the vaporized mixture is condensed at a temperature between 1°C and 6°C to separate a heavy fraction crude algae oil with a pour point of 0°C; and

[0020] ii) a second stage condensation (500) wherein the remaining vapor is condensed at a temperature between -5 °C and 0°C to separate a light fraction crude algae oil with a pour point of -5°C;

[0021] (v) processing the remaining vaporized components through a magnetic field to restructure the oil molecules;

[0022] (vi) esterifying the oil vapor in alcohol to produce a high-performance biofuel ester with a pour point below -10°C.

[0023] In another aspect, the present invention provides a high-performance biofuel ester is produced by the process above, wherein the biofuel ester is obtained in step (vi) after the oil vapor is esterified in alcohol, resulting in a biofuel ester with a pour point below -10°C, making it suitable for use in cold-climate applications such as aviation and automotive fuels.

[0024] In yet another aspect, the present invention provides a heavy fraction crude algae oil produced by the process above, wherein the heavy fraction crude algae oil is obtained in step (iv)(i) of the process, after the vaporized mixture is condensed at a temperature between 1°C and 6°C, resulting in a heavy fraction crude algae oil with a pour point of 0°C.

[0025] In yet another aspect, the present invention provides a light fraction crude algae oil produced by the process above, wherein the light fraction crude algae oil is obtained in step (iv)(ii) of the process, after the remaining vapor is condensed at a temperature between -5°C and 0°C, resulting in a light fraction crude algae oil with a pour point of -5 °C.

[0026] In yet another aspect, the present invention provides a biofuel composition comprising the biofuel ester obtained by the process above wherein the biofuel ester is suitable for use in aviation or automotive engines under low-temperature conditions.

[0027] In yet another aspect, the present invention provides a purified algae oil composition produced by the process above, wherein the purified algae oil is obtained in step (iii) after the algae slurry or liquid algae is subjected to the ion exchange system, resulting in a purified algae oil composition with reduced heavy metal contaminants.

[0028] In yet another aspect, the present invention provides a crude algae oil composition produced by the process above, comprising a mixture of heavy and light fractions of crude algae oil,wherein the heavy fraction is obtained in step (iv)(i) with a pour point of 0°C, and the light fraction is obtained in step (iv)(ii) with a pour point of -5°C.

[0029] In another aspect, the present invention provides a system for extracting algae oil from algae slurry or liquid algae, comprising:

[0030] i) a stabilization tank (100) for controlling flow rate and temperature of the algae slurry, maintaining temperatures between 40°C to 70°C;

[0031] ii) an interference wave extractor (200) comprising piezoelectric devices operating in the frequency range of 11 MHz to 26 MHz to generate interference waves that enhance cavitation energy and cause vaporization of the algae oil mixture.

[0032] iii) an ion exchanger system (300) comprising at least three layers for purifying the vaporized mixture, including:

[0033] i) Copper plates arranged as the first layer, positively charged at 10-30 amps;

[0034] ii) Carbon rods arranged as the second layer, negatively charged at 10-30 amps; and iii) Copper plates arranged as the third layer, grounded to zero voltage,

[0035] iv) condensation system comprising at least two stages of cooling to condense the vaporized mixture, with the first stage condensation (400) cools to 1-6°C and the second stage condensation (500) cools to -5 to 0°C, wherein the condensation process has limitations in separating fine volatile components and residual impurities;

[0036] iv) a magnetic field processing unit (600) for applying Lorentz and Faraday principles to restructure oil molecules.

[0037] v) a vacuum esterification unit (700) for infusing the vaporized algae oil into alcohol to produce a biofuel ester with a pour point below -10°C.

[0038] BRIEF DESCRIPTION OF DRAWINGS

[0039] Figure 1 illustrates the overview of the system of the present invention.

[0040] Figure 1 A illustrates the block diagram of the present system.

[0041] Figure 2 illustrates the temperature control over time within the stabilization tank.

[0042] Figure 3 illustrates the graph on the cavitation energy vs. frequency of interference waves.

[0043] Figure 4 illustrates the ion exchange system (200) of the present invention.Figure 5 illustrates a photographic image of the copper plate removing the heavy metal.

[0044] Figure 6 illustrates the effectiveness of the ion exchange system in reducing heavy metal concentrations.

[0045] Figure 7 illustrates the flowchart detailing the two-stage condensation process.

[0046] Figure 8 illustrates the system for restructuring of oil molecules to finally to produce biofuel.

[0047] Figure 9 illustrates the magnetic field strength vs. restructuring efficiency.

[0048] Figure 9A illustrates the effect of magnetic field strength on molecular weight distribution.

[0049] Figure 9B illustrates the speed of fatty acid calculated from time of flight.

[0050] Figure 10 illustrates the comparison of pour points of the algal oil.

[0051] Figure 11 illustrates the relationship between esterification temperature and biofuel ester yield.

[0052] Figure 12 illustrates the relationship between alcohol-to-oil ratio and biofuel ester yield.

[0053] Figure 13 illustrates proportions of heavy and light fractions of crude algae oil before and after the multi-stage condensation process, alongside the pour points.

[0054] Figure 14 illustrates the relation between the pour point and esterification temperature.

[0055] Figure 15 illustrates the relation between the pour point and Alcohol-to-Oil Ratio.

[0056] Figure 16 illustrates the engine efficiency using the biofuel ester of the present invention.

[0057] Figure 17 illustrates the engine emission using the biofuel ester of the present invention.

[0058] REFERRENCE NUMERALS

[0059] 100 Stabilization Tank;

[0060] 200 Interference Extractor;

[0061] 300 Ion Exchanger System

[0062] 301 Copperplate

[0063] 302 Carbon rod303 Section A

[0064] 304 Section B

[0065] 400 First Condensation Stage

[0066] 500 Second Condensation Stage

[0067] 600 Electromagnetic Chamber

[0068] 601 Magnetron

[0069] 602 Chamber with alcohol

[0070] 603 Vacuum

[0071] 700 Vacuum System or a vacuum esterification unit

[0072] DETAIL DESCRIPTION OF THE INVENTION

[0073] Those skilled in the art will be aware that the present disclosure is subject to variations and modifications other than those specifically described. It is to be understood that the present disclosure includes all such variations and modifications. The disclosure also includes all such steps, features, compositions, and compounds referred to or indicated in this specification, individually or collectively, and any and all combinations of any or more of such steps or features.

[0074] For convenience, before further description of the present disclosure, certain terms employed in the specification, and examples are delineated here. These definitions should be read in the light of the remainder of the disclosure and understood as by a person of skill in the art. The terms used herein have the meanings recognized and known to those of skill in the art, however, for convenience and completeness, particular terms and their meanings are set forth below.

[0075] Definitions

[0076] For convenience, before further description of the present disclosure, certain terms employed in the specification, and examples are delineated here. These definitions should be read in the light of the remainder of the disclosure and understood as by a person of skill in the art. The terms used herein have the meanings recognized and known to those of skill in the art, however, for convenience and completeness, particular terms and their meanings are set forth below.The articles “a”, “an” and “the” are used to refer to one or to more than one (i.e., to at least one) of the grammatical object of the article.

[0077] The terms “comprise” and “comprising” are used in the inclusive, open sense, meaning that additional elements may be included. It is not intended to be construed as “consists of only”.

[0078] Throughout this specification, unless the context requires otherwise the word “comprise”, and variations such as “comprises” and “comprising”, will be understood to imply the inclusion of a stated element or step or group of element or steps but not the exclusion of any other element or step or group of element or steps.

[0079] The term “including” is used to mean “including but not limited to”. “Including” and “including but not limited to” are used interchangeably.

[0080] In an aspect, the present invention provides a method for extracting algae oil from wet algae slurry or liquid algae, comprising the steps of:

[0081] (i) providing a stabilization tank (100) configured to stabilize input conditions by controlling the flow and temperature of an algae slurry or liquid algae within the range of 40°C to 70°C and subjecting the algae slurry or liquid algae in the stabilization tank;

[0082] (ii) subjecting the algae slurry or liquid algae of step (i) to interference wave extraction interference (200) using piezoelectric devices operating at frequencies between 11 MHz and 26 MHz to enhance cavitation energy causing the mixture to vaporize;

[0083] (iii) passing the vaporized mixture of step (ii) through an ion exchange system (300) to isolate the heavy metals from vapor to improve the purity of the extracted oil; wherein the ion exchange system further comprises:

[0084] i) copper plates arranged as the first layer, positively charged at 10-30 amps;

[0085] ii) carbon rods as the second layer, negatively charged at 10-30 amps;

[0086] iii)copper plates as the third layer, grounded to zero voltage;

[0087] iv) condensing the vaporized mixture in a multi-stage condensation process to obtain separated heavy and light fractions of crude algae oil; wherein the multi-stage condensation process comprises:

[0088] i) a first stage condensation (400) wherein the vaporized mixture is condensed at a temperature between 1°C and 6°C to separate a heavy fraction crude algae oil with a pour point of 0°C; andii) a second stage condensation (500) wherein the remaining vapor is condensed at a temperature between -5 °C and 0°C to separate a light fraction crude algae oil with a pour point of -5°C;

[0089] v) processing the remaining vaporized components through a magnetic field to restructure the oil molecules;

[0090] vi) esterifying the oil vapor in alcohol to produce a high-performance biofuel ester with a pour point below -10°C.

[0091] In an embodiment, the stabilization tank (100) has an adjustable flow rate between 0.01 L / s and 5 L / s.

[0092] In an embodiment, the interference wave extraction is achieved by piezoelectric devices operating at 10 to 120 watts per second.

[0093] In an embodiment, esterification is carried out by drawing the vapour by a vacuum system (700) and infusing into liquid alcohol.

[0094] In an embodiment, the magnetic field processes the vaporized components by applying Lorentz and Faraday principles to trigger molecular restructuring, thereby enabling the release of oxygen and merging of hydrogen with other molecules.

[0095] In an embodiment, the esterification step produces a biofuel with a pour point below -10°C, suitable for use in aviation and automotive fuel applications.

[0096] In an embodiment, the algae oil produced is suitable for use as biofuel, lubricants, and other industrial applications requiring renewable and low-temperature resilient oils.

[0097] In another aspect, the present invention provides a high-performance biofuel ester is produced by the process above, wherein the biofuel ester is obtained in step (vi) after the oil vapor is esterified in alcohol, resulting in a biofuel ester with a pour point below -10°C, making it suitable for use in cold-climate applications such as aviation and automotive fuels.

[0098] In another aspect, the present invention provides a heavy fraction crude algae oil produced by the process above, wherein the heavy fraction crude algae oil is obtained in step (iv)(i) of the process, after the vaporized mixture is condensed at a temperature between 1°C and 6°C, resulting in a heavy fraction crude algae oil with a pour point of 0°C.

[0099] In another aspect, the present invention provides a light fraction crude algae oil produced by the process above, wherein the light fraction crude algae oil is obtained in step (iv)(ii) of theprocess, after the remaining vapor is condensed at a temperature between -5°C and 0°C, resulting in a light fraction crude algae oil with a pour point of -5 °C.

[0100] In another aspect, the present invention provides a biofuel composition comprising the biofuel ester obtained by the process above wherein the biofuel ester is suitable for use in aviation or automotive engines under low-temperature conditions.

[0101] In another aspect, the present invention provides a purified algae oil composition produced by the process above, wherein the purified algae oil is obtained in step (iii) after the algae slurry or liquid algae is subjected to the ion exchange system, resulting in a purified algae oil composition with reduced heavy metal contaminants.

[0102] In another aspect, the present invention provides a crude algae oil composition produced by the process above, comprising a mixture of heavy and light fractions of crude algae oil, wherein the heavy fraction is obtained in step (iv)(i) with a pour point of 0°C, and the light fraction is obtained in step (iv)(ii) with a pour point of -5°C.

[0103] In another aspect, the present invention provides a system for extracting algae oil from algae slurry or liquid algae, comprising:

[0104] i) a stabilization tank (100) for controlling flow rate and temperature of the algae slurry, maintaining temperatures between 40°C to 70°C;

[0105] ii) an interference wave extractor (200) comprising piezoelectric devices operating in the frequency range of 11 MHz to 26 MHz to generate interference waves that enhance cavitation energy and cause vaporization of the algae oil mixture.

[0106] iii) an ion exchanger system (300) comprising at least three layers for purifying the vaporized mixture, including:

[0107] i) Copper plates arranged as the first layer, positively charged at 10-30 amps;

[0108] ii) Carbon rods arranged as the second layer, negatively charged at 10-30 amps; and iii) Copper plates arranged as the third layer, grounded to zero voltage,

[0109] iv) condensation system comprising at least two stages of cooling to condense the vaporized mixture, with the first stage condensation (400) cools to 1-6°C and the second stage condensation (500) cools to -5 to 0°C, wherein the condensation process has limitations in separating fine volatile components and residual impurities;

[0110] v) a magnetic field processing unit (600) for applying Lorentz and Faraday principles to restructure oil molecules.vi) a vacuum esterification unit (700) for infusing the vaporized algae oil into alcohol to produce a biofuel ester with a pour point below -10°C.

[0111] the stabilization tank (100) has an adjustable flow rate between 0.01 L / s and 5 L / s.

[0112] In an embodiment, the esterification unit uses methanol or ethanol as the alcohol for esterification.

[0113] In an embodiment, the biofuel ester produced in the esterification unit has a pour point of below -10°C, making it suitable for use in aviation and automotive fuel applications.

[0114] In an embodiment, the condensation stages are configured to separate the heavy fraction crude algae oil with a pour point of 0°C and the light fraction crude algae oil with a pour point of -5°C.

[0115] WORKING EXAMPLES

[0116] Example 1: Method / System for Extracting Algae Oil from Wet Algae Slurry or Liquid Algae

[0117] The present invention provides a method for extracting and purifying algae oil from wet algae slurry or liquid algae through a multi-step phase-shifting extraction process. The method integrates key technologies such as temperature control, interference wave extraction, microcavitation enhancement, ion exchange purification, and multi-stage condensation to efficiently obtain algae oil of high purity.

[0118] Designed to overcome challenges such as heavy metal contamination and achieving low pour points, the invention not only extracts crude algae oil but also converts it into biofuels suitable for aviation and automotive applications. The process involves critical steps, including stabilizing the algae slurry, enhancing oil release via interference wave technology, isolating contaminants using a specialized ion exchange system, and utilizing multi-stage condensation to produce distinct heavy and light fractions of crude algae oil.

[0119] The obtained fractions are subsequently processed through esterification to produce a high-performance biofuel ester with a low pour point, making it ideal for cold-temperature applications. Additionally, the invention encompasses a system specifically configured to execute these processes, ensuring optimal efficiency and scalability for industrial use. The system as represented in Figure 1 comprises:1. Stabilization Tank (100)

[0120] 2. Interference Extractor (200)

[0121] 3. Ion Exchanger System (300)

[0122] 4. First Condensation Stage (400)

[0123] 5. Second Condensation Stage (500)

[0124] 6. Electromagnetic Chamber (600)

[0125] 7. Vacuum System (700)

[0126] Referring to Figure 1, there is provides an overview of the system of the present invention. Referring to Figure 1 A, provides a block diagram of the present system. Figure 1A of the present invention provides each component of the system of the present invention.

[0127] The above a system execute the method with the below steps:

[0128] Step I: Stabilization of Algae Slurry

[0129] The method begins in the stabilization tank (100), where algae slurry or liquid algae is stabilized. The tank maintains the temperature within the range of 40°C to 70°C to ensure uniform thermal distribution and optimize conditions for cavitation. The flow rate is controlled between 0.01 L / s and 5 L / s to release heat generated during subsequent cavitation, thereby preparing the slurry for efficient extraction in the next step.

[0130] In the present invention, the pumping rate output from stabilization tank to interference extractor range 10 liter to 30 liter hour and the pumping rate input from interference extractor to stabilization tank range 10 liter to 30 liter hour.

[0131] In the system, the temperature of the algae slurry is controlled over time within the stabilization tank.

[0132] Figure 2 of the present invention illustrates the graph showing how the temperature of the algae slurry is controlled over time within the stabilization tank. Figure 2 of the present invention demonstrate the precise control of the slurry's temperature (within the range of 40°C to 70°C) for optimal extraction conditions.

[0133] The graph in Figure 2 shows the production of vapor vs heat. The starting temperature in the stabilization tank (100) is preset to 27 °C and cut off temperature at 60°C. It can be seen that at 27 Celsius the vapor production is 4 litre per hour and vapor reduce when temperatureincrease. The system facilitates multiple circulation pumping with flow rate 20 litre per hour that will activate per 15 minutes, through which the stabilization tank (100) is able to maintain temperature 40 Celsius with vapor production at 3 litre per hour

[0134] Step II: Interference Wave Extraction

[0135] The stabilized slurry flows into the interference extractor (200), where piezoelectric devices operating at frequencies of 11 MHz to 26 MHz create ultrasonic interference waves. These waves significantly enhance micro-cavitation energy, enabling effective vaporization of water and oil in the algae slurry. Energy bursts of 10 to 120 watts per second are applied uniformly across the system, producing cavitation bubbles that release algae oil into the vapor phase.

[0136] Figure 3 of the present invention illustrates the graph on the cavitation energy vs. frequency of interference waves.

[0137] Based on the graph of Figure 3 it can be seen that, the cavitation energy vs. frequency relationship shows peaks in cavitation energy at specific frequencies. These peaks correspond to optimal cavitation conditions for microbubble implosion, which are critical for oil extraction from algae.

[0138] The key factors which facilitates the optimal oil extraction are:

[0139] 1) High Cavitation Energy: Optimal oil extraction occurs when cavitation energy is maximized, as stronger implosions disrupt cell membranes more effectively and release intracellular oil.

[0140] 2) Stability of Interference Waves: Frequencies near the peaks ensure stable wave interference, enhancing energy transfer to the microbubbles.

[0141] 3) Feedstock-Specific Behavior: Algae cell structure and oil content can vary, so resonance frequencies must align with the physical characteristics of the algae.

[0142] From the graph of Figure 3 it can be seen that peaks in cavitation energy occur at approximately, 5 MHz and 15 MHz. Thus, the recommended frequency of algal extraction is 5 MHz and 15 MHz.

[0143] At 5 MHz the lower-frequency waves are less likely to overheat or damage sensitive oils while ensuring effective cavitation and at 15 MHz the higher-frequency waves can provide better precision for harder-to-extract oils but may require more energy.Step III: Ion Exchange for Purification

[0144] The vaporized mixture is transferred to the ion exchanger system (300) for purification. This system comprises three layers:

[0145] 1. Positively charged copper plates (10-30 amps) to attract negatively charged impurities.

[0146] 2. Negatively charged carbon rods (10-30 amps) to attract positively charged contaminants.

[0147] 3. Grounded copper plates employing zero-voltage technology to neutralize residual impurities.

[0148] This multi-layer setup removes heavy metals and other contaminants, resulting in a purified oil vapor free of harmful substances.

[0149] Referring to Figure 4, ion exchange system (300) of the present invention is illustrated. The ion exchange system (300) is comprised of Copper plate (301), Carbon rod (302), Section A (303), Section B (304), Vapor Enter (305) and Vapor exit (306). The Copper plate (301) has a length of 10 cm and height of 4 cm. There are plurality of carbon rod (302) in the ion exchange system.

[0150] Figure 4 illustrates 10 carbon rod (302) per section. Each carbon rod (302) is of diameter 3 mm and height of 4 cm. The range between each rod is 2cm. The vapour from the interference extractor (200), enters the ion exchange system (300) through the vapour in (305) and exits from the chamber by vapour out (306).

[0151] The Section A copper plate (303), is negatively charged plate of 20 Amp 24 vdc and the Section B (304) copper plate, is positively charge of 20 Amp 24 vdc The carbon rod (302), is positively and negatively charged 20 Amp 24 vdc placed side by side.

[0152] In the table below, there is provided the mineral detected using EDX system from copper plate.

[0153]

[0154]

[0155] Figure 5 of the present invention illustrates a photographic image of the copper plate removing the heavy metal.

[0156] The table below shows the data showing the reduction in heavy metal content after passing through the ion exchange system in a specific embodiment of the present invention.

[0157]

[0158] Referring to Figure 6 of the present invention, the graph illustrates the effectiveness of the ion exchange system in reducing heavy metal concentrations (e.g., Lead, Cadmium, Mercury, Chromium, Zinc, and Nickel) from vaporized feedstock.

[0159] Figure 6 illustrates the performance of the ion exchange system in removing heavy metals, with the x-axis representing the applied current (ranging from 5 to 10 amperes) and the y-axis showing the percentage of heavy metal removed. The data reveal that metals like Lead (Pb) achieve the highest removal efficiency, reaching up to 80% at 10 amperes, while metals such as Nickel (Ni) have a lower maximum removal efficiency of 60%. Notably, there is a consistent positive correlation between amperage and removal efficiency for all metals, indicating that higher amperage enhances the system's performance. This trend highlights the effectiveness of the ion exchange system in mitigating heavy metal contamination within the Oasis Dynamics system.

[0160] Step IV: Multi-Stage Condensation

[0161] The purified vapor enters the first condensation stage (400), maintained at 1°C to 6°C. Here, heavier fractions of algae oil condense into a liquid form with a pour point of 0°C, suitable for applications not requiring ultra-low pour points.The remaining vapor progresses to the second condensation stage (500), held at -5°C to 0°C, where lighter fractions condense into oil with a pour point of -5°C. This produces a high-quality crude algae oil optimized for cold climate applications.

[0162] Referring to Figure 7, the flowchart detailing the two-stage condensation process with temperature conditions for each stage is illustrated.

[0163] Step V: Magnetic Restructuring of Oil Molecules

[0164] The residual vapor passes into the electromagnetic chamber (600), where electromagnetic waves, based on Lorentz and Faraday principles, induce molecular restructuring. This process releases oxygen and facilitates the bonding of hydrogen with oil molecules, creating a hydrogenated oil vapor with enhanced properties for biofuel applications.

[0165] Step VI: Esterification to Produce Biofuel

[0166] In the final step, the vaporized oil is drawn into the vacuum system (700), where it reacts with alcohol to undergo esterification. This results in the production of biofuel esters with a pour point below -10°C, making them suitable for aviation and automotive fuels in extremely cold climates.

[0167] Referring to Figure 8, the system for restructuring of oil molecules to finally to produce biofuel is illustrated. The system has an electromagnetic chamber (600), plurality of magnetron (601), chamber with alcohol (602) and vacuum (603). In the said system, the vapor containing fatty acids from the condenser (500) enters the electromagnetic field chamber (600), where the vapours experience magnetic field inside the electromagnetic field chamber (600) produced by the plurality of magnetron (601). The magnetron (601) releases magnetic field range at 1 ghz to 4 ghz at range of 0.5 second to 5 second. The magnetic field will influent fatty acid and vapor to experience Lorentz and faraday law. The treated fatty acid and vapor then will force into alcohol to produce biofuel in the chamber with alcohol (602).

[0168] When the vapor containing fatty acids exits the condenser (500) and enters the electromagnetic field chamber (600), the following physical phenomena occur under the influence of the magnetic field and electric field:

[0169] 1. Lorentz Force (Magnetic Influence)The vapor and fatty acid molecules, if charged or polarized, are subjected to the Lorentz Force when moving through the magnetic field.

[0170] The Lorentz Force is described as:

[0171] F z in TT% \

[0172] = q(E -t- v x B)

[0173] where:

[0174] • F : Force on a particle

[0175] • q: Charge of the particle

[0176] • E: Electric field vector

[0177] • v: Velocity of the particle

[0178] • B: Magnetic field vector

[0179] The vapor in the system contains ions and polar molecules, it experiences a force that alters their trajectory. This motion aligns or reorganizes the molecules in a manner conducive to hydrogenation and deoxygenation.

[0180] 2. Faraday's Law (Electromagnetic Induction)

[0181] When the vapor containing fatty acid interacts with the time-varying magnetic field, Faraday’s Law governs the induction of currents or electromotive force (EMF) in the vapor stream.

[0182] Faraday’s Law is given by:

[0183]

[0184] where:

[0185] • s: Induced electromotive force (EMF)

[0186] • b=B-A: Magnetic flux

[0187] • t: Time

[0188] The fatty acid in vapor then will experience electromagnetic induction in the magnetic field that induces currents or polarization in the vapor molecules. This promotes molecularinteractions such as the addition of hydrogen (hydrogenation) or the removal of oxygen atoms (deoxygenation).

[0189] 3. Hydrogenation and Deoxygenation Mechanisms

[0190] The induced currents and polarization bring hydrogen atoms in close proximity to the unsaturated bonds in fatty acids thus causing hydrogenation of the unsaturated fatty acids. The alignment of molecules via Lorentz force increases the reaction probability.

[0191] Simplified reaction:

[0192] R ■■■ CH - CH ■■■■ R1+ H ■■■■ R - CH2-■ CH2■■■■ R'

[0193] Further, the electromagnetic-induced polarization facilitates the removal of oxygen, breaking C-0 bonds causing deoxygenation.

[0194] For example:

[0195]

[0196] 4. Additional Physical Effects Due to Magnetic field

[0197] The charged particles or ions in the vapor experience circular motion or cyclotron motion due to the magnetic field, which enhances the mixing and reaction kinetics.

[0198] Under electromagnetic influence, molecules can ionize, leading to intermediate steps that accelerate chemical changes facilitating ionization and recombination.

[0199] The Oasis Dynamics magnetic field reactor leverages a series of magnetrons to generate pulsing magnetic fields with specific parameters: pulse duration ranging from 0.5 to 5 seconds and a frequency range between 1 MHz to 4 MHz.

[0200] Shorter pulses (e.g., 0.5 seconds) deliver rapid energy bursts that can destabilize weak molecular bonds, while longer pulses (e.g., 5 seconds) allow for sustained exposure, enabling deeper restructuring of more complex molecular configurations.The frequency range plays a critical role, with lower frequencies (1 MHz) broadening the excitation of oil molecules and aiding in the breakdown of larger clusters, while higher frequencies (up to 4 MHz) target finer molecular interactions to enhance atomic-level alignment. The strength of the magnetic field also influences the process, with stronger fields aligning polar molecules more effectively, thereby improving molecular restructuring. This magnetic pulsing process significantly enhances the efficiency and performance of biofuels, optimizing molecular structure for better combustion, reducing viscosity, improving pour points, and increasing calorific value, making the biofuel more suitable for high-performance applications such as aviation fuel.

[0201] Figure 9 of the present invention illustrates the magnetic field strength vs. restructuring efficiency.

[0202] Figure 9 illustrates that the restructuring efficiency increases with magnetic field strength, ranging from 0.1 to 0.6 Tesla, but plateaus at higher values.

[0203] In the said graph X-Axis represents the range of magnetic field strengths applied by the magnetic reactor (0.1 Tesla to 0.6 Tesla). This range reflects the realistic operational parameters of the reactor system. Y-Axis represents the restructuring Efficiency of the system, indicating the percentage of oil molecules effectively restructured under varying magnetic field strengths.

[0204] The graph illustrates that restructuring efficiency increases with stronger magnetic fields but approaches a plateau at higher strengths. At 0.1 Tesla, the restructuring efficiency starts at 10%, showing limited molecular reordering. Efficiency rapidly improves with increased magnetic field strength, reaching 80% at 0.4 Tesla. Beyond 0.5 Tesla, the efficiency gains begin to plateau, stabilizing at around 95%. This suggests that additional strength may have diminishing returns.

[0205] The parameters play a crucial role in optimizing the magnetic processing of oil. Pulse duration, ranging from 0.5 to 5 seconds, influences the interaction between the magnetic field and oil molecules — longer pulses sustain exposure, enhancing molecular interaction, while shorter pulses create rapid alignment suitable for smaller, simpler molecular groups.Frequency, from 1 to 4 MHz, affects the restructuring efficiency — higher frequencies (3-4 MHz) improve the alignment of smaller, more complex molecular clusters, while lower frequencies (1-2 MHz) are effective for larger clusters, breaking emulsified layers and realigning molecular bonds. Magnetic processing is vital for enhancing oil molecule uniformity and reducing impurities, directly improving biofuel performance metrics such as calorific value, pour point, and emissions. The optimization graph highlights the reactor's efficiency, emphasizing the need for fine-tuning magnetic field strength to achieve maximum performance.

[0206] The magnetic processing effect of the present invention

[0207] Referring to Figure 9A of the present invention the effect of magnetic field strength on molecular weight distribution is illustrated. The line in the graph shows that increasing magnetic field strength reduces the molecular weight distribution, indicating effective molecular restructuring.

[0208] Referring to Figure 9B of the present invention the speed of fatty acid is calculated from time of flight. The line in the graph shows the speed of fatty acids (in m / s) over increasing distances (30 cm to 120 cm). The speed is calculated based on the time of flight, showing a linear relationship for constant acceleration or consistent flow conditions.

[0209] These graphs together showcase the dual effects of magnetic processing: molecular restructuring and the dynamics of fatty acid movement.

[0210] Based on the method described above the biofuel ester from wet algae slurry was obtained in the following conditions in the embodiments I to IV:

[0211] Embodiment I

[0212] • Materials: Wet algae slurry containing 30% algae biomass was obtained from from cultivated salt water environment that add with nutrient. The sample are commonly available that have been cultivated for biofuel.

[0213] Stabilization: The temperature in the stabilization tank was maintained at a temperature of 50°C with a flow rate of 0.01 L / s for 2 hours for ensuring uniform thermal distribution to the algal slurry of the subsequent step.Interference Wave Extraction: The slurry is subjected to ultrasonic interference waves at 15 MHz, with each point within the tank is energized at 10 watts per second which results in vaporization of the oil.

[0214] • Purification: The vapor is passed through an ion exchange system with copper plates at 20 amps and carbon rods at 25 amps. The oil passes through a series of stages to remove heavy metals.

[0215] • Multi-stage Condensation: The vapor is condensed at 3°C in the first stage and at - 2°C in the second stage, producing a heavy fraction oil with a pour point of 0°C and a light fraction with a pour point of -5°C.

[0216] • Magnetic Processing: The remaining vapor is processed through a magnetic field to restructure the oil molecules.

[0217] • Esterification: The oil is esterified with methanol to produce a biofuel ester with a pour point of -12°C, suitable for use in aviation fuel.

[0218] Embodiment II

[0219] • Materials: Liquid algae with a moisture content of 85% was obtained from cultivated salt water environment that add with nutrient. The sample are commonly available that have been cultivated for biofuel.

[0220] • Stabilization: The temperature in the stabilization tank was maintained at a temperature of 60°C with a flow rate of 3 L / s for 1 hours for ensuring uniform thermal distribution to the algal slurry of the subsequent step.

[0221] • Interference Wave Extraction: The slurry is subjected to ultrasonic interference waves at 20 MHz, with each point within the tank is energized at 100 watts per second which results in vaporization of the oil.

[0222] • Purification: The vapor is passed through an ion exchange system with copper plates at 25 amps and carbon rods at 15 amps. The oil passes through a series of stages to remove heavy metals.

[0223] • Multi-stage Condensation: The vapor is condensed at 4°C in the first stage and at - 3°C in the second stage, producing a heavy fraction oil with a pour point of 0°C and a light fraction with a pour point of -5°C.• Magnetic Processing: The remaining vapor is processed through a magnetic field to restructure the oil molecules.

[0224] • Esterification: The oil is esterified with methanol to produce a biofuel ester with a pour point of -15°C, suitable for use in aviation fuel.

[0225] Characterization of the algal oil obtained

[0226]

[0227] The table presents the fatty acid composition of three different samples (Sample 1, Sample 2, and Sample 3) analyzed using Gas Chromatography -Mass Spectrometry (GCMS). The GCMS is set to make detection of fatty acid from our produce condensation liquid, a liquid produce in condensation 1 and 3. Samples 1, 2 and 3 are samples from 3 tests to check the stability of our process in extracting oil from algae slurry.

[0228] The fatty acid components are expressed as percentages of total fatty acid methyl esters (FAME). For each sample, the presence of various fatty acids is listed, including saturated fatty acids like propionic acid (C3:0), palmitic acid (C16:0), stearic acid (C18:0), and unsaturated fatty acids like oleic acid (C18:l) and linoleic acid (C18:2).

[0229] Sample 1 contains the highest percentage of stearic acid (44.21%), followed by palmitic acid (11.77%) and oleic acid (5.7%).

[0230] Sample 2 has a similar composition but slightly lower levels of palmitic acid (9.98%) and oleic acid (3.7%), while Sample 3 shows values closer to Sample 1, with 44.32% stearic acid and 11.56% palmitic acid.

[0231] The total FAME percentages for all samples are relatively high, ranging from 60.43% to 63.37%, indicating that the majority of the components in these samples are fatty acid derivatives. Some fatty acids such as capric acid (C6:0) and octanoic acid (C8:0) are missing or unquantified in the samples, while others like heneicosanoic acid (C21:0) and docosanoic acid (C22:0) appear in smaller amounts across the samples.

[0232] Example 2: Comparison of standard algae oil (ISO 8217) with the algal oil of the present invention

[0233] In the table below, the key properties of standard algae oil (ISO 8217) was compared the with oil processed using the Oasis Dynamics Algae Oil Extraction Technology.

[0234]

[0235] The Oasis Dynamics biofuel demonstrates several notable properties compared to standard biodiesel specifications. Its viscosity is 24.1 CST, which is lower than the standard range of 30-50 CST at 40°C, making the oil easier to refine and handle while still meeting biodiesel standards. The pour point of 0°C indicates improved flow characteristics in colder conditions, suitable for moderate climates, while the cloud point matches the standard at 5°C but may require improvement for extremely cold climates to prevent solidification. The sulphur content is non-detectable, making the oil cleaner and more appropriate for low-emission fuels, and its calorific value is 37.4 MJ / kg, slightly above the standard range of 35-38 MJ / kg, offering enhanced fuel performance. The carbon content is 75.6%, closely aligning with the typical 76% standard for energy-dense fuels. Nitrogen content is 4%, within the standard range of 3-6%, but a slight reduction could further improve emissions. With a flash point of 115°C, the biofuel is safe for storage and handling, falling within the standard range of 100-120°C. The density is 0.892 g / cm3, also within the standard range of 0.88-0.95 g / cm3, making it suitable for blending into biofuels.Overall, the table demonstrates that the oil extracted using Oasis Dynamics technology exhibits favorable characteristics for biofuel production, including low viscosity, non-detectable sulfur, high calorific value, and safe handling properties, making it an efficient and environmentally friendly alternative to standard algae oil.

[0236] Example 3: Comparison of Pour Point of Crude and Purified Algae Oils

[0237] Referring to Figure 10 of the present invention, the pour points of four different oil types obtained in the present invention focusing on their performance in cold climates is provided. In the graph the X-axis represents different oil types, including Crude Algae Oil, Heavy Fraction Crude Oil, Light Fraction Crude Oil, and Biofuel Ester while the Y-axis represents the pour point in degrees Celsius, indicating the lowest temperature at which the oil remains fluid, where lower values reflect better performance in cold climates.

[0238] Crude Algae Oil is the initial output from algae oil extraction.

[0239] Heavy Fraction Crude Oil is a thicker, less refined component commonly used in industrial applications, while Light Fraction Crude Oil is a more refined product used in fuels such as gasoline and kerosene.

[0240] Biofuel Ester, derived from algae oil, is a highly refined product optimized for cold-weather and renewable energy applications.

[0241] Crude Algae Oil has a pour point of 0°C, making it suitable for moderate climates but less ideal for colder conditions. Heavy Fraction Crude Oil, with a pour point of -10°C, offers better cold-weather performance but remains limited in extreme cold. Light Fraction Crude Oil improves further with a pour point of -20°C, demonstrating superior fluidity in colder environments. Biofuel Ester, with a remarkable pour point of -40°C, outperforms all other oil types, showing exceptional cold-weather suitability, ideal for aviation fuel or winter-use biodiesel.

[0242] Overall, Biofuel Ester’s significantly lower pour point highlights its superior adaptability to cold climates, a direct benefit of advanced refining and processing. The trend across oil types demonstrates that as oils become more refined, their pour points improve, showcasing the importance of innovative extraction technologies like Oasis Dynamics in enhancing fuel performance.

[0243] Example 4: Yield of Biofuel Ester at Different Esterification Conditions1

[0244] Referring to Figure 11 of the present invention, the relationship between esterification temperature and biofuel ester yield is provided.

[0245] The relationship between esterification temperature and biofuel ester yield follows a distinct trend.

[0246] The yield steadily increases from 85% at 40°C, reaching a peak of 98% at 60°C.

[0247] However, beyond 60°C, the yield begins to decline, dropping slightly to 95% at 70°C and further to 90% at 80°C.

[0248] This indicates that 60°C is the optimal temperature for esterification under the given conditions, as it produces the highest yield.

[0249] At lower temperatures, the reaction proceeds more slowly, resulting in reduced yield, while higher temperatures may lead to side reactions or thermal degradation of reactants and products, thereby decreasing the overall yield. This underscores the importance of temperature control to maximize efficiency and output in the esterification process.

[0250] Referring to Figure 12 of the present invention, the relationship between alcohol-to-oil ratio and biofuel ester yield is provided.

[0251] The relationship between alcohol-to-oil ratio and biofuel ester yield shows a clear trend.

[0252] The yield increases from 80% at a ratio of 3:1, reaching its maximum of 98% at ratios of 6:1 and 9:1.

[0253] However, at a ratio of 12:1, the yield slightly declines to 97%. This indicates that the optimal alcohol-to-oil ratios for maximizing yield are 6: 1 and 9:1.

[0254] Higher alcohol-to-oil ratios drive the reaction toward ester formation, enhancing yield. However, excessively high ratios, such as 12:1, can dilute the reactants, reduce reaction efficiency, and increase recovery costs for unreacted alcohol, highlighting the need to balance ratio selection for both efficiency and cost-effectiveness.

[0255] Example 5: Crude Algae Oil Composition Before and After Condensation

[0256] Referring to Figure 13 of the present invention, proportions of heavy and light fractions of crude algae oil before and after the multi-stage condensation process, alongside the pour points is provided.This chart combines the proportions of heavy and light fractions of crude algae oil before and after the multi-stage condensation process, alongside the pour points:

[0257] • Blue Bars: Proportions before condensation (33% heavy, 67% light).

[0258] • Green Bars: Proportions after condensation (60% heavy, 40% light).

[0259] • Red Line: Pour points for heavy and light fractions, showing -10°C and 0°C, respectively.

[0260] This visualization highlights how the process increases the heavy fraction and supports the novel separation approach. The pour points further validate the separation efficiency based on physical properties.

[0261] Example 6: Comparison on pour Point of Biofuels and Esterification Conditions Referring to Figure 14 of the present invention, the relation between the pour point and esterification temperature is provided. It can be seen that as the esterification temperature increases, the pour point of the biofuel decreases.

[0262] This trend suggests that higher temperatures improve the fluidity of the biofuel at low temperatures.

[0263] Referring to Figure 15 of the present invention, the relation between the pour point and Alcohol-to-Oil Ratio is provided. It can be seen that increasing the alcohol-to-oil ratio also decreases the pour point, with diminishing returns at very high ratios. This indicates an optimal range for maximizing low-temperature performance.

[0264] Example 7: Engine performance using the biofuel ester of the present invention

[0265] Referring to Figure 16 of the present invention, the engine efficiency of the present invention is illustrated using the biofuel ester.

[0266] The biofuel ester of the present invention demonstrates consistently higher engine efficiency compared to conventional fuels across all temperature ranges, with its performance peaking at 91% efficiency at 20°C. In contrast, conventional fuels exhibit lower initial efficiency and a more gradual increase, reaching a maximum efficiency of 86% at 20°C. This highlights the superior combustion properties and energy conversion potential of biofuel ester, making it a more efficient alternative for fuel applications.Referring to Figure 17 of the present invention, the engine emission of the present invention is illustrated using the biofuel ester. It is seen that the biofuel ester of the present invention, generates significantly lower emissions compared to conventional fuels, starting at 50 units at -20°C and steadily decreasing to 30 units at 20°C. In contrast, conventional fuels produce higher emissions, beginning at 70 units at -20°C and reducing to 50 units at 20°C. This demonstrates the superior environmental performance of biofuel ester, offering cleaner combustion and reduced pollutant output across a range of temperatures.

[0267] Example 8: Comparative advantage of the present invention over the traditional method

[0268] The below table shows the advantages of the present invention over the existing traditional methods.

[0269]

[0270] Overall, the present invention provides increased yield, improved purification, scalability, and lower processing time. The process of the present invention is also environment friendly.

Claims

CLAIMS1. A method for extracting algae oil from wet algae slurry or liquid algae, comprising the steps of:(i) providing a stabilization tank (100) configured to stabilize input conditions by controlling the flow and temperature of an algae slurry or liquid algae within the range of 40°C to 70°C and subjecting the algae slurry or liquid algae in the stabilization tank; (ii) subjecting the algae slurry or liquid algae of step (i) to interference wave extraction interference (200) using piezoelectric devices operating at frequencies between 11 MHz and 26 MHz to enhance cavitation energy causing the mixture to vaporize;(iii) passing the vaporized mixture of step (ii) through an ion exchange system (300) to isolate the heavy metals from vapor to improve the purity of the extracted oil; wherein the ion exchange system further comprises:i) copper plates (301) arranged as the first layer, positively charged at 10-30 amps;ii) carbon rods (302) as the second layer, negatively charged at 10-30 amps; iii) copper plates as the third layer (303, 304), grounded to zero voltage; (iv) condensing the vaporized mixture in a multi-stage condensation process to obtain separated heavy and light fractions of crude algae oil;wherein the multi-stage condensation process comprises:i) a first stage condensation (400) wherein the vaporized mixture is condensed at a temperature between 1°C and 6 °C to separate a heavy fraction crude algae oil with a pour point of0°C; andii) a second stage condensation (500) wherein the remaining vapor is condensed at a temperature between -5 °C and 0°C to separate a light fraction crude algae oil with a pour point of -5°C;(v) processing the remaining vaporized components through a magnetic field to restructure the oil molecules;(vi) esterifying the oil vapor in alcohol to produce a high-performance biofuel ester with a pour point below -10°C.

2. The method of claim 1, wherein the stabilization tank (100) has an adjustable flow rate between 0.01 L / s and 5 L / s.

3. The method of claim 1, wherein the interference wave extraction is achieved by piezoelectric devices operating at 10 to 120 watts per second.

4. The method of claim 1, wherein esterification is carried out by drawing the vapour by a vacuum system (700) and infusing into liquid alcohol.

5. The method of claim 1, wherein the magnetic field processes the vaporized components by applying Lorentz and Faraday principles to trigger molecular restructuring, thereby enabling the release of oxygen and merging of hydrogen with other molecules.

6. The method of claim 1, wherein the esterification step produces a biofuel with a pour point below -10°C, suitable for use in aviation and automotive fuel applications.

7. The method of claim 1, wherein the algae oil produced is suitable for use as biofuel, lubricants, and other industrial applications requiring renewable and low-temperature resilient oils.

8. A high-performance biofuel ester produced by the process of claim 1, wherein the biofuel ester is obtained in step (vi) after the oil vapor is esterified in alcohol, resulting in a biofuel ester with a pour point below -10°C, making it suitable for use in coldclimate applications such as aviation and automotive fuels.

9. A heavy fraction crude algae oil produced by the process of claim 1, wherein the heavy fraction crude algae oil is obtained in step (iv)(i) of the process, after the vaporized mixture is condensed at a temperature between 1°C and 6 °C, resulting in a heavy fraction crude algae oil with a pour point of 0°C.

10. A light fraction crude algae oil produced by the process of claim 1, wherein the light fraction crude algae oil is obtained in step (iv)(ii) of the process, after the remaining vapor is condensed at a temperature between -5 °C and 0°C, resulting in a light fraction crude algae oil with a pour point of -5°C.

11. A biofuel composition comprising the biofuel ester obtained by the process of claim 1, produced by the process of claim 1, wherein the biofuel ester is suitable for use in aviation or automotive engines under low-temperature conditions.

12. A purified algae oil composition produced by the process of claim 1, wherein the purified algae oil is obtained in step (iii) after the algae slurry or liquid algae is subjected to the ion exchange system (300), resulting in a purified algae oil composition with reduced heavy metal contaminants.

13. A crude algae oil composition produced by the process of claim 1, comprising a mixture of heavy and light fractions of crude algae oil, wherein the heavy fraction is obtained instep (iv)(i) with a pour point of 0°C, and the light fraction is obtained in step (iv)(ii) with a pour point of -5°C.

14. A system for extracting algae oil from algae slurry or liquid algae, comprising:i) a stabilization tank (100) for controlling flow rate and temperature of the algae slurry, maintaining temperatures between 40°C to 70°C;ii) an interference wave extractor (200) comprising piezoelectric devices operating in the frequency range of 11 MHz to 26 MHz to generate interference waves that enhance cavitation energy and cause vaporization of the algae oil mixture.iii) an ion exchanger system (300) comprising at least three layers for purifying the vaporized mixture, including:i) Copper plates (301) arranged as the first layer, positively charged at 10-30 amps;ii) Carbon rods (302) arranged as the second layer, negatively charged at 10-30 amps; andiii) Copper plates (303, 304) arranged as the third layer, grounded to zero voltage, iv) condensation system comprising at least two stages of cooling to condense the vaporized mixture, with the first stage condensation (400) cools to 1-6°C and the second stage condensation (500) cools to -5 to 0°C, wherein the condensation process has limitations in separating fine volatile components and residual impurities;vi) a magnetic field processing unit (600) for applying Lorentz and Faraday principles to restructure oil molecules by magnetrons (601); andvii) a vacuum esterification unit (700) for infusing the vaporized algae oil into alcohol to produce a biofuel ester with a pour point below -10°C.

15. The system of claim 14, wherein the stabilization tank (100) has an adjustable flow rate between 0.01 L / s and 5 L / s.

16. The system of claim 14, wherein the esterification unit uses methanol or ethanol as the alcohol for esterification.

17. The system of claim 14, wherein the biofuel ester produced in the esterification unit has a pour point of below -10°C, making it suitable for use in aviation and automotive fuel applications.

18. The system of claim 14, wherein the condensation stages are configured to separate the heavy fraction crude algae oil with a pour point of 0°C and the light fraction crude algae oil with a pour point of -5°C.

Images