US20200032153A1 - Method for Producing HydroCarbon-Based Synthetic Fuel By Adding Water to Hyrocarbon-Based Fuel Oil - Google Patents

Method for Producing HydroCarbon-Based Synthetic Fuel By Adding Water to Hyrocarbon-Based Fuel Oil Download PDF

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US20200032153A1
US20200032153A1 US16/337,824 US201716337824A US2020032153A1 US 20200032153 A1 US20200032153 A1 US 20200032153A1 US 201716337824 A US201716337824 A US 201716337824A US 2020032153 A1 US2020032153 A1 US 2020032153A1
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water
fuel oil
hydrocarbon
oil
synthetic fuel
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English (en)
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Fumio Aoki
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Tristarhco Co Ltd
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Tristarhco Co Ltd
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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
    • C10L1/32—Liquid carbonaceous fuels consisting of coal-oil suspensions or aqueous emulsions or oil emulsions
    • C10L1/328—Oil emulsions containing water or any other hydrophilic phase
    • 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
    • C10L2200/00—Components of fuel compositions
    • C10L2200/02—Inorganic or organic compounds containing atoms other than C, H or O, e.g. organic compounds containing heteroatoms or metal organic complexes
    • C10L2200/0295—Water
    • 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
    • C10L2200/00—Components of fuel compositions
    • C10L2200/04—Organic compounds
    • C10L2200/0407—Specifically defined hydrocarbon fractions as obtained from, e.g. a distillation column
    • C10L2200/0438—Middle or heavy distillates, heating oil, gasoil, marine fuels, residua
    • 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
    • C10L2250/00—Structural features of fuel components or fuel compositions, either in solid, liquid or gaseous state
    • C10L2250/06—Particle, bubble or droplet size
    • 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
    • C10L2290/14—Injection, e.g. in a reactor or a fuel stream during fuel production
    • C10L2290/146—Injection, e.g. in a reactor or a fuel stream during fuel production of water
    • 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
    • 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
    • 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
    • C10L2290/36—Applying radiation such as microwave, IR, UV

Definitions

  • the present invention relates to a method of producing a hydrocarbon-based synthetic fuel equivalent to a hydrocarbon-based base fuel oil by adding water to the base oil.
  • Fuel obtained by employing the conventional technique of mixing water to fuel oil is regarded as environmental load-reducing fuel, because the technique is capable of significantly reducing the amount of fuel to be used, and reducing carbon dioxide (CO 2 ) emission by an amount corresponding to the reduced amount of fuel used. Further, fuel oil according to this technique can be expected to be completely combusted, so that there are advantageous effects of being able to fairly reduce the amount of air to be used for combustion, and thus to suppress generation of nitrogen oxides and particulate matter (PM), and reduce an environmental load due to emission gas from boilers or internal combustion engines.
  • PM nitrogen oxides and particulate matter
  • JP 4682287B proposes a water-added fuel production method which comprises: adding catalase to a mixture of fuel oil and water; stirring and mixing the catalase-added fuel oil-water mixture while bringing the mixture into contact with a natural mineral or a metal excited by a vibrational wave such as an ultrasonic wave, thereby enhancing the degree of transparency of the mixture in an emulsion state. More specifically, the Patent Document 1 discloses a method which comprises: stirring and mixing the catalase-added fuel oil-water mixture under a contact with a natural mineral or a metal excited by a vibrational wave; and to heating the stirred and mixed fuel oil-water mixture to 30° C.
  • the catalase-added fuel oil-water mixture is brought into contact with a natural mineral or a metal excited by a vibrational wave, to fragment a molecular assembly of the fuel oil and the water, and then, after stirring and mixing the fuel oil-water mixture, the stirred and mixed fuel oil-water mixture is heated and pressurized, whereby it is possible to fuse the fuel oil and the water together, and enhance the degree of transparency of a water-added fuel in an emulsion state.
  • Example 1 two examples, Example 1 and Example 2, are shown, and it is described that, in each of the examples, water and fuel oil were mixed in equal amount, and transparent fuel oil could be obtained by going through a fusion step.
  • this production method makes it possible to prevent an oil-water separation phenomenon in an emulsion fuel having a water addition rate of 50% or more.
  • the production method described in the Patent Document 1 is based on the assumption that the amount of hydrocarbon serving as a source of combustion calorie is reduced by adding water to fuel oil, and is intended to compensate for the decline in combustion calorie due to the reduction of the hydrocarbon, by increasing the content rate of hydrogen in the fuel oil by the action of catalase. That is, teaching of the Patent Document 1 is that the hydrogen content rate can be increased by using catalase to decompose hydrogen peroxide into hydrogen and oxygen, and allowing the hydrogen to remain in the fuel oil, while releasing the oxygen to the atmosphere.
  • there is a limit on compensating for the decline in rate of hydrocarbon due to water addition only by increasing the hydrogen content rate. Thus, it is difficult to expect a significant increase in amount of fuel, from the method taught by the Patent Document 1.
  • Patent Document 2 JP 2014-47229A discloses a method of producing an emulsion fuel which has capability to avoid fuel oil-water separation over a long period of time without using any surfactant, and exhibits about the same equality and calorific value as those of base fuel oil, This method comprises: causing water to flow in contact with tourmaline irradiated with far-infrared rays, microwave or ultrasonic wave; causing fuel oil to flow in contact with titanium oxide balls each having an electromagnetic wave-responsive catalyst added thereto; mixing the water and the fuel oil to prepare a mixture; and applying heat and pressure to the mixture while circulating the mixture.
  • the hydrogen content rate can be increased by addition of catalase.
  • the Patent Document 2 does not include any technical teaching going beyond that of the Patent Document 1.
  • Non-Patent Document 1 In the research paper titled “An efficient way of producing fuel hydrocarbon from CO 2 and activated water” authored by Tadayuki IMANAKA, et al., and published to the Web by J-STAGE on Aug. 29, 2015 (Non-Patent Document 1), there is disclosed a method which comprises: generating activated water by performing treatment in which water containing nanobubbles is subjected to irradiation with UV light and black light (wavelength; 350 nm to 400 nm) in the presence of a titanium dioxide catalyst; mixing this activated water with light oil; and strongly stirring the resulting mixture to produce a synthetic oil.
  • UV light and black light wavelength; 350 nm to 400 nm
  • the activated water is mixed with light oil by a special mixture serving as a reaction tank, such that the resulting mixture is brought into collision with a wall of the mixer, and the mixture is circulated to repeat the collision.
  • carbon dioxide is supplied to an upper space of the mixer serving as a reaction tank.
  • a cloudy emulsion is generated in the above process.
  • the emulsion is statically stored (left at rest), the emulsion is separated into two phases consisting of an oil phase and a water phase. Then, oil equivalent to light oil can be obtained from the oil phase.
  • the research paper of the Non-Patent Document 1 reports that, with respect to the light oil used as base oil, light oil increased in amount by 5 to 10 volume % was obtained through the method disclosed therein.
  • carbon dioxide is supplied to the upper space of the mixer. This is understood as a technique of compensating for carbon which became deficient due to water addition, by decomposition of carbon dioxide.
  • Patent Document 2 JP 2014-47229A
  • Non-Patent Document 1 Tadayuki IMANAKA, et al., “An efficient way of producing fuel hydrocarbon from CO 2 and activated water”, J-STAGE, published to the Web on Aug. 29, 2015
  • Non-Patent Document 2 Shinobu KODA, “Chemical Application of Cavitation; Sonochemistry (Application of Cavitation Induced by Ultrasound)”, Journal of the Institute of Electronics, Information and Communication Engineers of JAPAN, Vol J89-A, No. 9 (2006)
  • Non-Patent Document 3 Keiji YASUDA, “Decomposition of Chemical Compounds by Ultrasound and Development of Sonochemical Reactor”, “THE CHEMICAL TIMES”, published by Kanto Chemical Co., In, Apr. 1, 2009
  • Non-Patent Document 4 Yoshiteru MIZUKOSHI, “Basis of Ultrasonic Waves”, presentation material for “Monodzukuri Basic Course (34th Technical Seminar)” held on Feb. 20, 2013 at the Creation-Core Higashiosaka
  • the methods described in the above heretofore-known documents might be able to achieve a certain level of increase rate with respect to fuel oil used as base oil, there is a limit on the level of increase rate.
  • the increase rate is no more than 10 volume %, and in the methods described in the Patent Documents 1 and 2, an achievable of the increase rate is only about 20 volume %.
  • the present invention addresses the above conventional problem, and an object thereof is to provide a method of producing a hydrocarbon-based synthetic fuel by adding water to base oil, wherein the method is capable of significantly increasing the ratio of the synthetic fuel to a hydrocarbon-based fuel serving as the base oil.
  • a base fuel oil i.e., fuel before water addition
  • a method of producing a hydrocarbon-based synthetic fuel oil having a volume greater than that of a hydrocarbon-based base fuel oil, by addition of water to the hydrocarbon-based base fuel oil wherein a process of using a first-order hydrocarbon-based synthetic fuel oil produced in a first cycle of the production method, as a base fuel oil for producing a second-order hydrocarbon-based synthetic fuel oil, the process being carried out one or more times to produce a hydrocarbon-based synthetic fuel oil having a high water addition rate.
  • a hydrocarbon-based synthetic fuel oil production method which comprises:
  • hydrocarbon-based synthetic fuel oil production method which comprises:
  • the activated water is activated such that it includes hotspots arising from microbubbles.
  • the activated water generation step is carried out by heating water to a temperature ranging from 35° C. to 45° C., while applying a voltage to the water, and, radiating an ultrasonic wave to the water. More preferably, the voltage application is performed by radiating an ultrasonic wave to tourmaline immersed in the water to bring the tourmaline into an excited state.
  • the activated water includes hotspots arising from microbubbles
  • the water contains a substance effective in holding the hotspots arising from microbubbles.
  • the hotspots arising from microbubbles are generated by radiating, to the water, an ultrasonic wave having a frequency different from a frequency of the ultrasonic wave which is radiated to the tourmaline.
  • the reactive environment in the stirring and mixing step is formed by adding catalase to the water and then stirring the water while radiating an ultrasonic wave to the water. More preferably, the stirring is performed to create strong waves on a surface of the mixture of the water and the base fuel oil.
  • the reactive environment in the stirring and mixing step is formed by adding photocatalyst to the water and then stirring the water while radiating ultraviolet light to the water.
  • a synthetic fuel oil produced by the method of the present invention is a hydrocarbon-based synthetic fuel oil which is substantially free of water (H 2 O) and has a composition and physical properties substantially identical or equal to or approximate to those of a base fuel oil.
  • the base fuel oil is light oil for use as diesel fuel
  • a synthetic light oil produced by the present invention is substantially free of water (H 2 O), and it has been ascertained that no oil-water separation occurs even after long-term storage.
  • the method of the present invention also can produce heavy oil substantially identical or equal to or approximate to the A-Class heavy oil.
  • the resulting synthetic fuel is substantially free of water (H 2 O) and has a composition and physical properties substantially identical to or approximate to those of the base fuel oil.
  • H 2 O water
  • carbon dioxide it is conceivable to take in carbon dioxide in surrounding air through a liquid surface of the mixture of the base fuel oil and the water, and decompose the carbon dioxide to utilize the resulting carbon as at least a large part of carbon necessary for a reaction for producing the synthetic fuel.
  • the stirring and mixing step in a case where the stirring and mixing step is performed in a space opened to the atmosphere, it is effective that, in the stirring and mixing step, the mixture of the base fuel oil and the water is recirculated to create strong waves on a liquid surface of the mixture.
  • a surrounding area of a site for performing the stirring and mixing step is a closed space, the amount of carbon dioxide to be taken in from surrounding air becomes insufficient.
  • an intended synthetic fuel can be obtained by adding carbon to the mixture of the base fuel oil and the water.
  • carbon to be added it is possible to use charcoal obtained by carbonizing wood. It is also possible to advantageously use a carbon powder used in industrial applications.
  • carbon monoxide gas or carbon dioxide gas may be added and then decomposed in the same manner as that for carbon dioxide gas taken in from surrounding air, and resulting carbon may be used to produce a synthetic fuel.
  • hydrogen necessary for creating hydrocarbon as a combustible component is obtained by decomposition of molecules of the activated water.
  • water molecules are activated to include hotspots arising from microbubbles. It has been ascertained that hydrogen necessary for the reaction can be obtained by adding at least one selected from the group consisting of catalase, sodium hydroxide and an aqueous hydrogen peroxide solution, to water including such activated molecules, and stirring the resulting mixture.
  • a mixing ratio by volume of the water to the base fuel oil is set to about 1 or less with respect to 1 of base fuel oil.
  • the stirring and mixing step includes: putting only the base fuel oil into a stirring and mixing tank; and then adding and mixing the water after undergoing a water activation step and an additive input step, to and with the base fuel oil in increments of a given amount, while stirring the base fuel oil.
  • the mixture is intensely stirred to create strong waves on a liquid surface. This advantageously enables carbon dioxide in air to be taken in the mixture.
  • the method of the present invention is implemented using an apparatus comprising: a stirring and mixing tank having a cylindrical portion; and at least one injection pipe for putting the water after undergoing the water activation step and the additive input step, into the stirring and mixing tank by means of injection or the like, wherein an injection direction of the water from the injection pipe is set to have a given angle with respect to a diametrical line of the cylindrical portion.
  • the given angle is preferably in the range of about 40 degrees to about 50 degrees, particularly about 45 degrees.
  • the given angle in each of the injection pipes is preferably set to a specific angle, e.g., about 45 degrees, falling within the range of about 40 degrees to about 50 degrees.
  • an injection port of the injection pipe is preferably disposed at a position upwardly away from the liquid surface by at least about 8 cm, preferably 10 cm or more, to inject the activated water onto the liquid surface in the form of a high-speed jet.
  • the injection pipe has a protruding portion protruding inside the stifling and mixing tank.
  • the protruding portion preferably has a length of about 10 cm.
  • catalase may be added by 0.04 to 0.05% in terms of a ratio by weight thereof to the water, in the additive input step.
  • the water activation step may include activating the water such that an ORP (Oxidation-Reduction Potential) value thereof falls within the range of 160 mV to-200 mV.
  • ORP Oxidation-Reduction Potential
  • the water activation step may include: keeping tourmaline or a copper ion generating material in contact with the water; and, in this state, alternately radiating first and second ultrasonic waves each having a respective one of a frequency of 10 kHz to 60 kHz and a frequency of 200 kHz or more, to the water, or the tourmaline or the copper ion generating material, thereby activating the water by electrical energy radiated from the tourmaline or copper ions radiated from the copper ion generating material.
  • the fusion step may be performed under a pressurization condition set at about 0.3 MPa or more and a heating condition set in the range of about 40° C. to about 80° C.
  • the stirring and mixing step may be performed using an OHR (Original Hydrodynamic Reaction) mixer.
  • the method of the present invention makes it possible to obtain a hydrocarbon-based synthetic fuel oil which is less likely to cause or free from causing oil-water separation after being synthesized or fused once. Further, by repeating the cycle of the steps, using a synthetic fuel oil obtained in the previous cycle as a base oil for the current cycle, it becomes possible to efficiently produce a hydrocarbon-based synthetic fuel oil having a high water addition rate.
  • the synthetic fuel oil produced by the method of the present invention is substantially free of water (H 2 O) and has a composition and physical properties substantially identical to or approximate to those of the base fuel oil, as mentioned above.
  • the hydrocarbon-based synthetic fuel oil of the present invention is equal to or superior to existing fuel oils, in terms of a calorific value per unit quantum, and has an advantageous effect of being less likely to cause degradation or corrosion of a combustion chamber, an exhaust pipe or the like after combustion, as compared to the existing fuel oils.
  • the synthetic fuel oil of the present invention can achieve advantageous effects of: being excellent in perfect combustibility; being less likely to generate carbon monoxide; and being low in amount of emission of carbon monoxide.
  • FIG. 1 is a process chart of a synthetic fuel oil production method according to one embodiment of the present invention.
  • FIG. 2 is a diagram depicting the overall configuration of a production apparatus capable of implementing the synthetic fuel oil production method according to the one embodiment.
  • FIG. 3 is a diagram depicting the structure of an injection pipe for injection to a reaction tank, in a stirring device usable in the production apparatus in FIG. 2 .
  • FIG. 4 is a schematic diagram depicting one example of an ionization device usable in the production apparatus in FIG. 2 .
  • FIG. 5 is a chart presenting a result of GC-MS analysis regarding a hydrocarbon-based synthetic fuel oil obtained in one example using light oil as base oil.
  • FIG. 6 is a chart presenting a result of GC-MS analysis regarding a synthetic fuel obtained in another example using light oil as base oil.
  • FIG. 7 is a chart presenting a result of GC-MS analysis regarding the light oil used as base oil.
  • FIG. 8 is a chart presenting a result of GC-MS analysis regarding yet another synthetic fuel obtained in yet another example using A-heavy oil as base oil.
  • FIG. 9 is a chart presenting a result of GC-MS analysis regarding the A-heavy oil used as base oil.
  • FIG. 1 is a flowchart of a process regarding the method according to this embodiment, to be performed in the following production apparatus.
  • FIG. 2 is a diagram depicting the overall configuration of a production apparatus capable of implementing the synthetic fuel production method according to this embodiment, and
  • FIG. 3 is a diagram depicting the structure of an injection pipe for performing water injection to a reaction tank of the production apparatus in FIG. 2 .
  • the synthetic fuel production apparatus 1 comprises a base oil improving tank 2 , a water refining tank 3 , a reaction accelerator injection unit 4 , a reaction tank 5 , a statically-storing tank 6 , and a product receiving tank 7 .
  • This apparatus 1 can be outlined as follows. Base fuel oil is subjected to pretreatment in the base oil improving tank 2 , and water is subjected to activation treatment in the water refining tank 3 . Then, an additive is put into a given tank from the reaction accelerator injection unit 4 . Further, the base fuel oil and the water are stirred, mixed and fused together in the reaction tank 5 .
  • a hydrocarbon-based synthetic fuel oil as a product is introduced into the product receiving tank 7 from the statically-storing tank 6 .
  • the base oil improving tank 2 is a tank for subjecting base fuel oil to pretreatment prior to the mixing.
  • the base fuel oil is supplied from another base oil tank 201 .
  • This base oil improving tank is intended to set the temperature of the base oil to a value appropriate to the mixing.
  • the base fuel oil is supplied from the base oil tank 201 to the base oil improving tank 2 . Then, the base fuel oil is heated up to a given temperature by a first heater 8 provided in the base oil improving tank 2 , and controlled at the given temperature by a first thermocouple (T).
  • T first thermocouple
  • the base fuel oil within the base oil improving tank 2 may be circulated according to a first pump such that it is extracted from the base oil improving tank 2 , and re-put into the base oil improving tank 2 via a header pipe 202 .
  • the pretreatment may include fragmenting molecules of the base fuel oil using a catalyst.
  • the water refining tank 3 is configured to perform a water activation step (activated water generation step).
  • water to be used in the method according to the present invention is soft water.
  • water is preferably supplied from a water softening device 301 .
  • This water refining tank 3 is intended to keep the temperature of the water at a value appropriate to the mixing, and fragment molecules of the water to reach an active level to form activated water including hotspots arising from microbubbles.
  • the water supplied to the water refining tank 3 is heated up to a given temperature by a second heater 8 provided in the water refining tank 3 , and controlled at the given temperature by a second thermocouple (T).
  • the level of activation can be measured using an ORP (Oxidation-Reduction Potential) meter.
  • the water refining tank 3 is provided with an ultrasonic wave generator 10 at the bottom thereof.
  • the ultrasonic wave generator 10 is operable to radiate an ultrasonic wave to the water to thereby fragment a molecular assembly of the water.
  • tourmaline or a copper ion generating material is preferably used as a catalyst 9 .
  • the catalyst 9 is kept in contact with the water, so that it is possible to improve efficiency of the activation by electrical energy radiated from the catalyst 9 .
  • an ultrasonic wave may be radiated to the catalyst 9 , such as tourmaline or a copper ion generating material, immersed in the water contained in the water refining tank 3 , to promote action of the catalyst.
  • the water within the water refining tank 3 may be circulated according to a second pump such that it is extracted toward a header pipe 302 and returned to the water refining tank 3 from the header pipe 302 .
  • the water is extracted from a lower portion of the water refining tank, and, after being pressurized by the second pump re-injected from an upper portion of the water refining tank via the header pipe 302 .
  • the activation of the water may be performed by plasma arc water treatment configured to generate a discharge between two electrodes connected to a high-voltage transformer to thereby cause dissociation and ionization of the water.
  • the plasma arc water treatment can be performed by a plasma arc water treatment unit provided in a circulation path of the water at a position between the water refining tank 3 and the second pump 11 .
  • alumina can be suitably used as the catalyst 9 .
  • electrical stimulus the application of electrical energy and the plasma arc water treatment will be collectively or generically referred to as “electrical stimulus”.
  • the reaction accelerator injection unit 4 is provided as a means to put an additive as a reaction accelerator into the water refining tank 3 or the reaction tank 5 .
  • the additive is a substance capable of decomposing hydrogen peroxide into hydrogen and oxygen, and releasing the oxygen to the atmosphere in the form of gas. Based on this function, it is possible to increase a hydrogen content ratio in a resulting synthetic fuel oil to prevent lowering of the calorific value of the synthetic fuel oil.
  • As the additive it is possible to use catalase, sodium hydroxide, an aqueous hydrogen peroxide solution or the like. The input amount of the additive needs to be finely adjusted.
  • the addition amount of catalase is preferably in the range of 0.04% to 0.05%, in terms of a ratio by weight thereof to the water. If the addition amount of catalase is less than 0.04%, it becomes impossible to sufficiently bring out an intended effect. On the other hand, if the addition amount is greater than 0.05%, it becomes impossible to ensure sufficient dissolution, leading to an increase in scum and thus deterioration in quality of a resulting synthetic fuel oil.
  • the reaction tank 5 is provided as a means to perform a stirring and mixing step and a fusion step.
  • the base fuel oil is supplied from the base oil improving tank 2 to an upper portion of a reaction tank container 13 .
  • the water is supplied from the water refining tank 3 to a lateral side of the container 13 of the reaction tank 5 via an injection pipe 14 .
  • a mixture of the base fuel oil and the water is circulated according to a third pump such that it is extracted from a discharge port 15 of the container 13 of the reaction tank 5 , and re-put into the container 13 of the reaction tank 5 via an OHR (Original Hydrodynamic Reaction) mixer 12 , a header pipe 502 and the injection pipe 14 , in a pressurized state.
  • OHR Oil Hydrodynamic Reaction
  • the OHR mixer 12 is provided as a means to efficiently mix a plurality of materials together.
  • This reaction tank 5 undergoes a pressure of about 3 to 9 atm during the fusion step, so that it is necessary to have a structure capable withstanding a higher pressure as compared to the remaining tanks.
  • the reaction tank 5 is provided with a third heater 8 at a vertically intermediate position thereof. The mixture of the base fuel oil and the water is controlled at a given temperature by the third heater 8 .
  • the statically-storing tank 6 is a tank for temporarily storing a product liquid after the fusion step.
  • impurities generated from the additive and others, such as scum are precipitated.
  • a synthetic fuel oil in which the base fuel oil and the water are perfectly fused together and the impurities are separated from each other through static storage in the statically-storing tank 6 , and the synthetic fuel oil as a supernatant is supplied to the product receiving tank 7 .
  • the additive is included in the impurities, so that the impurities are returned to the reaction tank 5 .
  • a residence time period in the statically-storing tank is preferably set to about one hour.
  • the product liquid after the fusion step contains water
  • the product liquid is subjected to phase separation in the statically-storing tank 6 to form an upper oil phase and a lower water phase, and a synthesis oil as the upper oil phase is extracted as a product into the product receiving tank 7 .
  • the product receiving tank 7 is a tank for storing the synthetic fuel oil produced as a product.
  • the produced synthetic fuel oil is supplied from the product receiving tank 7 to a product storage tank 701 , when it is accumulated to a certain amount.
  • the water treating process comprises a water activation step and an additive input step.
  • the base fuel oil treating process comprises a base oil improving step and an additive input step.
  • the activated water after undergoing the water activation step and the additive input step and the base fuel oil after undergoing the base oil improving step and the additive input step are stirred and mixed together in a stirring and mixing step, and the resulting mixture is produced as a first-order synthetic oil through a fusion step.
  • a filtration step is performed before extraction of the first-order synthetic oil
  • the water activation step is performed in the water refining tank 3 .
  • a water molecule assembly is fragmented to reach an active level.
  • By fragmenting molecules of the water to reach the active level it becomes possible to improve compatibility with molecules of the base fuel oil to thereby enable a larger amount of water to be used for producing a synthetic fuel.
  • water is put into the water refining tank 3 , and an ultrasonic wave is radiated from the ultrasonic wave generator 10 to the water, so that the water is vibrated at a high frequency to promote fragmentation of the water molecules.
  • the fragmentation of the water molecules can be promoted by alternately radiating two types of ultrasonic waves having different frequencies.
  • the two types of ultrasonic waves may have a frequency of 10 kHz to 60 kHz and a frequency of 200 kHz or more, respectively, to facilitate the molecular fragmentation.
  • an electrical stimulus is applied to the water by additionally using, as the catalyst, tourmaline or a copper ion generating material.
  • an electrical stimulus can be applied to the water to form hotspots arising from microbubbles in the water, so that it is possible to increase the degree of activation of the water.
  • the ultrasonic waves are preferably radiated such that they hit the catalytic material such as tourmaline or a copper ion generating material.
  • the level of activation caused by radiation of the ultrasonic waves can be ascertained by measuring ORP (Oxidation-Reduction Potential) (mv).
  • ORP Oxidation-Reduction Potential
  • An ORP value of the water to be obtained by radiating the ultrasonic waves thereto is preferably from 160 mV to ⁇ 790 mV, more preferably from 30 mV to ⁇ 600 mV.
  • an ORP value of normal tap water is from 700 mV to 500 mV.
  • oxygen is released from the water to improve the hydrogen content ratio in the water.
  • a reaction time period may be suitably set to about 1 hour, the same activation effect can be obtained even when it is set in the range of 20 minutes to 1 day.
  • the additive input step is intended to add the additive stored in the reaction accelerator injection unit 4 , to the water refining tank 3 or the reaction tank 5 , to thereby increase the hydrogen content ratio in the water.
  • the additive it is possible to use one or more selected from the group consisting of catalase, sodium hydroxide and an aqueous hydrogen peroxide solution.
  • the input amount of the additive needs to be finely adjusted.
  • the addition amount of catalase is preferably from 0.04% to 0.05%, in terms of a ratio by weight thereof to the water, as mentioned above. If the addition amount is less than 0.04%, it becomes impossible to sufficiently bring out an intended effect. On the other hand, if the addition amount is greater than 0.05%, it becomes impossible to ensure sufficient dissolution, leading to an increase in scum and thus deterioration in fuel quality.
  • the intended effect as an additive can be sufficiently brought out by adding it in an amount of 0.001 weight % to 0.1 weight %, with respect to 100 weight % of the water.
  • an aqueous hydrogen peroxide solution the intended effect as an additive can be sufficiently brought out by adding it in an amount of 0.001 weight % to 0.1 weight %, with respect to 100 weight % of the water.
  • the stirring and mixing step the water after being activated in the water refining tank 3 and subjected to input of the additive is mixed with the base fuel oil.
  • the base fuel oil is put into the reaction tank 5 .
  • This base fuel oil is circulated through the OHR mixer 12 of the reaction tank 5 .
  • molecules of the base fuel oil are also homogenized, so that the base fuel oil is more likely to be fused with the water.
  • the activated water is put into the reaction tank 5 from the water refining tank 3 little by little. This is intended to enable the water to be possibly homogeneously dispersed with respect to the base fuel oil.
  • the activated water supplied from the water refining tank 3 is pressurized by the second pump 11 of the water refining tank 3 , and mixed with the base fuel oil extracted from the discharge port 15 of the reaction tank 5 , and the resulting mixture is pressurized by the third pump 11 of the reaction tank 5 , and further subjected to mixing by the OHR mixer 12 .
  • the OHR mixer 12 is operated to apply a pressure of 3 atm (0.3 MPa) or more and a temperature of 40° C. to 80° C.
  • respective pressures of the second and third pumps 11 of the water refining tank 3 and the reaction tank 5 are set in a manner suited to the pressure of the OHR mixer 12
  • respective warming levels of the second and third heaters 8 of the water refining tank 3 and the reaction tank 5 are also set in a manner suited to the temperature of the OHR mixer 12 .
  • the activated water and the base fuel oil mixed by the OHR mixer 12 are re-put into the reaction tank 5 from the injection pipe 14 via the header pipe 502 .
  • Efficiency and quality of the mixing varies depending on an angle of the injection pipe 14 with respect to the reaction tank 5 , and a protruding amount of the injection pipe 14 toward an inside of the reaction tank 5 .
  • the mixture of the activated water and the base fuel oil is preferably circulated through a pipe having a nominal diameter of 15 A to 50 A at a flow rate of 20 L/min to 50 L/min.
  • a mixing time period may be set in the range of about 5 minutes to about 1 hour.
  • the fusion step is performed after completion of the input of the activated water from the water refining tank 3 into the reaction tank 5 , and achieved by circulating the mixture of the activated water and the base fuel oil through the OHR mixer 12 .
  • the pressure and the temperature during the fusion step are set, respectively, to 3 atm (0.3 MPa) or more and in the range of 40° C. to 80° C., as with the stirring and mixing step.
  • this fusion step by circulating the mixture of the activated water and the base fuel oil through the OHR mixer 12 for a sufficient period of time, it is possible to promote fusion between the activated water and the base fuel oil to produce a hydrocarbon-based synthetic fuel oil free from a risk of separation.
  • the pressure to be applied to the mixture is preferably set to 0.3 MPa (3 atm) or more.
  • the temperature may be 70° C. or less. It is most effective that the pressure and the temperature are set, respectively, to 0.9 MPa and 50° C. It is appropriate to set the reaction time period to fall within the range of 20 minutes to 60 minutes after reaching the above pressure and temperature.
  • the filtration step is intended to separate, from a fully produced synthetic fuel, scum-like substances arising from solidification of components of an enzyme used during the production process, or other components.
  • the technique using the statically-storing tank 6 is based on an idea of statically storing produced substances to separate them from each other due to a difference in specific gravity. Specifically, substances having relatively large specific gravities, such as scum, are accumulated on the bottom, and the synthetic fuel having a relatively small specific gravity gathers as a supernatant layer.
  • the synthetic fuel as the supernatant layer is send to the product receiving tank 7 to obtain a hydrocarbon-based synthetic fuel oil as a product.
  • the residence time period of the mixture in the statically-storing tank 6 is desirably set to 1 hour or more.
  • the produced substances may be enabled to pass through a filtration filter to separate scum or the like from the synthetic fuel.
  • a filtration filter it is possible to use a filter having a pore size of about 10 to 30 ⁇ m. It is preferable to enable the produced substances to pass through the filtration filter at a temperature of 40° C. or less.
  • a passing speed is preferably set in the range of about 20 to 50 L/min when a pipe has a nominal diameter of 20 A to 50 A, wherein a lower passing speed is more preferable.
  • the number of times of passing through the filtration filter may be one or more.
  • a cycle of the above steps can be repeated using the obtained first-order synthetic fuel oil as a base fuel oil to produce a second-order synthetic fuel oil.
  • the cycle can be repeated n-times (where n is an integer of 2 or more) in sequence, using a synthetic fuel oil obtained in a previous cycle, as a base fuel oil for the current cycle, to produce a n-th-order synthetic fuel oil.
  • the n-th-order synthetic fuel oil produced by the method according to the present invention has a significantly high water addition rate.
  • FIG. 3 is a diagram depicting the structure of an injection pipe for injection to the reaction tank 5 , usable in the production apparatus.
  • FIG. 3( a ) is a top plan view for explaining a positional relationship between the reaction tank 5 and the injection pipe 14 .
  • FIG. 3( b ) is a side view of the reaction tank 5 .
  • the steps for production of the synthetic fuel have been described. Among them, it is important how to circulate the mixture of the activated water and the base fuel oil, in the stirring and mixing step and the fusion step.
  • the circulation is performed by enabling the mixture extracted from the discharge port 15 of the reaction tank 5 to be re-put into the reaction tank 5 from the lateral side of the upper portion of the reaction tank 5 via the pump the OHR mixer 12 and the injection pipe 14 , in the form of a jet flow.
  • this circulation process it is ideal that all of the mixture is evenly circulated.
  • the inventor of the present invention made a study on the relationship between the reaction tank 5 and the injection pipe 14 for re-putting the mixture into the reaction tank 5 .
  • the reaction tank 5 in this example has a circular cylindrical upper portion, and a conical lower portion.
  • four injection pipes 14 are attached to a lateral wall of the upper portion of the reaction tank 5 , and arranged so as to inject the mixture of the activated water and the base fuel oil into the reaction tank 5 from four directions, respectively.
  • An angle of a longitudinal direction of each of the injection pipes 14 with respect to a diametrical line of the cylindrical upper portion of the reaction tank 5 passing through a central axis of the cylindrical upper portion of the reaction tank 5 and an attached point at which the injection pipe 14 is attached to the cylindrical portion of the reaction tank 5 is defined as an attachment angle or injection direction of the injection pipe 14 . Then, under the condition that the attachment angle is changed in the range of 0 degree to 90 degrees, a time required for the fusion and quality of a resulting synthetic fuel were checked. In FIG. 3( c ) , an injection pipe 14 a 1 is attached such that the attachment angle becomes 0 degree.
  • injection pipes 14 a 2 , 14 a 3 , 14 a 4 are attached while an angle with respect to an axis of the injection pipe 14 a 1 is gradually increased in increments of 15 degrees.
  • a test was conducted by changing the angle in increments of 15 degrees. As a result, it was ascertained that, when the angle with respect to the axis is 45 degrees, the time required for the fusion is minimized, and a resulting synthetic fuel has good quality.
  • the attachment angle of each of the injection pipes 14 is preferable set in the range of about 40 to 50 degrees with respect to the diametrical line.
  • a protruding amount of each of the injection pipes 14 toward an inside of a reaction tank 5 having a diameter of 60 cm as depicted in FIG. 3( d ) , a time required for the fusion and quality of a resulting synthetic fuel were checked.
  • an injection pipe 14 b 1 is attached such that the protruding amount becomes 0.
  • injection pipes 14 b 2 , 14 b 3 , 14 b 4 are attached while the protruding amount is gradually increased.
  • the protruding amount was increased in increments of 10 cm. As a result, it was ascertained that, when the protruding amount is 10 cm, the time required for the fusion is minimized, and a resulting synthetic fuel has good quality.
  • the attachment angle with respect to the diametrical line of the cylindrical portion of the reaction tank 5 is optimally set to 45 degrees, and the protruding amount of the injection pipe 14 toward the inside of the reaction tank 5 is optimally set to 10 cm.
  • the injection pipe 14 is disposed at a position upwardly away from a liquid surface in the reaction tank 5 , preferably by at least 8 cm, more preferably by at least 10 cm, and preferably configured to inject the mixture therefrom at a high speed.
  • FIG. 4 is a schematic diagram depicting one example of a plasma arc treatment unit usable in the production apparatus capable of implementing the method according to the present invention.
  • This plasma arc water treatment unit 20 comprises a first electrode 21 (indicated by the hexagonal dotted-line in FIG. 4 ) disposed in a central region of the unit, and a plurality of (in FIG. 4 , twelve) second electrode 22 arranged to surround the first, central, electrode 21 , wherein the first and second electrodes 21 , 22 are connected to a high-voltage transformer (not depicted).
  • a high-voltage transformer not depicted
  • the plasma arc water treatment unit 20 is installed between the water refining tank 3 and the second pump and the water from the water refining tank is sent to pass through the plasma arc water treatment unit 20 , so that it becomes possible to activate water by plasma arc water treatment.
  • Preferred examples of the plasma arc water treatment unit may include a plasma arc water treatment unit used in Ultra U-MAN manufactured by Nippon Risuiken, K. K.
  • Tourmaline produced in Estado de Tocantins, Brazil, and having a particle size of 20 mm to 80 mm was purchased from New Wave SA. Further, catalase (trade name “Leonet F-35”) was purchased from Nagase ChemteX Corporation. These tourmaline and catalase were used in the following examples.
  • microbubble means tiny air bubbles generated by a local pressure variation when the ultrasonic wave is radiated to the water.
  • Non-Patent Document 2 The research paper titled “Chemical Application of Cavitation; Sonochemistry (Application of Cavitation Induced by Ultrasound)” authored by Shinobu KODA, School of Engineering, graduate School of Engineer, Nagoya University, and presented in Journal of the Institute of Electronics, Information and Communication Engineers of JAPAN, Vol J89-A, No. 9 (2006) (Non-Patent Document 2), the research paper titled “Decomposition of Chemical Compounds by Ultrasound and Development of Sonochemical Reactor” authored by Keiji YASUDA, School of Engineering, graduate School of Engineer, Nagoya University, and presented in “THE CHEMICAL TIMES”, published by Kanto Chemical Co., In, Apr.
  • Non-Patent Document 3 the presentation material for “Monodzukuri Basic Course (34th Technical Seminar)” held on Feb. 20, 2013 at the Creation-Core Higashiosaka, by Yoshiteru MIZUKOSHI, Institute for Materials Research, Tohoku University (Non-Patent Document 4), sonochemistry based on radiating a strong ultrasonic wave to liquid to create a state in which tiny air bubbles are generated in the liquid, i.e., a cavitation state, to cause decomposition of liquid molecules is discussed in detail.
  • tiny air bubbles i.e., microbubbles
  • tiny air bubbles i.e., microbubbles
  • an ultrasonic wave expand to about several ten p.m after several cycles and subsequently rapidly contract by a quasi-adiabatic compression process.
  • the inside of each air bubble reaches a temperature of 5000 K to several tens of thousand K, and a pressure of one thousand several hundred atm.
  • This high-temperature and high-pressure local field is referred to as a hotspot, and understood as an origin of a chemical action by cavitation.
  • a first-order synthetic fuel oil was produced using A-Class heavy oil as the base oil in the following manner.
  • A-heavy oil (Class 1 (A), No. 1 heavy oil purchased from Fuji Kosan Co., Ltd.) was put in a 25 L container provided with a temperature gauge and connected to a circulation pump as with the aforementioned container.
  • the circulation pump was activated to start circulation of the A-heavy oil.
  • a preset temperature of a 3 kW line heater provided in a circulation path of the A-heavy oil was set to 40° C., and the circulation was continued for one hour after confirming that the temperature of the A-heave oil in the container reached 40° C. or more.
  • Activated water and A-heavy oil obtained in the above manner were mixed and stirred, and a resulting mixture was further fused together by applying heat and pressure thereto, in the following manner.
  • 10 L of the activated water and 10 L of the obtained A-heavy oil were put in a 25 L, open-type container having an upper portion opened to the atmosphere, wherein the container was provided with a 1 kW warming heater and a propeller-type stirrer, in addition to a temperature gauge.
  • the container was connected to a circulation pump and a blending mixer (OHR (Original Hydrodynamic Reaction) mixer manufactured by OHR Laboratory Corporation).
  • OHR Oil Hydrodynamic Reaction
  • the warming heater was powered on to enable the temperature of the liquids in the container to be maintained at 40° C. 10 mL of the same catalase as described above was added thereto. After the elapse of 40 minutes, the stirrer was powdered on to mix and stir the activated water and the A-heavy oil. Then, the circulation pump was activated and adjusted such that a supply pressure to the blending mixer becomes about 0.5 MPa, to circulate the mixture.
  • a circulation pipe for allowing the mixture to be put into the container from the circulation path therethrough in the above process was disposed at a position upwardly away from a surface of the mixture in the container by about 8 cm.
  • first-order synthetic fuel oil 2 was produced in the same manner as that in the production Case 1, and an analytical sampler was collected therefrom. The amount of the collected sample was 20 L.
  • Table 1 presents a result of componential analysis of the two types of first-order synthetic fuel oils 1 and 2 produced in the above manner.
  • Each of the first-order synthetic fuel oils 1 and 2 is obtained by mixing and fusing the activated water and the base fuel oil together at a ratio of 1:1.
  • each of the first-order synthetic fuel oils 1 and 2 is superior to the base oil, which shows that the intended effect of the present invention is brought out.
  • the present invention makes it possible to fully fuse the base fuel oil and the activated water, and produce a high-quality hydrocarbon-based synthetic fuel oil.
  • a first-order synthetic fuel oil was produced using the apparatus depicted in FIGS. 2 and 3 and using light oil as base oil.
  • 150 L of tap water was poured into the refined water container having the tourmaline-receiving section packed with the same tourmaline as that used in the production of the first-order synthetic fuel oil 1.
  • the second heater installed in the water refining tank was powered on, and a preset temperature thereof was set to 40° C.
  • 150 mL of the same catalase as that used in the production of the first-order synthetic fuel oil 1 was added thereto.
  • the second circulation pump connected to the water refining tank was activated (discharge pressure: 0.5 MPa), and the ultrasonic wave generator installed in the water refining tank was activated to radiate an ultrasonic wave (frequency: 40 kHz) to the water and the tourmaline for 60 minutes until the temperature of the water reaches 40° C., and additionally for 60 minutes after the temperature reached 40° C.
  • the ultrasonic wave generator installed in the water refining tank was activated to radiate an ultrasonic wave (frequency: 40 kHz) to the water and the tourmaline for 60 minutes until the temperature of the water reaches 40° C., and additionally for 60 minutes after the temperature reached 40° C.
  • the flow rate at a distal end of the injection pipe was set to 3.3 m/s.
  • the oxidation-reduction potential of the resulting water was measured by an ORP meter. As a result, it was 20 mV. In this way, activated water was obtained.
  • Activated water and light oil obtained in the above manner were put into the reaction tank, and mixed and stirred. Further, the activated water and the light oil were fused together by applying heat and pressure thereto. Specifically, 75 L of the light oil in the base oil improving tank and 55 L of the activated water in the water refining tank were transferred to the reaction tank (water addition rate: 42%). 62 mL of the same catalase as that used in the production of the first-order synthetic fuel oil 1 was added thereto. Then, the third heater was powered on to enable the temperature of the liquid in the container to become 40° C.
  • the third circulation pump was activated and adjusted such that a supply pressure to the blending mixer becomes about 0.5 MPa, to circulate the mixture for 60 minutes.
  • a supply pressure to the blending mixer becomes about 0.5 MPa, to circulate the mixture for 60 minutes.
  • only one of the four injection pipes was selected and used (the remaining three injection pipes were closed), and the flow rate at a distal end of the selected injection pipe was set to 2.0 m/s.
  • the selected injection pipe was attached in such a manner as to be kept from submerging in the mixture in the reaction tank. Specifically, the selected injection pipe was disposed at a position upwardly away from a surface of the mixture in the reaction tank by about 8 cm. An analytical sampler was collected from the resulting liquid. The amount of the collected sample was 114 L.
  • a first-order synthetic fuel oil 4 was produced in the same manner as that in the production of the first-order synthetic fuel oil 3.
  • the oxidation-reduction potential of the water obtained in the water refining tank was measured by an ORP meter. As a result, it was 26 mV.
  • An analytical sampler was collected from a liquid obtained in the reaction tank. An amount of the collected sample was 114 L.
  • the A-Class heavy oil (Class 1 (A), No. 1 heavy oil purchased from Fuji Kosan Co., Ltd.) was used as the base oil; the temperature of the reaction tank was set to 36° C.; the circulation time period in each of the water refining tank and the base oil improving tank was set to 90 minutes; and the addition amount of catalase was set to 230 mL and 130 mL, respectively, for the water refining tank and the reaction chamber, the production Case 5 of first-order synthetic fuel oil was carried out in the same manner as that in the production Case 3 of the first-order synthetic fuel oil.
  • the oxidation-reduction potential of the water obtained in the water refining tank was measured by an ORP meter. The measured value was 18 mV.
  • An analytical sampler was collected from a liquid obtained in the reaction tank. An amount of the collected sample was 114 L.
  • Table 2 presents a result of componential analysis of the two types of first-order synthetic fuel oils 4 and 5 produced in the above manner.
  • the sample of the first-order synthetic fuel oil 3 obtained in the above manner using light oil as base oil was subjected to qualitative analysis based on gas chromatogram-mass spectrometry (GC-MS).
  • An analytical sample was prepared by diluting the sample of the first-order synthetic fuel oil 3, with n-hexane 1000 times.
  • HP-5MS length: 30 m, inner diameter: 2.5 mm, membrane thickness: 0.25 ⁇ m
  • He was used as carrier gas.
  • An injection amount of the analytical sample was set to 1 ⁇ L, and an injection mode was set to the splitless mode.
  • An oven temperature was held at 50° C. for 3 minutes, and then after being increased from 50° C. to 100° C.
  • FIG. 5 A GC-MS chart obtained as a result of the analysis is depicted in FIG. 5 , wherein FIG. 5( a ) is a TIC chromatogram, and FIG. 5( b ) is a mass spectrum indicating peaks at about 18.4 min.
  • the sample of the first-order synthetic fuel oil 5 obtained in the above manner using A-heavy oil as base oil was also subjected to the same qualitative analysis. A result of the analysis is presented in FIG. 8 .
  • the samples of the first-order synthetic fuel oils 3 and 4 obtained in the above manner using light oil as base oil were subjected to properties test. Items and methods of the properties test were as follows.
  • JPI method JPI-5S-49
  • an amount of sludge measured was lower than 0.1 mg/100 mL as a measurement limit.
  • the sample of the first-order synthetic fuel oil 3 obtained in the above manner using light oil as base oil was subjected to the JC08 mode driving test (vehicle used: Nissan NV350, LDF-VW2E26, Vehicle mass: 1840 kg).
  • JC08 mode driving test vehicle used: Nissan NV350, LDF-VW2E26, Vehicle mass: 1840 kg.
  • commercially-available light oil JIS No. 2 was subjected to the same driving test.
  • the amount of water remaining in the water phase was 4 L. Through this process, it could be ascertained that 1 L water in the 5 L water was converted into a synthetic fuel oil. This shows that the amount of the first-order synthetic fuel oil is increased by 10% as compared to the base oil.
  • Example 1 of the present invention a second-order synthetic fuel oil was produced using the first-order synthetic fuel oil Case 6 as base oil. Specifically, 10 L of the first-order synthetic fuel oil Case 6 was conditioned through the base oil improving tank 2 , and then put into the reaction tank 5 . Simultaneously, 5 L of the activated water formed in the process described in the “Formation of Activated Water” was put into the reaction tank 5 to perform the mixing, stirring and fusion steps under the same conditions as those in the production of the first-order synthetic fuel oil 2. Subsequently, a resulting mixture was transferred to the statically-storing tank 6 , and statically stored therein for 1 hour. As a result, the mixture was separated into an upper oil phase and a lower water phase.
  • oil existing in the upper oil phase was extracted as a second-order synthetic fuel oil.
  • the amount of the extracted second-order synthetic fuel oil was 11 L.
  • the amount of water remaining in the water phase was 4 L.
  • 1 L water in the 5 L water was converted into a synthetic fuel oil. This shows that the amount of the second-order synthetic fuel oil is increased by 10% as compared to the first-order synthetic fuel oil used as base oil.
  • a third-order synthetic fuel oil was produced, using, as base oil, the second-order synthetic fuel oil obtained in the above process.
  • 10 L of the second-order synthetic fuel oil obtained in the above process was conditioned through the base oil improving tank 2 , and then put into the reaction tank 5 .
  • 5 L of the activated water formed in the process described in the “Formation of Activated Water” was put into the reaction tank 5 to perform the mixing, stirring and fusion steps under the same conditions as those in the production of the first-order synthetic fuel oil 2.
  • a resulting mixture was transferred to the statically-storing tank 6 , and statically stored therein for 1 hour.
  • the mixture was separated into an upper oil phase and a lower water phase. Then, oil existing in the upper oil phase was extracted as a third-order synthetic fuel oil. The amount of the extracted third-order synthetic fuel oil was 11 L. The amount of water remaining in the water phase was 4 L. Through this process, it could be ascertained that 1 L water in the 5 L water was converted into a synthetic fuel oil. This shows that the amount of the third-order synthetic fuel oil is increased by 10% as compared to the second-order synthetic fuel oil used as base oil.
  • the first-order synthetic fuel oil 6 and the second-order synthetic fuel oil produced in the Example 1 were subjected to calorific value measurement and component analysis.
  • a result of the measurement and analysis is presented in Table 5 in comparative manner with the commercially-available light oil used, as base oil, in the production Case 6 of the first-order synthetic fuel oil.
  • the Example 1 is one example using the first-order synthetic fuel oil Case 6 as base oil.
  • a second-order synthetic fuel oil can be produced using one of the first-order synthetic fuel oils 1 to 5, in the same manner as that in the Example 1.

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US20140305028A1 (en) * 2013-04-11 2014-10-16 Bio Hitech Energy Co. Apparatus and method for manufacturing a reformed fuel
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US20140223808A1 (en) * 2013-02-12 2014-08-14 Bio Hitech Energy Co. Method of Manufacturing a Reforming Fuel by Adding Water to a Fuel Oil and the Manufacturing Apparatus thereof
US20140305028A1 (en) * 2013-04-11 2014-10-16 Bio Hitech Energy Co. Apparatus and method for manufacturing a reformed fuel
US20180037823A1 (en) * 2016-08-02 2018-02-08 Bio Hitech Energy Co. Manufacturing apparatus and method for fuel hydrocarbon

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