WO2016159254A1 - Hydrated fuel production method and production apparatus - Google Patents

Hydrated fuel production method and production apparatus Download PDF

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Publication number
WO2016159254A1
WO2016159254A1 PCT/JP2016/060712 JP2016060712W WO2016159254A1 WO 2016159254 A1 WO2016159254 A1 WO 2016159254A1 JP 2016060712 W JP2016060712 W JP 2016060712W WO 2016159254 A1 WO2016159254 A1 WO 2016159254A1
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WIPO (PCT)
Prior art keywords
water
fuel
stirring
tank
base oil
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PCT/JP2016/060712
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French (fr)
Japanese (ja)
Inventor
青木　文男
Original Assignee
株式会社Ｔｒｉｓｔａｒｈｃｏ
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Priority to US15/563,413 priority Critical patent/US20180086997A1/en
Priority to JP2016523340A priority patent/JP6146789B2/en
Publication of WO2016159254A1 publication Critical patent/WO2016159254A1/en

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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
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/10—Liquid carbonaceous fuels containing additives
    • 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
    • C10L10/00—Use of additives to fuels or fires for particular purposes
    • C10L10/02—Use of additives to fuels or fires for particular purposes for reducing smoke development
    • 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
    • C10L1/10—Liquid carbonaceous fuels containing additives
    • C10L1/12—Inorganic compounds
    • C10L1/1233—Inorganic compounds oxygen containing compounds, e.g. oxides, hydroxides, acids and salts thereof
    • C10L1/1258—Inorganic compounds oxygen containing compounds, e.g. oxides, hydroxides, acids and salts thereof hydrogen peroxide, oxygenated 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
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/10—Liquid carbonaceous fuels containing additives
    • C10L1/14—Organic compounds
    • C10L1/30—Organic compounds compounds not mentioned before (complexes)
    • 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
    • C10L2290/38—Applying an electric field or inclusion of electrodes in the apparatus

Definitions

  • the present invention relates to a method and an apparatus for producing a hydrolyzed fuel obtained by adding water to fuel oil.
  • Hydrous fuel is a fuel that mixes water with fuel oil.
  • the fuel used is greatly reduced, and CO 2 (carbon dioxide) is reduced by the amount of fuel reduction. Since complete combustion is expected, the amount of air used for combustion can be reduced considerably. Along with this, generation of nitrogen oxides and particulate matter (PM) can be suppressed, and there is an effect of reducing the environmental load caused by the gas discharged from the boiler and the internal combustion engine.
  • water-added fuel is very useful, but in general, water and oil are difficult to fuse completely, and even when mixed, they tend to separate over time. Moreover, even if it is not impossible to perform the fusion sufficiently, it takes a very long time, and it is predicted that it is far from practical use from an economic point of view.
  • Patent Document 1 As one method for improving the efficiency of chemical fuels, conventionally, a hydrofuel technology (Patent Document 1) in which fuel oil and water are mixed and produced in the presence of a surfactant has been proposed and has become a publicly known technology. Yes. More specifically, in Patent Document 1, natural ore is brought into contact with an oil-water mixture to which oxygen is added, and at the same time, stirring and mixing are performed while applying ultrasonic vibration. A method of heating to 0 ° C. and pressurizing at a pressure of 3 atm to 1O atm is disclosed. According to this method, it is explained that a water-in-oil fuel can be obtained. Patent Document 1 states that this production method can prevent an oil-water separation phenomenon of an emulsion fuel having a hydrolysis rate of 5% or more.
  • the present invention focuses on these problems in the prior art, and a main object of the present invention is to provide a method and an apparatus for producing a hydrolyzed fuel that can solve all of these problems. Another object of the present invention is that the composition and physical characteristics are substantially the same as or close to those of the fuel base oil that is the fuel before water addition, from the viewpoint of oil-water separation. Also, it is to provide a method and an apparatus for producing a hydrated fuel capable of producing a hydrated fuel having characteristics equivalent to those of fuel base oil.
  • the method for producing a hydrolyzed fuel according to the present invention includes a water activation step of activating water molecules by applying electrical stimulation to water by a method such as application of a high voltage, and catalase as an additive to water.
  • a water activation step of activating water molecules by applying electrical stimulation to water by a method such as application of a high voltage, and catalase as an additive to water.
  • the water after the water activation step is mixed with the fuel base oil and stirred, and during the stirring and mixing step, or It includes at least a fusing step of fusing the fuel base oil and water that have undergone the step under high temperature and high pressure.
  • activate water molecules means that the water molecules are likely to undergo the reactions required in the stirring and mixing step and the fusion step described above.
  • the hydrofuel produced by the method of the present invention is substantially free of water (H 2 O) and has a composition and physical properties that are substantially the same as or close to that of the fuel base oil. It will be a thing.
  • the fuel base oil is a light oil used as a diesel fuel
  • a surprising result is obtained that the obtained hydrofuel is a light oil equivalent to the light oil that is the base oil. Since the light oil produced by the present invention does not substantially contain water (H 2 O), it has been confirmed that oil-water separation does not occur even when stored for a long period of time.
  • the fuel base oil is A heavy oil, it is possible to produce heavy oil that is substantially equivalent to or close to the A heavy oil.
  • the hydrolyzed fuel is substantially free of water (H 2 O) and is substantially the same as or close to the fuel base oil.
  • H 2 O water
  • carbon dioxide in ambient air is taken in from the liquid level of a mixture of fuel base oil and water, and the carbon dioxide is decomposed and utilized.
  • the surrounding area where the stirring and mixing process is performed is a closed space, the amount of carbon dioxide taken in from the ambient air is insufficient, but under such circumstances, carbon is added to the fuel base oil and water mixture. It was confirmed that the intended water-added fuel could be obtained by adding. Moreover, it is estimated that hydrogen required for the production
  • the water molecule is activated by the electrical stimulation given in the method of the present invention, and at least one of catalase, sodium hydroxide, and aqueous hydrogen peroxide solution is added to the water containing the activated water molecule.
  • the amount of water added to the fuel base oil is not particularly limited, but if the amount of water added to the fuel base oil becomes too large, the reaction time required for the production of the hydrofuel having the desired composition will be excessive. There is a concern that it will become impractical.
  • the inventor of the present invention has confirmed that a desired water-added fuel can be produced in a sufficiently short time even when water is mixed with fuel base oil 1 at a ratio of about 1 by volume. When the amount of water added is less than this, the desired result can be obtained in a shorter time. Therefore, in the present invention, the mixing ratio of the fuel base oil and water is preferably about 1 or less with respect to the fuel base oil 1 in terms of volume ratio.
  • the agitation and mixing step first, only the fuel base oil is charged into the agitation and mixing tank, and the water after the water activation step and the additive addition step is added and mixed in predetermined amounts while stirring. Is preferred. In this case, it is preferable to vigorously stir so as to generate a strong wave on the liquid surface in order to take carbon dioxide in the air into the liquid.
  • an apparatus having a stirring and mixing tank having a cylindrical portion, and at least one injection pipe for introducing water that has undergone a water activation step and an additive addition step into the tank by a method such as injection. It is preferable that the water jet direction of the jet pipe has a predetermined angle with respect to the diameter line of the cylindrical portion.
  • the predetermined angle is about 40 degrees to about 50 degrees, in particular about 45 degrees.
  • the predetermined angle in all the spray tubes is a specific angle in the range of about 40 degrees to about 50 degrees, for example, about 45 degrees. It is preferable to do so.
  • the discharge port of the injection pipe is positioned at least 8 cm, preferably 10 cm or more above the liquid level, and activated as a high-speed jet. It is preferable to spray water on the liquid surface.
  • the injection pipe has a projecting portion that projects into the stirring and mixing tank tank.
  • the length of the protrusion is preferably about 10 cm.
  • catalase in an additive injection step by 0.04 to 0.05% by weight with respect to water.
  • the water activated in the water activation step described above has an ORP of 160 mV to ⁇ 200 mV.
  • the water activation step maintains the tourmaline or copper ion generating material in contact with water, and the water or the tourmaline or copper ion generating material is 10 KHz to 60 KHz. Until then, two frequency ultrasonic waves of 200 KHz or higher are alternately irradiated, and water is activated by electrical energy radiated from the tourmaline or copper ions radiated from the copper ion generating material.
  • the pressure applied in the fusion step is 0.3 MPa or more, and the heating temperature is 40 ° C to 80 ° C.
  • an OHR mixer is used in the stirring and mixing step.
  • an apparatus for producing a hydrolyzed fuel is provided that mixes fuel oil and water to produce hydrous fuel.
  • This apparatus includes a water activation apparatus that activates water by applying electrical stimulation to water, and an additive injection apparatus that adds at least one of catalase, sodium hydroxide, and aqueous hydrogen peroxide as an additive to water.
  • a fusion device for fusing.
  • the water activation device may include an ultrasonic generator. This water activation device is provided with a portion for accommodating a catalyst, and the catalyst is preferably tourmaline.
  • the water activation device may also comprise a plasma arc treatment device.
  • This water activation device includes a portion for accommodating the catalyst, and the catalyst is preferably aluminum.
  • the stirring and mixing device may include an open stirring and mixing tank that is open to the atmosphere.
  • the stirring and mixing device includes an injection pipe for injecting the liquid to be stirred and mixed into the stirring and mixing tank, and the injection pipe is preferably at least 8 cm away from the liquid level in the stirring and mixing tank, more preferably at least 10 cm. It is preferable to be arranged at a different place.
  • the fusion apparatus may include an OHR mixer.
  • the hydrofuel produced by the method and apparatus of the present invention is substantially free of water (H 2 O) and is substantially the same as or close to the fuel base oil. It has a composition and a physical characteristic to do.
  • the hydrothermal fuel of the present invention has a calorific value per unit quantity equal to or higher than that of existing fuel oil, and is deteriorated after combustion, such as a combustion chamber and an exhaust pipe, as compared with existing fuel oil. And there is an effect that there is little corrosion.
  • the water-added fuel of the present invention is excellent in complete combustibility, hardly produces carbon monoxide, and achieves effects such as low carbon monoxide emission.
  • FIG. 1 is a flow diagram of a method according to an embodiment of the present invention performed using a manufacturing apparatus according to the present invention.
  • FIG. 2 is an overall configuration diagram of a manufacturing apparatus used in the method for manufacturing a water-added fuel according to the present invention
  • FIG. 3 is a structural diagram of an injection pipe for performing water injection into a reaction tank of the manufacturing apparatus according to the present invention. It is.
  • the water-added fuel production apparatus 1 is composed of a base oil improvement tank 2, a purified water tank 3, a reaction accelerator injection unit 4, a reaction tank 5, an improved oil stationary tank 6, and a product receiving tank 7. The The outline of the apparatus 1 will be described.
  • the base oil improvement tank 2 pretreatment of the fuel base oil is performed, water is activated in the purified water tank 3, and the additive is supplied from the reaction accelerator injection section 4 to a predetermined tank.
  • the reaction tank 5 the fuel base oil and water are agitated and mixed and fused, in the improved oil stationary tank 6, unnecessary residues such as scum are removed, and the product hydrolyzed fuel is introduced into the product receiving tank 7. .
  • the base oil improvement tank 2 is a tank that performs a process before the fuel oil is mixed.
  • the fuel base oil is supplied from another base oil tank 201. The purpose of this tank is to make the temperature of the oil suitable for mixing.
  • the fuel base oil After the fuel base oil is supplied from the base oil tank 201 to the base oil improvement tank 2, it is heated by the heater 8 provided in the base oil improvement tank 2, and is managed at a predetermined temperature by the thermocouple (T).
  • the fuel base oil in the base oil improvement tank 2 may be taken out from the base oil improvement tank 2 by the pump 11 and re-injected into the tank through the header pipe 202 in order to increase the uniformity of the oil temperature. Further, oil molecules may be subdivided as a pretreatment using a catalyst.
  • the purified water tank 3 performs the process of activating water.
  • the water used in the present method is preferably soft water, and therefore water is supplied from the water softening device 301.
  • the purpose of the purified water tank 3 is to maintain the temperature of water at a temperature suitable for mixing, and to subdivide the water molecules to an active level.
  • the water supplied to the purified water tank 3 is heated by a heater 8 provided in the purified water tank 3 and is controlled at a predetermined temperature by a thermocouple (T).
  • T thermocouple
  • the degree of activation can be measured by an ORP (oxidation / reduction potential) meter.
  • An ultrasonic generator 10 is provided at the bottom of the purified water tank 3, and the water molecular aggregate can be subdivided by irradiating the ultrasonic wave from the ultrasonic generator 10. At this time, it is preferable to irradiate two types of ultrasonic waves alternately. Specifically, ultrasonic waves of 10 kHz to 60 kHz and ultrasonic waves of 200 kHz or higher are alternately applied. By doing so, the efficiency of activation is improved. Furthermore, in the purified water tank 3, tourmaline and a copper ion generating material can be used as the catalyst 9.
  • the efficiency of activation can be improved by bringing the catalyst 9 into contact with water by the electric energy radiated from the catalyst 9.
  • the water may be circulated by taking out the water in the tank to the header 302 by the pump 11 and returning it to the purified water tank 3 again from the header 302 so that the activation is performed evenly. At this time, water is drawn from the bottom of the tank, pressure is applied by the pump 11, and water is re-injected from the top of the tank through the header pipe 302. By setting it as such a structure, the temperature and activation of water can be performed equally.
  • the activation of water can also be performed by a plasma arc treatment of water in which a discharge is generated between electrodes connected to a high-voltage transformer and water is dissociated and ionized by this discharge.
  • a plasma arc treatment of water in which a discharge is generated between electrodes connected to a high-voltage transformer and water is dissociated and ionized by this discharge.
  • the treatment can be performed by installing a plasma arc treatment apparatus between the purified water tank 3 and the pump 11 in the water circulation path.
  • aluminum can be used suitably as the catalyst 9.
  • electrical stimulation the above-described application of electrical energy and plasma arc treatment of water are collectively referred to as “electrical stimulation”.
  • the reaction accelerator injecting section 4 is for introducing an additive into the purified water tank 3 or the reaction tank 5 as a reaction accelerator.
  • the additive has the effect of decomposing hydrogen peroxide into hydrogen and oxygen and releasing the oxygen into the atmosphere as a gas. If it does so, the hydrogen content ratio in a water-added fuel can be increased and the fall of the emitted-heat amount can be prevented.
  • catalase, sodium hydroxide, aqueous hydrogen peroxide solution or the like is used as an additive.
  • the amount to be fed needs to be finely adjusted.
  • the amount of catalase added is preferably 0.04% to 0.05% by weight with respect to water. If the amount of catalase added is less than 0.04%, the effect is weak, and if it exceeds 0.05%, it does not dissolve sufficiently, and scum is increased on the contrary, and the quality of the fuel is lowered.
  • the reaction vessel 5 is for performing a stirring and mixing step and a fusion step.
  • the fuel base oil is supplied from the base oil improvement tank 2 to the upper part of the reaction tank container 13.
  • Water is supplied from the purified water tank 3 to the side surface of the reaction vessel container 13 through the injection pipe 14.
  • the mixture of oil and water is taken out by the pump 11 from the discharge port 15 of the reaction vessel container 13, and in a pressurized state, passes through the OHR mixer 12, passes from the header pipe 502 through the injection pipe 14, and passes through the reaction vessel container 13. Circulated inside.
  • the OHR mixer 12 mixes a plurality of substances efficiently. Since this tank applies a pressure of about 3 to 9 atm in the fusion process, it needs to have a structure that can withstand a higher pressure than other tanks.
  • the improved oil stationary tank 6 is a tank for temporarily storing the product after the fusion process. In this tank, scum generated by additives is precipitated. Hydrolyzed fuel in which oil and water are completely integrated and impurities are separated by being left in the improved oil standing tank 6, and the hydrolyzed fuel as a supernatant is supplied to the product receiving tank 7. Since the impurities include additives, the impurities are returned to the reaction vessel 5.
  • the residence time in this tank is preferably about 1 hour.
  • the product receiving tank 7 is a tank that stores the hydrolyzed fuel produced as a product.
  • the produced water-added fuel is supplied from the product receiving tank 7 to the product storage tank 701 at a certain stage.
  • This method includes an activation process, an additive charging process, a stirring and mixing process, a fusion process, and a filtration process.
  • the activation process is performed by the purified water tank 3. This process subdivides water molecules to activity levels. By subdividing the water to the active level, the affinity with the fuel base oil is improved, and more water can be used for the production of the hydrous fuel.
  • the water is vibrated at a high frequency to promote fragmentation. By having two types of ultrasonic frequencies and irradiating them alternately, subdivision of water can be promoted.
  • the frequency of the ultrasonic waves can be further subdivided by using two types of frequencies of 10 KHz to 60 KHz and 200 KHz or more.
  • electric stimulation is given to water further using tourmaline and a copper ion generation material as a catalyst.
  • electrical stimulation is given to water, and activation can be further promoted.
  • the degree of activation by irradiating with ultrasonic waves can be confirmed by measuring ORP (redox potential) (mv).
  • the ORP of water obtained by irradiating with ultrasonic waves is preferably 160 mV to -200 mV.
  • the normal tap water ORP is 700 mV to 500 mV.
  • oxygen is released and the hydrogen content ratio is improved.
  • the reaction time is suitably about 1 hour, but the effect can be obtained even from 20 minutes to 1 day.
  • the additive charging step the hydrogen content ratio of water is increased by adding the additive stored in the reaction accelerator injection unit 4 to the purified water tank 3 or the reaction tank 5.
  • the additive one or more of catalase, sodium hydroxide, and hydrogen peroxide aqueous solution are used. It is necessary to finely adjust the amount of additive added.
  • the amount of catalase added is preferably 0.04% to 0.05% by weight with respect to water. If it is less than 0.04%, the effect is weak, and if it is more than 0.05%, it does not dissolve sufficiently, so that the scum is increased and the quality of the fuel is lowered.
  • Sodium hydroxide is sufficiently effective as an additive when added in an amount of 0.001 to 0.1% by weight based on water.
  • aqueous hydrogen peroxide solution the addition of 0.001% to 0.1% by weight with respect to water can sufficiently exhibit the effect as an additive.
  • the stirring and mixing step the water after being activated in the purified water tank 3 and charged with the additive is mixed with the fuel base oil.
  • the fuel base oil is charged into the reaction tank 5.
  • This base fuel oil is circulated through the OHR mixer 12 in the reaction vessel 5.
  • the molecules of the fuel base oil are also made uniform and can be easily fused with water.
  • water is poured into the reaction tank 5 from the purified water tank 3 little by little. This is because water is dispersed as uniformly as possible in the fuel base oil.
  • the water supplied from the purified water tank 3 is pressurized by the pump 11 of the purified water tank 3, mixed with oil from the discharge port 15, pressurized by the pump 11 of the reaction tank 5, and mixed by the OHR mixer 12. .
  • the pressure of the OHR mixer 12 is preferably 3 atm (0.3 MPa) or more, and the temperature is preferably 40 ° C. to 80 ° C. Therefore, the pressure of the pump 11 of the purified water tank 3 and the reaction tank 5 is set to a pressure corresponding to that, and the heating of the heater 8 of the purified water tank 3 and the reaction tank 5 is also set to the pressure. Water and oil mixed in the OHR mixer 12 are reintroduced into the reaction tank 5 from the injection pipe 14 through the header pipe 502.
  • the efficiency and quality of mixing vary depending on the angle of the injection tube 14 with respect to the reaction tank 5 and the amount of protrusion inside the reaction tank 5.
  • the mixture of water and fuel base oil is preferably circulated through a pipe size of 15 A to 50 A at a flow rate of 20 L / min to 50 L / min.
  • the mixing time can be about 5 minutes to 1 hour.
  • the fusion process In the fusion process, the introduction of water from the purified water tank 3 to the reaction tank 5 is completed, and the fusion process is performed by circulating through the OHR mixer 12.
  • the pressure is preferably 3 atm (0.3 MPa) or more as in the stirring and mixing step, and the temperature is preferably from 40 ° C to 80 ° C.
  • the pressurizing pressure is preferably 0.3 MPa (3 atm) or higher, and the temperature is preferably 70 ° C. or higher, but higher pressurizing pressure and lower
  • the pressure of 0.9 MPa and the temperature of 50 ° C. are the most effective.
  • the reaction time is suitably 20 minutes to 60 minutes after reaching this pressure and temperature.
  • the filtration step is a step of separating a scum-like product obtained by coagulating an enzyme component and other components when the enzyme is used at the time of production from the completely produced water fuel.
  • the method using the improved oil stationary tank 6 is a method in which the product is allowed to stand and the specific gravity is separated. Scum, which has a relatively high specific gravity, accumulates at the bottom, and the water is concentrated in the upper layer because of its low specific gravity.
  • the upper layer hydrolyzed fuel is sent to the product receiving tank 7 to complete the product.
  • the residence time in the improved oil stationary tank 6 is desirably 1 hour or longer. Also, the water fuel and scum can be separated by passing through a filtration filter.
  • a filtration filter having a size of about 10 ⁇ m to 30 ⁇ m is used.
  • the temperature for passing through the filtration filter is preferably 40 ° C. or less, and the passage time is preferably about 20 L / min to 50 L / min in the pipes 20A to 50A, but the speed is more preferable.
  • count of filtration filter should just be 1 time or more.
  • FIG. 3 is a structural diagram of the injection pipe to the reaction tank of the production apparatus according to the present invention.
  • FIG. 3A is a view of the relationship between the reaction tank 5 and the injection pipe 14 as viewed from above.
  • FIG. 3B is a side view of the reaction vessel 5.
  • each process for producing the hydrolyzed fuel has been described. Among them, how to circulate the mixture of water and fuel base oil in the stirring and mixing process and the fusion process is important.
  • FIG. 3 is a structural diagram of the injection pipe to the reaction tank of the production apparatus according to the present invention.
  • FIG. 3A is a view of the relationship between the reaction tank 5 and the injection pipe 14 as viewed from above.
  • FIG. 3B is a side view of the reaction vessel 5.
  • the mixture is discharged from the discharge port 15 of the reaction tank 5 from the pump 11 and the OHR mixer 12 through the injection pipe 14 and from the upper side surface of the reaction tank 5. It is carried out by charging the reaction vessel 5 again in an injection state. In circulation, ideally all of the mixture is circulated evenly. However, if the method of recharging into the reaction vessel 5 is not appropriate, only a part of the mixture will be circulated more and the other part will not be circulated so much, or the whole will not be a uniform hydrofuel, or It takes a very long time to make it uniform.
  • the inventor of the present invention examined the relationship between the injection tube 14 for recharging the mixture into the reaction vessel 5 and the reaction vessel 5.
  • the reaction vessel 5 has a cylindrical body at the top and a cone at the bottom.
  • Four injection pipes 14 are arranged on the upper side surface, and the oil / water mixture can be injected into the reaction tank 5 from four directions as shown in FIG.
  • FIG. 3 (c) the angle in the length direction of the injection tube 14 with respect to the diameter line connecting the central axis of the cylindrical portion of the reaction vessel 5 and the attachment point where the injection tube 14 is attached to the reaction vessel 5, The mounting angle or the injection direction of the injection pipe 14 was determined.
  • the amount of protrusion of the injection tube 14 into the reaction vessel 5 having a diameter of 60 cm, the time required for fusion, and the quality of the produced hydrofuel were examined.
  • the protrusion amount when the protrusion amount is 0, it is the injection pipe 14b1.
  • the amount of protrusion was increased to 14b2, 14b3, 14b4.
  • the amount of protrusion was examined in units of 10 cm. As a result, when the protrusion amount was 10 cm, the time required for fusion was the shortest, and the quality of the produced hydrocombustion was good.
  • the mixture is injected into the reaction vessel 5 through the injection tube 14 at an angle of 45 degrees with respect to the diameter line of the cylinder, and the projection amount of the injection tube 14 into the reaction vessel 5 is optimally 10 cm. is there.
  • the projection amount of the injection tube 14 into the reaction vessel 5 is optimally 10 cm. is there.
  • a natural vortex can be created in the tank. Therefore, mixing can be performed efficiently.
  • the injection tube 14 is disposed so as to be located at least 8 cm, preferably at least 10 cm above the liquid level in the reaction vessel 5, and the mixture is injected from the injection tube 14 at a high speed.
  • FIG. 4 is a schematic diagram showing an example of a plasma arc processing apparatus that can be used as an activation apparatus of a manufacturing apparatus according to the present invention.
  • the plasma arc treatment device 20 surrounds the central electrode with an electrode 21 (shown as a hexagon in the figure) disposed at the center of the device, each connected to a high voltage transformer (not shown).
  • a plurality of (in the figure, twelve) electrodes 22 are provided. By supplying power to the electrodes, arc discharge occurs between the electrodes.
  • a plasma arc treatment apparatus 20 is installed between the purified water tank 3 and the pump 11, and water from the purified water tank is passed through the plasma arc treatment apparatus 20.
  • water can be activated by plasma arc treatment.
  • a plasma arc processing apparatus for example, a plasma arc processing apparatus used for Ultra U-MAN manufactured by Nippon Risuiken Co., Ltd. can be preferably used.
  • Example 1 A water-added fuel using A heavy oil as a base oil was produced by the following method. First, a tourmaline container with a volume of 25 liters equipped with a part for accommodating tourmaline, an ultrasonic generator (35 kHz ultrasonic transducer), and a thermometer and connected with a circulation pump (24 liters / minute ⁇ 0.5 Mpa). (Small size tourmaline imported directly from New Wave, Co., Ltd.) 3 kg and 20 liters of tap water were added. To this water, 20 ml of catalase (Leonet F-35 manufactured by Nagase ChemteX Corporation) was added. Next, the ultrasonic vibrator was activated, and water circulation was started by a circulation pump.
  • a circulation pump 24 liters / minute ⁇ 0.5 Mpa
  • the set temperature of the 3 kW line heater provided in the water circulation path was set to 40 ° C., and the circulation was continued for 1 hour from the time when it was confirmed that the temperature of the water in the container became 40 ° C. or higher. After 1 hour, the redox potential of the water in the container was measured with an ORP meter, and it was 12 mV.
  • a heavy oil (Type 1 No. 1 A heavy oil purchased from Fujikosan Co., Ltd.) was placed in a 25 liter container equipped with a thermometer and connected to a circulation pump, as in the above container. Circulation of heavy oil A was started by a circulation pump. The set temperature of the 3 kW line heater provided in the circulation path of A heavy oil was set to 40 ° C., and the circulation was continued for 1 hour from the time when it was confirmed that the temperature of the A heavy oil in the container became 40 ° C. or higher.
  • the activated water and heavy oil A obtained in this way were mixed and stirred as follows, and were further fused by applying temperature and pressure.
  • a thermometer a 1 kW heating heater and a propeller type stirrer are connected, a circulation pump is connected, and a mixing mixer (OHR mixer manufactured by OHR Fluid Engineering Laboratory Co., Ltd.) is connected to an upper part of a 25 liter 10 liters of activated water and 10 liters of the obtained heavy fuel oil A were placed in an open system container opened to the atmosphere.
  • the heater was turned on so that the temperature of the liquid in the container was maintained at 40 ° C.
  • 10 ml of the same catalase as described above was added.
  • the stirrer was turned on, and water and A heavy oil were mixed and stirred.
  • the circulating pump was operated, and the supply pressure to the mixing mixer was adjusted to be about 0.5 MPa, and the mixed liquid was circulated.
  • the circulation pipe for introducing the liquid into the container from the circulation path was positioned about 8 cm above the liquid level of the mixed liquid in the container.
  • the stirrer, the circulation pump and the heating heater were stopped.
  • the liquid (hydrolyzed fuel) thus obtained was allowed to stand for about 3 days, and a sample was taken for analysis. The amount of sample collected was 20 liters.
  • Example 2 As a base oil, a hydro fuel was produced in the same manner as in Example 1 except that a commercially available light oil (No. 2 light oil purchased from JX Energy Co., Ltd. (ENEOS)) was used instead of A heavy oil. A sample was taken. The amount of sample collected was 20 liters.
  • ENEOS JX Energy Co., Ltd.
  • Table 1 shows the component analysis results of the water fuel produced in Example 1 and Example 2 of the present invention. It is a mixture of water and oil, mixed one-on-one. For comparison, the same component analysis was performed on the A heavy oil and light oil used as the base oil. First, looking at the total calorific value and the true calorific value, it can be seen that both Example 1 and Example 2 exceed the base oil, and the effect of the present invention is obtained. Next, looking at the item of moisture, the volume% of moisture in both Example 1 and Example 2 is 0.00%. Since fuel oil and water are mixed and fused one-on-one, if sufficient fusion is not achieved, the amount of water should be detected. However, the volume% of water being 0.00% means that the fuel oil and water were completely fused and were not analyzed as water components. Thus, according to the present invention, the fuel base oil and water can be completely fused to produce a high-quality water-added fuel.
  • Example 3 The apparatus as shown in FIG.2 and FIG.3 was used, and the fuel oil was manufactured using light oil as base oil.
  • 150 liters of tap water was injected into a purified water tank filled with the same tourmaline as that used in Example 1 in a portion containing tourmaline.
  • the heater installed in the purified water tank was turned on and the temperature was set to 40 ° C.
  • 150 ml of the same catalase used in Example 1 was added.
  • the circulation pump connected to the purified water tank is operated (discharge pressure 0.5 MPa), and the ultrasonic generator installed in the purified water tank is operated to reach 40 ° C. for 60 minutes until the water temperature reaches 40 ° C.
  • ultrasonic waves (frequency: 40 kHz) were further irradiated for 60 minutes.
  • the flow velocity at the tip of the injection tube was 3.3 m / s. It was 20 mV when the oxidation reduction potential of the water obtained by the ORP meter was measured.
  • the activated water and light oil thus obtained were mixed and stirred as follows, and were further fused by applying temperature and pressure. That is, 75 liters of the base oil in the base oil improvement tank and 55 liters of the activated water in the purified water tank were transferred to the reaction tank (hydration ratio of about 42%). Here, 65 ml of the same catalase as described above was added. The heater was turned on so that the temperature of the liquid in the container was 40 ° C. After the liquid temperature reached 40 ° C., the circulation pump was operated, and the supply pressure to the mixing mixer was adjusted to be about 0.5 MPa, and the mixed liquid was circulated for 60 minutes.
  • the injection tube was not submerged in the mixed solution in the reaction vessel. Specifically, the injection tube was arranged to be about 8 cm above the liquid level of the mixed solution in the reaction tank. A sample was taken from the resulting liquid for analysis. The amount of sample collected was 114 liters.
  • Example 4 While the temperatures of the purified water tank, the base oil improvement tank, and the reaction tank are higher than those in Example 3, they are set to 42 ° C., 41 ° C., and 44 ° C., respectively, while the circulation time in the purified water tank and the base oil improvement tank was made in the same manner as in Example 3 except that the fuel was reduced to half of that in Example 3 (that is, 60 minutes). In addition, it was 26 mV when the oxidation reduction potential of the water obtained with the ORP meter in the purified water tank was measured. A sample was taken from the liquid obtained in the reaction vessel for analysis. The amount of sample collected was 114 liters.
  • Example 5 While using A heavy oil (type 1 No. 1 A heavy oil purchased from Fujikosan Co., Ltd.) as the base oil and setting the reaction tank temperature to 36 ° C, the circulation time in the refined water tank and the base oil improvement tank is both 90
  • the hydrolyzed fuel was produced in the same manner as in Example 3 except that the amount of catalase added to the purified water tank and the reaction tank was 230 ml and 130 ml, respectively. In addition, it was 18 mV when the redox potential of the water obtained in the purified water tank was measured with the ORP meter. A sample was taken from the liquid obtained in the reaction vessel for analysis. The amount of sample collected was 114 liters.
  • Table 2 shows the component analysis results of the water fuel produced in Example 4 and Example 5 of the present invention.
  • FIG. (A) is a TIC chromatogram
  • (b) is a mass spectrum of a peak around 18.4 minutes.
  • the same qualitative analysis was performed for the sample of the hydrolyzed fuel obtained in Example 4.
  • the results are shown in FIG.
  • the same qualitative analysis was performed on light oil used as the fuel base oil.
  • FIG. 5 and FIG. 6 are compared with FIG. 7, the components having a large number of carbon atoms (those larger than C19) tend to decrease compared to the base oil, but were obtained in Example 3 and Example 4. It was confirmed that the component composition of the water fuel was in good agreement with the base oil.
  • Example 3 and Example 4 the property test was conducted on the samples of the hydrofuel obtained by the method of the present invention using light oil as the base oil.
  • the property test items and methods were as follows. ⁇ Density (vibration type 15 °C): JIS K2249 ⁇ Kinematic viscosity (30 °C): JIS K2283 ⁇ Nitrogen quantitative analysis: JIS K2609 ⁇ Sulfur content (ultraviolet fluorescence method): JIS K2541-6 ⁇ Oxygen content: ASTM D5622 -Light oil composition analysis (JPI method): JPI-5S-49 For comparison, the same property test was performed on light oil used as base oil. The results are shown in Table 3.
  • the water content obtained by the method of the present invention has a reduced aromatic content and an increased saturated content compared to the base oil.
  • a light oil with a small aromatic content and a high saturation content is desirable from the viewpoints of efficiency, toxic content of exhaust gas, and reduction of PM.
  • oxidation stability test of water fuel An oxidation stability test (test method: ASTM D2274) was conducted on the hydrofuel samples obtained by the method of the present invention using light oil as base oil in Example 3 and Example 4. For comparison, the same oxidative stability test was performed on light oil used as the base oil. The measured amount of sludge was below the measurement limit of 0.1 mg / 100 ml for any sample.
  • Example 3 [Running test with water fuel] A JC08 mode running test was conducted on the hydrofuel obtained by the method of the present invention using light oil as a fuel base oil in Example 3 (vehicle used: Nissan Motor NV350 model LDF-VW2E26 weight 1840 kg). For comparison, a similar running test was performed on a commercially available light oil (JIS No. 2). The results are shown in Table 4. For reference, emission control values are also shown. From Table 4, it is noted that the hydrofuel obtained by the method of the present invention has a particularly low CO 2 emission compared to commercially available light oil. The hydrous fuel obtained in Example 3 is 42% by volume derived from water.

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Abstract

Provided are a hydrated fuel production method and production apparatus capable of producing a hydrated fuel having substantially or approximately the same composition and physical properties in comparison to the fuel-source oil, which is the fuel before hydration, and also having properties similar to the fuel-source oil in terms of oil-water separation. The hydrated fuel production method comprises at least: a water activation step for activating the molecules of water by applying electrical stimulation to the water by using a method such as application of high-voltage electricity; a stirring/mixing step for mixing and stirring the fuel-source oil with the water that has undergone the water activation step, while adding, as an additive to the water, at least one of catalase, sodium hydroxide and aqueous hydrogen peroxide solution; and a fusion step of fusing the fuel-source oil and the water, at a high temperature and under high pressure, during the stirring/mixing step, or after having undergone said step.

Description

加水燃料の製造方法及び製造装置Hydrolyzed fuel production method and production apparatus
　本発明は、燃料油に水を加えた加水燃料の製造方法及び装置に関する。 The present invention relates to a method and an apparatus for producing a hydrolyzed fuel obtained by adding water to fuel oil.
　世界的に環境問題が重要課題となって久しい近年、対応案として、太陽光や風力発電などの技術開発が盛んに進められている。しかし、このような再生可能エネルギへ完全に移行できるようになるまでの間、枯渇化の問題を含む従来の化石燃料を大切に使用し、エネルギ損失が少ない内燃機関や燃焼施設・設備の開発、更には発熱や燃焼特性の優れた化石燃料自体を改善するなど、多方面からの技術開発を並行して進めて行く必要があり、その一つとして、燃料油に水を混合する方法の開発が進められている。 In recent years, environmental problems have become an important issue globally, and technological developments such as solar power and wind power generation have been actively promoted as countermeasures. However, until it becomes possible to completely shift to such renewable energy, the conventional fossil fuel including the problem of depletion is carefully used, and development of internal combustion engines and combustion facilities / equipment with low energy loss, Furthermore, it is necessary to proceed with technological development from various aspects such as fossil fuels with excellent heat generation and combustion characteristics. One of them is the development of a method for mixing water with fuel oil. It is being advanced.
　加水燃料とは、燃料油に水を混合するもので、使用燃料が大幅に削減され、燃料が削減された分だけＣＯ2（二酸化炭素）が削減されるので環境に良い燃料とされる。完全燃焼が期待されるので、燃焼に使用される空気量が相当量削減できる。それに伴い、窒素酸化物や粒子状物質（PM）の発生も抑制でき、ボイラーや内燃機関が排出するガスがもたらす環境負荷を低減させる効果がある。
　このように、加水燃料は、大変有用なものであるが、一般的に、水と油は完全な融合が難しく、混合しても時間が経過すると分離してしまう傾向がある。また、融合を十分に行うことが不可能ではないとしても、それには非常に時間がかかり、経済的観点から、実用化には程遠いと予測される。
　そのため、水と燃料油を完全に融合させ、時間が経過しても分離することがない加水燃料を製造できるような、短時間で水と燃料油の融合処理を行うことができる技術が望まれている。 Hydrous fuel is a fuel that mixes water with fuel oil. The fuel used is greatly reduced, and CO 2 (carbon dioxide) is reduced by the amount of fuel reduction. Since complete combustion is expected, the amount of air used for combustion can be reduced considerably. Along with this, generation of nitrogen oxides and particulate matter (PM) can be suppressed, and there is an effect of reducing the environmental load caused by the gas discharged from the boiler and the internal combustion engine.
As described above, water-added fuel is very useful, but in general, water and oil are difficult to fuse completely, and even when mixed, they tend to separate over time. Moreover, even if it is not impossible to perform the fusion sufficiently, it takes a very long time, and it is predicted that it is far from practical use from an economic point of view.
Therefore, there is a demand for a technique capable of performing a fusion process of water and fuel oil in a short time so that water and fuel oil can be completely fused and a hydrolyzed fuel that does not separate even after a lapse of time can be produced. ing.
　化学燃料の効率化の一手法として、従来から、燃料油と水とを界面活性剤の存在のもとで混合して生成する加水燃料技術（特許文献１）が提案され、公知技術となっている。より詳しく述べると、特許文献１は、酸素を添加した油水混合物に天然鉱石を接触させ、同時に超音波振動を与えながら攪拌混合し、さらに撹拌混合された燃料油と水の混合物を3O℃～15O℃に加熱し、かつ、気圧3気圧～1O気圧で加庄する方法を開示するもので、この方法によれば、エマルジョン状態の加水燃料が得られる、と説明されている。特許文献１においては、この製造方法により、加水化率5O%以上のエマルジヨン燃料の油水分離現象を防止できる、と述べられている。
　しかしながら、この製造方法では、得られるエマルジョン燃料が水（Ｈ2Ｏ）を含む組成であるため、油水分離現象を防止できる期間に限度があり、２～３ヶ月を経過すると油水分離現象が生じる可能性がある。また、加水燃料の透明度も油の透明度と比較して低い値となる傾向がある。そのため、特許文献１に教示された加水燃料の製造方法は、上述した問題の解決策として、満足できるものではない。 As one method for improving the efficiency of chemical fuels, conventionally, a hydrofuel technology (Patent Document 1) in which fuel oil and water are mixed and produced in the presence of a surfactant has been proposed and has become a publicly known technology. Yes. More specifically, in Patent Document 1, natural ore is brought into contact with an oil-water mixture to which oxygen is added, and at the same time, stirring and mixing are performed while applying ultrasonic vibration. A method of heating to 0 ° C. and pressurizing at a pressure of 3 atm to 1O atm is disclosed. According to this method, it is explained that a water-in-oil fuel can be obtained. Patent Document 1 states that this production method can prevent an oil-water separation phenomenon of an emulsion fuel having a hydrolysis rate of 5% or more.
However, in this production method, since the obtained emulsion fuel has a composition containing water (H 2 O), there is a limit to the period in which the oil-water separation phenomenon can be prevented, and the oil-water separation phenomenon may occur after a few months. There is sex. In addition, the transparency of the water fuel tends to be lower than that of the oil. For this reason, the method for producing a hydrolyzed fuel taught in Patent Document 1 is not satisfactory as a solution to the above-described problem.
特許第4682287号Patent No. 4682287
　本発明は、従来技術におけるこれらの問題に着目し、これらの問題をすべて解決できる加水燃料の製造方法及び装置を提供することを主目的とする。
　本発明の他の目的は、水添加前の燃料である燃料元油と対比して、組成及び物理的特性が実質的に同じであるか、又はこれに近似しており、油水分離の観点からも燃料元油と同等の特性を備えた加水燃料を製造することができる、加水燃料の製造方法及び製造装置を提供することである。 The present invention focuses on these problems in the prior art, and a main object of the present invention is to provide a method and an apparatus for producing a hydrolyzed fuel that can solve all of these problems.
Another object of the present invention is that the composition and physical characteristics are substantially the same as or close to those of the fuel base oil that is the fuel before water addition, from the viewpoint of oil-water separation. Also, it is to provide a method and an apparatus for producing a hydrated fuel capable of producing a hydrated fuel having characteristics equivalent to those of fuel base oil.
　本発明に係る加水燃料の製造方法は、水に対して、高電圧の印加等の方法により電気的刺激を与えて水の分子を活性化させる水活性化工程と、水に添加剤として、カタラーゼ、水酸化ナトリウム、過酸化水素水溶液の少なくとも一つを添加した状態で、該水活性化工程を経た水を、燃料元油と混合し攪拌する攪拌混合工程と、該攪拌混合工程中における、又は該工程を経た燃料元油と水を、高温及び高圧のもとで融合させる融合工程とを、少なくとも含むことを特徴とする。ここで、「水の分子を活性化させる」とは、水分子が、上述の撹拌混合工程及び融合工程において必要とされる反応を生じ易い状態になるようにすることを意味する。
　本発明の方法により製造された加水燃料は、水（Ｈ2Ｏ）を実質的に含まず、かつ、燃料元油と実質的に同一であるか、これに近似する組成及び物理的特性を有するものとなる。例えば、燃料元油がディーゼル燃料として使用される軽油である場合には、得られる加水燃料は、元油である軽油と同等の軽油となる、という驚くべき結果が得られる。本発明により製造される軽油は、実質的に水（Ｈ2Ｏ）を含まないので、長期間にわたり保存しても油水分離を生じないことが確認された。
　同様に、本発明の方法によれば、燃料元油がＡ重油である場合には、該Ａ重油と実質的に同等か、これに近似する重油を製造することができる。
　燃料元油に水を加えたにも拘わらず、加水燃料が、水（Ｈ2Ｏ）を実質的に含まず、かつ、燃料元油と実質的に同一であるか、これに近似する組成及び物理的特性を有するものとなるようにするためには、可燃成分である炭化水素を生成するための炭素を外部から取り入れることが必要になる。特定の理論に拘泥する趣旨ではないが、本発明の方法においては、燃料元油と水の混合物の液面から周囲空気中の二酸化炭素を取り込み、該二酸化炭素を分解してその炭素を利用することにより、加水燃料の生成のための反応に必要とされる炭素の少なくとも大部分を得ているものと推測される。撹拌混合工程が行われる周囲が閉空間である場合には、周囲空気中から取り込まれる二酸化炭素の量が不足するが、このような状況のもとでは、燃料元油と水の混合物に炭素を加えることにより意図する加水燃料が得られることが確認できた。
　また、可燃成分である炭化水素の生成に必要な水素は、活性化された水分子の分解により得られるものと推測される。水分子は、本発明の方法において与えられる電気的刺激により活性化されており、このように活性化された水分子を含む水に、カタラーゼ、水酸化ナトリウム、過酸化水素水溶液の少なくとも一つを添加した状態で、撹拌することにより、反応に必要な水素が得られることが確認されている。
　燃料元油に添加される水の量は、特に限界はないと考えられるが、燃料元油に対する水の添加量が多くなり過ぎると、所望の組成を有する加水燃料の生成に要する反応時間が過大になり、実用的ではなくなることが懸念される。本発明の発明者は、体積比で、燃料元油１に対し水を約１の割合で混合した場合にも、十分に短い時間で所望の加水燃料を生成できることを確認した。水の添加量がこれよりも少ない場合には、より短い時間で所望の結果を得ることができる。したがって、本発明において、燃料元油と水の混合割合は、体積比で、燃料元油１に対し、水は約１以下とすることが好ましい。 The method for producing a hydrolyzed fuel according to the present invention includes a water activation step of activating water molecules by applying electrical stimulation to water by a method such as application of a high voltage, and catalase as an additive to water. In the state where at least one of sodium hydroxide and hydrogen peroxide aqueous solution is added, the water after the water activation step is mixed with the fuel base oil and stirred, and during the stirring and mixing step, or It includes at least a fusing step of fusing the fuel base oil and water that have undergone the step under high temperature and high pressure. Here, “activate water molecules” means that the water molecules are likely to undergo the reactions required in the stirring and mixing step and the fusion step described above.
The hydrofuel produced by the method of the present invention is substantially free of water (H 2 O) and has a composition and physical properties that are substantially the same as or close to that of the fuel base oil. It will be a thing. For example, when the fuel base oil is a light oil used as a diesel fuel, a surprising result is obtained that the obtained hydrofuel is a light oil equivalent to the light oil that is the base oil. Since the light oil produced by the present invention does not substantially contain water (H 2 O), it has been confirmed that oil-water separation does not occur even when stored for a long period of time.
Similarly, according to the method of the present invention, when the fuel base oil is A heavy oil, it is possible to produce heavy oil that is substantially equivalent to or close to the A heavy oil.
Despite the addition of water to the fuel base oil, the hydrolyzed fuel is substantially free of water (H 2 O) and is substantially the same as or close to the fuel base oil. In order to achieve physical properties, it is necessary to incorporate carbon from the outside to generate hydrocarbons that are combustible components. Although not intended to be bound by a specific theory, in the method of the present invention, carbon dioxide in ambient air is taken in from the liquid level of a mixture of fuel base oil and water, and the carbon dioxide is decomposed and utilized. Thus, it is presumed that at least most of the carbon required for the reaction for the production of the hydrofuel is obtained. If the surrounding area where the stirring and mixing process is performed is a closed space, the amount of carbon dioxide taken in from the ambient air is insufficient, but under such circumstances, carbon is added to the fuel base oil and water mixture. It was confirmed that the intended water-added fuel could be obtained by adding.
Moreover, it is estimated that hydrogen required for the production | generation of the hydrocarbon which is a combustible component is obtained by decomposition | disassembly of the activated water molecule. The water molecule is activated by the electrical stimulation given in the method of the present invention, and at least one of catalase, sodium hydroxide, and aqueous hydrogen peroxide solution is added to the water containing the activated water molecule. It has been confirmed that hydrogen necessary for the reaction can be obtained by stirring in the added state.
The amount of water added to the fuel base oil is not particularly limited, but if the amount of water added to the fuel base oil becomes too large, the reaction time required for the production of the hydrofuel having the desired composition will be excessive. There is a concern that it will become impractical. The inventor of the present invention has confirmed that a desired water-added fuel can be produced in a sufficiently short time even when water is mixed with fuel base oil 1 at a ratio of about 1 by volume. When the amount of water added is less than this, the desired result can be obtained in a shorter time. Therefore, in the present invention, the mixing ratio of the fuel base oil and water is preferably about 1 or less with respect to the fuel base oil 1 in terms of volume ratio.
　本発明の方法においては、攪拌混合工程において、まず、燃料元油のみを攪拌混合タンクに投入し、攪拌しながら、水活性化工程と添加剤投入工程を経た水を所定量ずつ添加混合することが好ましい。この場合、液面に強い波立ちを生じるように激しく撹拌することが、空気中の二酸化炭素を液中に取り込むために好ましい。 In the method of the present invention, in the agitation and mixing step, first, only the fuel base oil is charged into the agitation and mixing tank, and the water after the water activation step and the additive addition step is added and mixed in predetermined amounts while stirring. Is preferred. In this case, it is preferable to vigorously stir so as to generate a strong wave on the liquid surface in order to take carbon dioxide in the air into the liquid.
　本発明の方法においては、円筒部分を持つ攪拌混合タンクと、水活性化工程と添加剤投入工程とを経た水を該タンク内に噴射等の手法により投入する少なくとも一つの噴射管とを有する装置を使用し、該噴射管による水の噴射方向は、該円筒部分の直径線に対して所定の角度を持つようにすることが好ましい。 In the method of the present invention, an apparatus having a stirring and mixing tank having a cylindrical portion, and at least one injection pipe for introducing water that has undergone a water activation step and an additive addition step into the tank by a method such as injection. It is preferable that the water jet direction of the jet pipe has a predetermined angle with respect to the diameter line of the cylindrical portion.
　円筒部分を持つ攪拌混合タンクに少なくとも一つの噴射管を備えた装置を使用する上記態様による本発明の方法においては、上記の所定の角度は、約４０度ないし約５０度、特に約４５度であることが好ましく、複数の噴射管が備えられる場合には、すべての噴射管における上記の所定の角度が、約４０度ないし約５０度の範囲内の特定の角度、例えば、約４５度であるようにすることが好ましい。撹拌混合タンク中の液面に上述した強い波立ちを生じさせるためには、噴射管の吐出口は、液面から少なくとも８ｃｍ、好ましくは１０ｃｍ又はそれ以上、上方に位置させ、高速噴流として活性化された水を液面に噴射することが好ましい。 In the method of the invention according to the above embodiment using an apparatus with at least one injection tube in a stirred mixing tank having a cylindrical portion, the predetermined angle is about 40 degrees to about 50 degrees, in particular about 45 degrees. Preferably, when multiple spray tubes are provided, the predetermined angle in all the spray tubes is a specific angle in the range of about 40 degrees to about 50 degrees, for example, about 45 degrees. It is preferable to do so. In order to generate the above-described strong wave on the liquid level in the stirring and mixing tank, the discharge port of the injection pipe is positioned at least 8 cm, preferably 10 cm or more above the liquid level, and activated as a high-speed jet. It is preferable to spray water on the liquid surface.
　本発明の上記態様においては、該噴射管は、攪拌混合タンクタンクの内部に突出する突出部を持つ構成にすることが好ましい。 In the above aspect of the present invention, it is preferable that the injection pipe has a projecting portion that projects into the stirring and mixing tank tank.
　この場合において、該突出部の長さは、約１０ｃｍとすることが好ましい。 In this case, the length of the protrusion is preferably about 10 cm.
　本発明の一態様においては、添加剤噴射工程において、カタラーゼを、水に対する重量比で０．０４から０．０５％添加することが好ましい。 In one aspect of the present invention, it is preferable to add catalase in an additive injection step by 0.04 to 0.05% by weight with respect to water.
　本発明のさらに他の態様においては、上述した水活性化工程において活性化された水は、そのＯＲＰが１６０ｍＶから－２００ｍＶとなるようにすることが好ましい。 In still another embodiment of the present invention, it is preferable that the water activated in the water activation step described above has an ORP of 160 mV to −200 mV.
　本発明の好ましい態様においては、水活性化工程は、トルマリン又は銅イオン発生材料を水に接触させた状態に保持し、水に対して、或いは、該トルマリン又は銅イオン発生材料に、１０ＫＨｚから６０ＫＨｚまでと、２００ＫＨｚ以上の２つの周波数超音波を交互に照射して、該トルマリンから放射される電気エネルギ又は該銅イオン発生材料から放射される銅イオンにより水を活性化することにより行われる。 In a preferred embodiment of the present invention, the water activation step maintains the tourmaline or copper ion generating material in contact with water, and the water or the tourmaline or copper ion generating material is 10 KHz to 60 KHz. Until then, two frequency ultrasonic waves of 200 KHz or higher are alternately irradiated, and water is activated by electrical energy radiated from the tourmaline or copper ions radiated from the copper ion generating material.
　本発明の更に好ましい態様においては、融合工程における加圧圧力を０．３ＭＰａ以上とし、加熱温度を４０℃から８０℃までの発明にとする。 In a further preferred embodiment of the present invention, the pressure applied in the fusion step is 0.3 MPa or more, and the heating temperature is 40 ° C to 80 ° C.
　本発明の更に好ましい態様においては、攪拌混合工程において、ＯＨＲミキサを用いる。
　さらに、本発明の他の態様においては、燃料油と水とを混合して加水燃料を生成する加水燃料の製造装置が提供される。この装置は、水に電気的刺激を与えて水を活性化する水活性化装置と、水に添加剤として、カタラーゼ、水酸化ナトリウム、過酸化水素水溶液の少なくとも一つを添加する添加剤噴射装置と、燃料元油と、水活性化装置及び添加剤噴射装置を経た水とを混合し攪拌する攪拌混合装置と、該攪拌混合装置を経た燃料元油と水の混合物を、高温及び高圧のもとで融合させる融合装置とを備えたものである。
　本発明の製造装置において、水活性化装置は、超音波発生装置を備えるものとすることができる。
　この水活性化装置は、触媒を収容する部分を備え、触媒はトルマリンとするのが好ましい。
　水活性化装置はまた、プラズマアーク処理装置を備えるものとすることができる。
　この水活性化装置は、触媒を収容する部分を備え、触媒はアルミニウムとするのが好ましい。
　本発明の製造装置において、攪拌混合装置は、大気に開放した開放系の攪拌混合タンクを備えるものとすることができる。
　この攪拌混合装置は、攪拌混合すべき液体を攪拌混合タンクに噴射する噴射管を備え、噴射管は、攪拌混合タンク中の液面から上方に、好ましくは少なくとも８ｃｍ、より好ましくは、少なくとも１０ｃｍ離れた場所に配置されているのが好ましい。
　本発明の製造装置において、融合装置は、ＯＨＲミキサを備えるものとすることができる。 In a further preferred embodiment of the present invention, an OHR mixer is used in the stirring and mixing step.
Furthermore, in another aspect of the present invention, an apparatus for producing a hydrolyzed fuel is provided that mixes fuel oil and water to produce hydrous fuel. This apparatus includes a water activation apparatus that activates water by applying electrical stimulation to water, and an additive injection apparatus that adds at least one of catalase, sodium hydroxide, and aqueous hydrogen peroxide as an additive to water. A mixture of fuel base oil and water that has passed through a water activation device and an additive injection device and stirred, and a mixture of fuel base oil and water that has passed through the stirring and mixing device at a high temperature and high pressure. And a fusion device for fusing.
In the production apparatus of the present invention, the water activation device may include an ultrasonic generator.
This water activation device is provided with a portion for accommodating a catalyst, and the catalyst is preferably tourmaline.
The water activation device may also comprise a plasma arc treatment device.
This water activation device includes a portion for accommodating the catalyst, and the catalyst is preferably aluminum.
In the production apparatus of the present invention, the stirring and mixing device may include an open stirring and mixing tank that is open to the atmosphere.
The stirring and mixing device includes an injection pipe for injecting the liquid to be stirred and mixed into the stirring and mixing tank, and the injection pipe is preferably at least 8 cm away from the liquid level in the stirring and mixing tank, more preferably at least 10 cm. It is preferable to be arranged at a different place.
In the production apparatus of the present invention, the fusion apparatus may include an OHR mixer.
　本発明によれば、上述した方法及び装置の構成により、合成された後には水と油に分離され難いか、又は分離される恐れが殆どない加水燃料を得ることができる。また、効率よく加水燃料を生成することができる。上述したように、本発明の方法及び装置により製造された加水燃料は、水（Ｈ2Ｏ）を実質的に含まず、かつ、燃料元油と実質的に同一であるか、又はこれに近似する組成及び物理的特性を有するものとなる。
　また、本発明の加水燃料は、既存の燃料油と単位分量当たりの発熱量が同等又はそれ以上であり、かつ、既存の燃料油と比較して、燃焼後の燃焼室、排気管等の劣化や腐食が少ないといった効果がある。さらに、本発明の加水燃料は、完全燃焼性に優れ、一酸化炭素が生成されにくく、また一酸化炭素の排出量も少ないなど、といった効果が達成される。 According to the present invention, it is possible to obtain a water-added fuel that is hardly separated into water and oil after synthesis or hardly separated after the synthesis by the above-described method and apparatus configuration. Further, it is possible to efficiently produce the water fuel. As described above, the hydrofuel produced by the method and apparatus of the present invention is substantially free of water (H 2 O) and is substantially the same as or close to the fuel base oil. It has a composition and a physical characteristic to do.
In addition, the hydrothermal fuel of the present invention has a calorific value per unit quantity equal to or higher than that of existing fuel oil, and is deteriorated after combustion, such as a combustion chamber and an exhaust pipe, as compared with existing fuel oil. And there is an effect that there is little corrosion. Further, the water-added fuel of the present invention is excellent in complete combustibility, hardly produces carbon monoxide, and achieves effects such as low carbon monoxide emission.
本発明に係る加水燃料の製造方法の工程図である。It is process drawing of the manufacturing method of the water fuel which concerns on this invention. 本発明に係る加水燃料の製造方法に用いる製造装置の全体構成図である。It is a whole block diagram of the manufacturing apparatus used for the manufacturing method of the water fuel which concerns on this invention. 本発明に係る製造装置に使用し得る撹拌装置の反応槽への噴射管の構造図である。It is a block diagram of the injection pipe to the reaction tank of the stirring apparatus which can be used for the manufacturing apparatus which concerns on this invention. 本発明に係る製造装置に使用し得るイオン化装置の一例の概略図である。It is the schematic of an example of the ionization apparatus which can be used for the manufacturing apparatus which concerns on this invention. 本発明に係る方法により軽油を元油として得られた加水燃料についてのＧＣ－ＭＳ分析の結果を示すチャートである。3 is a chart showing the results of GC-MS analysis of a hydrofuel obtained by using the method according to the present invention with light oil as a base oil. 本発明に係る方法により軽油を元油として得られた他の加水燃料についてのＧＣ－ＭＳ分析の結果を示すチャートである。It is a chart which shows the result of the GC-MS analysis about the other hydrofuel obtained by using the light oil as the base oil by the method according to the present invention. 元油として使用した軽油についてのＧＣ－ＭＳ分析の結果を示すチャートである。It is a chart which shows the result of GC-MS analysis about the light oil used as base oil. 本発明に係る方法によりＡ重油を元油として得られた他の加水燃料についてのＧＣ－ＭＳ分析の結果を示すチャートである。It is a chart which shows the result of the GC-MS analysis about the other hydrofuel obtained by using the heavy oil A as the base oil by the method according to the present invention. 元油として使用したＡ重油についてのＧＣ－ＭＳ分析の結果を示すチャートである。It is a chart which shows the result of GC-MS analysis about A heavy oil used as base oil.
　本発明による加水燃料の製造方法について、以下に実施形態を図面に基づいて説明する。
　なお、本実施例で示される加水燃料の製造方法の全体的な構成及び各細部の構成、数値は、下記に述べる実施形態及び実施例に限定されるものではなく、本発明の技術的思想の範囲内、即ち、同一の作用効果を発揮できる形状及び寸法の範囲内で変更することができるものである。 DESCRIPTION OF EMBODIMENTS Embodiments of a method for producing a water fuel according to the present invention will be described below with reference to the drawings.
It should be noted that the overall structure of the method for producing a hydrolyzed fuel shown in the present example, the structure of each detail, and the numerical values are not limited to the embodiments and examples described below, but are based on the technical idea of the present invention. It can be changed within the range, that is, within the range of the shape and size that can exhibit the same effect.
　図１、図２、及び図３に従って、本発明の実施形態を説明する。図１は、本発明に係る製造装置を用いて遂行される本発明の一実施形態による方法のフロー図である。図２は、本発明に係る加水燃料の製造方法に用いる製造装置の全体構成図であり、図３は、本発明に係る製造装置の反応槽への水噴射を行うための噴射管の構造図である。
　本発明の一実施形態において、加水燃料製造装置１は、元油改善槽２、精製水槽３、反応促進剤注入部４、反応槽５、改善油静置槽６、及び製品受槽７から構成される。この装置１の概要を説明すると、元油改善槽２で、燃料元油の前処理を行い、精製水槽３で水の活性化を行い、反応促進剤注入部４から添加剤を所定の槽に投入し、反応槽５で燃料元油と水の攪拌混合及び融合を行い、改善油静置槽６でスカムなどの不要な残留物を除去し、製品受槽７に製品である加水燃料を導入する。
　元油改善槽２は、燃料油を混合する前の処理を行う槽である。燃料元油は、別の元油槽２０１から供給される。この槽は、油の温度を混合に適した温度にすることを目的とするものである。燃料元油は、元油槽２０１から元油改善槽２に供給された後、該元油改善槽２に設けられたヒータ８によって加熱され、熱電対（Ｔ）によって所定の温度に管理される。
　元油改善槽２内の燃料元油は、油温の均一度を高めるために、ポンプ１１により該元油改善槽２から取出し、ヘッダ管２０２を通して槽内に再投入してもよい。また、触媒を用いて、前処理として、油の分子を細分化してもよい。 The embodiment of the present invention will be described with reference to FIGS. 1, 2, and 3. FIG. 1 is a flow diagram of a method according to an embodiment of the present invention performed using a manufacturing apparatus according to the present invention. FIG. 2 is an overall configuration diagram of a manufacturing apparatus used in the method for manufacturing a water-added fuel according to the present invention, and FIG. 3 is a structural diagram of an injection pipe for performing water injection into a reaction tank of the manufacturing apparatus according to the present invention. It is.
In one embodiment of the present invention, the water-added fuel production apparatus 1 is composed of a base oil improvement tank 2, a purified water tank 3, a reaction accelerator injection unit 4, a reaction tank 5, an improved oil stationary tank 6, and a product receiving tank 7. The The outline of the apparatus 1 will be described. In the base oil improvement tank 2, pretreatment of the fuel base oil is performed, water is activated in the purified water tank 3, and the additive is supplied from the reaction accelerator injection section 4 to a predetermined tank. In the reaction tank 5, the fuel base oil and water are agitated and mixed and fused, in the improved oil stationary tank 6, unnecessary residues such as scum are removed, and the product hydrolyzed fuel is introduced into the product receiving tank 7. .
The base oil improvement tank 2 is a tank that performs a process before the fuel oil is mixed. The fuel base oil is supplied from another base oil tank 201. The purpose of this tank is to make the temperature of the oil suitable for mixing. After the fuel base oil is supplied from the base oil tank 201 to the base oil improvement tank 2, it is heated by the heater 8 provided in the base oil improvement tank 2, and is managed at a predetermined temperature by the thermocouple (T).
The fuel base oil in the base oil improvement tank 2 may be taken out from the base oil improvement tank 2 by the pump 11 and re-injected into the tank through the header pipe 202 in order to increase the uniformity of the oil temperature. Further, oil molecules may be subdivided as a pretreatment using a catalyst.
　精製水槽３は、水を活性化する工程を遂行する。本発の方法に使用される水は、軟水であることが好ましく、したがって、水は軟水化装置３０１から供給される。この精製水槽３は、水の温度を混合に適した温度に維持すると共に、水の分子を活性レベルまで細分化することを目的とする。該精製水槽３に供給された水は、該精製水槽３に設けられたヒータ８によって、加熱され、熱電対（Ｔ）によって所定の温度に管理される。ＯＲＰ（酸化・還元電位）計によって、活性化の程度を測定することができる。精製水槽３の底部には超音波発生部１０が設けられており、該超音波発生部１０から、超音波を水に照射することで、水の分子集合体を細分化することができる。この際、２種類の超音波を交互に照射すること好適である。具体的には、１０ｋＨｚ～６０ｋＨｚの超音波と２００ｋＨｚ以上の超音波を交互に照射する。こうすることで、活性化の効率が向上する。
　さらに、精製水槽３においては、触媒９として、トルマリン、銅イオン発生材料を用いることもできる。超音波発生部１０から超音波を照射する際に、水に触媒９を接触させることで、該触媒９から放射される電気エネルギにより、活性化の効率を向上させることができる。
　活性化が均等に行われるように、槽内の水をポンプ１１によりヘッダ３０２に取出し、該ヘッダ３０２から再度、精製水槽３に戻すことにより、水を循環させてもよい。この際、水を槽の下部から引き出し、ポンプ１１で圧力をかけ、ヘッダ管３０２を通して、槽の上部から水を再噴射させる。このような構造とすることで、水の温度、活性化を均等に行うことができる。
　水の活性化は、高圧トランスに接続された電極間に放電を発生させ、この放電により水を解離・電離させるような、水のプラズマアーク処理によって行うこともできる。プラズマアーク処理により水を活性化させる場合、例えば、水の循環経路中、精製水槽３とポンプ１１との間にプラズマアーク処理装置を設置することにより、処理を行うことができる。また、プラズマアーク処理を行う場合、触媒９としてアルミニウムを好適に使用することができる。
　本発明においては、上述した電気エネルギの印加、及び水のプラズマアーク処理を総称して、「電気的刺激」と呼ぶ。 The purified water tank 3 performs the process of activating water. The water used in the present method is preferably soft water, and therefore water is supplied from the water softening device 301. The purpose of the purified water tank 3 is to maintain the temperature of water at a temperature suitable for mixing, and to subdivide the water molecules to an active level. The water supplied to the purified water tank 3 is heated by a heater 8 provided in the purified water tank 3 and is controlled at a predetermined temperature by a thermocouple (T). The degree of activation can be measured by an ORP (oxidation / reduction potential) meter. An ultrasonic generator 10 is provided at the bottom of the purified water tank 3, and the water molecular aggregate can be subdivided by irradiating the ultrasonic wave from the ultrasonic generator 10. At this time, it is preferable to irradiate two types of ultrasonic waves alternately. Specifically, ultrasonic waves of 10 kHz to 60 kHz and ultrasonic waves of 200 kHz or higher are alternately applied. By doing so, the efficiency of activation is improved.
Furthermore, in the purified water tank 3, tourmaline and a copper ion generating material can be used as the catalyst 9. When the ultrasonic wave is irradiated from the ultrasonic wave generation unit 10, the efficiency of activation can be improved by bringing the catalyst 9 into contact with water by the electric energy radiated from the catalyst 9.
The water may be circulated by taking out the water in the tank to the header 302 by the pump 11 and returning it to the purified water tank 3 again from the header 302 so that the activation is performed evenly. At this time, water is drawn from the bottom of the tank, pressure is applied by the pump 11, and water is re-injected from the top of the tank through the header pipe 302. By setting it as such a structure, the temperature and activation of water can be performed equally.
The activation of water can also be performed by a plasma arc treatment of water in which a discharge is generated between electrodes connected to a high-voltage transformer and water is dissociated and ionized by this discharge. When water is activated by plasma arc treatment, for example, the treatment can be performed by installing a plasma arc treatment apparatus between the purified water tank 3 and the pump 11 in the water circulation path. Moreover, when performing a plasma arc process, aluminum can be used suitably as the catalyst 9.
In the present invention, the above-described application of electrical energy and plasma arc treatment of water are collectively referred to as “electrical stimulation”.
　反応促進剤注入部４は、反応促進剤として添加剤を精製水槽３又は反応槽５に投入するものである。添加剤は、過酸化水素を水素と酸素に分解して酸素はガスとして大気に放出させる効果がある。そうすると、加水燃料内の含有水素比率を増大させ発熱量の低下を防止できる。添加剤としては、カタラーゼ、水酸化ナトリウム、過酸化水素水溶液などを用いる。投入する量は、細かく調整する必要がある。カタラーゼを添加する場合には、該カタラーゼの添加量は、水に対する重量比で、０．０４％から０．０５％が好適である。カタラーゼの添加量が０．０４％よりも少ないと効果が薄く、０．０５％よりも多いと十分溶けず、返ってスカムを増やすこととなり、燃料の品質を下げることとなる。 The reaction accelerator injecting section 4 is for introducing an additive into the purified water tank 3 or the reaction tank 5 as a reaction accelerator. The additive has the effect of decomposing hydrogen peroxide into hydrogen and oxygen and releasing the oxygen into the atmosphere as a gas. If it does so, the hydrogen content ratio in a water-added fuel can be increased and the fall of the emitted-heat amount can be prevented. As an additive, catalase, sodium hydroxide, aqueous hydrogen peroxide solution or the like is used. The amount to be fed needs to be finely adjusted. When catalase is added, the amount of catalase added is preferably 0.04% to 0.05% by weight with respect to water. If the amount of catalase added is less than 0.04%, the effect is weak, and if it exceeds 0.05%, it does not dissolve sufficiently, and scum is increased on the contrary, and the quality of the fuel is lowered.
　反応槽５は、攪拌混合工程及び融合工程を遂行するためのものである。燃料元油は、元油改善槽２から反応槽容器１３の上部に供給される。水は、精製水槽３から反応槽容器１３の側面に、噴射管１４により供給される。油と水の混合物は、反応槽容器１３の排出口１５からポンプ１１により取り出され、加圧された状態で、ＯＨＲミキサ１２を通って、ヘッダ管５０２から噴射管１４を通って反応槽容器１３内に循環させられる。ＯＨＲミキサ１２は、複数の物質を効率よく混合するものである。この槽は、融合工程において３～９気圧程度の圧力をかけるので、他の槽よりも高圧力に耐える構造とする必要がある。槽の中段には、ヒータ８があり、油と水の混合物は、該ヒータ８によって所定の温度に管理される。 The reaction vessel 5 is for performing a stirring and mixing step and a fusion step. The fuel base oil is supplied from the base oil improvement tank 2 to the upper part of the reaction tank container 13. Water is supplied from the purified water tank 3 to the side surface of the reaction vessel container 13 through the injection pipe 14. The mixture of oil and water is taken out by the pump 11 from the discharge port 15 of the reaction vessel container 13, and in a pressurized state, passes through the OHR mixer 12, passes from the header pipe 502 through the injection pipe 14, and passes through the reaction vessel container 13. Circulated inside. The OHR mixer 12 mixes a plurality of substances efficiently. Since this tank applies a pressure of about 3 to 9 atm in the fusion process, it needs to have a structure that can withstand a higher pressure than other tanks. There is a heater 8 in the middle of the tank, and the mixture of oil and water is managed at a predetermined temperature by the heater 8.
　改善油静置槽６は、融合工程後の生成物を一時的に貯蔵する槽である。この槽で、添加物などで発生したスカムなどを沈殿させる。油と水が完全に一体となった加水燃料と、不純物とは、この改善油静置槽６内に静置することによって分離され、上澄みである加水燃料が製品受槽７に供給される。不純物には添加剤も含まれることから、不純物は、反応槽５に戻す。この槽での滞留時間は１時間程度が好適である。 The improved oil stationary tank 6 is a tank for temporarily storing the product after the fusion process. In this tank, scum generated by additives is precipitated. Hydrolyzed fuel in which oil and water are completely integrated and impurities are separated by being left in the improved oil standing tank 6, and the hydrolyzed fuel as a supernatant is supplied to the product receiving tank 7. Since the impurities include additives, the impurities are returned to the reaction vessel 5. The residence time in this tank is preferably about 1 hour.
　製品受槽７は、製品として生成された加水燃料を貯蔵する槽である。生成された加水燃料は、ある程度まとまった段階で製品受槽７から製品貯蔵槽７０１に供給される。 The product receiving tank 7 is a tank that stores the hydrolyzed fuel produced as a product. The produced water-added fuel is supplied from the product receiving tank 7 to the product storage tank 701 at a certain stage.
　次に、加水燃料の製造方法について説明する。この方法は、活性化工程、添加剤投入工程、攪拌混合工程、融合工程、及びろ過工程からなる。
　活性化工程は、精製水槽３によって行われる。この工程は、水の分子を活性レベルまで細分化するものである。水を活性レベルまで細分化することによって、燃料元油との親和性が向上し、より多くの水を加水燃料の生成に使用することができる。水を精製水槽３に入れ、超音波発生部１０によって、超音波を水に照射することで、水を高周波で振動させることで、細分化を促す。超音波の周波数を２種類持ち、交互に照射することで、水の細分化を促すことができる。超音波の周波数は、例えば、１０ＫＨｚ～６０ＫＨｚと２００ＫＨｚ以上の２種類とすることでより細分化が可能となる。また、超音波発生部１０を用いる際に、さらに、トルマリン、銅イオン発生材料を触媒として用いて、水に電気的刺激を与える。このような触媒材料を水に接触させた状態で超音波発生部１０を動作させることで、水に対して電気的刺激が与えられ、より活性化を進めることができる。 Next, the manufacturing method of the water fuel will be described. This method includes an activation process, an additive charging process, a stirring and mixing process, a fusion process, and a filtration process.
The activation process is performed by the purified water tank 3. This process subdivides water molecules to activity levels. By subdividing the water to the active level, the affinity with the fuel base oil is improved, and more water can be used for the production of the hydrous fuel. By putting water into the purified water tank 3 and irradiating the ultrasonic wave with water by the ultrasonic wave generation unit 10, the water is vibrated at a high frequency to promote fragmentation. By having two types of ultrasonic frequencies and irradiating them alternately, subdivision of water can be promoted. For example, the frequency of the ultrasonic waves can be further subdivided by using two types of frequencies of 10 KHz to 60 KHz and 200 KHz or more. Moreover, when using the ultrasonic wave generation part 10, electric stimulation is given to water further using tourmaline and a copper ion generation material as a catalyst. By operating the ultrasonic generator 10 in a state where such a catalyst material is in contact with water, electrical stimulation is given to water, and activation can be further promoted.
　超音波を照射することによる活性化の程度は、ＯＲＰ（酸化還元電位）（ｍｖ）を測定することで確認することができる。超音波を照射して得られる水のＯＲＰは、１６０ｍＶ～－２００ｍＶが好ましい。通常の水道水のＯＲＰは７００ｍＶ～５００ｍＶである。
　また、超音波を照射することによって、酸素が放出され、含有水素比率が向上する。
　例えば、水２００Ｌを改質するためにトルマリンと水を接触させる場合には、２０Ｌ／ｍｉｎ～５０Ｌ／ｍｉｎの流量で水を配管１５Ａ～５０Ａから噴出させることが望ましい。およそ反応時間は１時間程度が適当であるが、２０分から１日でも効果を出すことができる。 The degree of activation by irradiating with ultrasonic waves can be confirmed by measuring ORP (redox potential) (mv). The ORP of water obtained by irradiating with ultrasonic waves is preferably 160 mV to -200 mV. The normal tap water ORP is 700 mV to 500 mV.
Moreover, by irradiating with ultrasonic waves, oxygen is released and the hydrogen content ratio is improved.
For example, in the case where tourmaline and water are brought into contact with each other in order to reform 200 L of water, it is desirable to eject water from the pipes 15A to 50A at a flow rate of 20 L / min to 50 L / min. The reaction time is suitably about 1 hour, but the effect can be obtained even from 20 minutes to 1 day.
　次に、添加剤投入工程について説明する。添加剤投入工程は、反応促進剤注入部４に貯蔵された添加剤を精製水槽３又は反応槽５に添加することで、水の含有水素比率を増大させるものである。
　添加剤としては、カタラーゼ、水酸化ナトリウム、過酸化水素水溶液の一種又は複数種を用いる。添加剤の投入量は、細かく調整する必要がある。前述したように、カタラーゼを使用する場合には、カタラーゼの添加量は、水に対する重量比で、０．０４％から０．０５％とするのが好適である。０．０４％よりも少ないと効果が薄く、０．０５％よりも多いと十分溶けず、返ってスカムを増やすこととなり、燃料の品質を下げることとなる。
　水酸化ナトリウムについては、水に対して０．００１重量％～０．１重量％の添加で添加剤としても効果を十分発揮する。過酸化水素水溶液の場合は、水に対して０．００１重量％から０．１重量％の添加で添加剤としても効果を十分発揮する。 Next, the additive charging process will be described. In the additive charging step, the hydrogen content ratio of water is increased by adding the additive stored in the reaction accelerator injection unit 4 to the purified water tank 3 or the reaction tank 5.
As the additive, one or more of catalase, sodium hydroxide, and hydrogen peroxide aqueous solution are used. It is necessary to finely adjust the amount of additive added. As described above, when catalase is used, the amount of catalase added is preferably 0.04% to 0.05% by weight with respect to water. If it is less than 0.04%, the effect is weak, and if it is more than 0.05%, it does not dissolve sufficiently, so that the scum is increased and the quality of the fuel is lowered.
Sodium hydroxide is sufficiently effective as an additive when added in an amount of 0.001 to 0.1% by weight based on water. In the case of an aqueous hydrogen peroxide solution, the addition of 0.001% to 0.1% by weight with respect to water can sufficiently exhibit the effect as an additive.
　次に、攪拌混合工程について説明する。攪拌混合工程では、精製水槽３において活性化され、添加剤が投入された後の水と、燃料元油とを混合する。まず、反応槽５に燃料元油のみを投入する。この燃料元油を反応槽５のＯＨＲミキサ１２を通して循環させる。ＯＨＲミキサ１２を通すことで、燃料元油の分子も均一化され、水と融合しやすくなる。ある程度、循環が完了したところで、精製水槽３から水を反応槽５に少量ずつ投入する。これは、燃料元油に対して水をできるだけ均一に分散させるためである。精製水槽３から供給される水は、精製水槽３のポンプ１１によって加圧され、排出口１５からの油と混合され、反応槽５のポンプ１１によって加圧され、ＯＨＲミキサ１２によって混合されていく。ＯＨＲミキサ１２の圧力は３気圧（０．３ＭＰａ）以上、温度は４０℃から８０℃が好適である。したがって、精製水槽３、反応槽５のポンプ１１の圧力は、それに見合った圧力とし、精製水槽３、反応槽５のヒータ８の加温もそれに見合ったものとする。ＯＨＲミキサ１２で混合された水と油は、ヘッダ管５０２を通って、噴射管１４から反応槽５に再投入される。反応槽５に対する噴射管１４の角度、反応槽５内部での突出量によって、混合の効率、質が変化する。
　例えば、水１００Ｌを燃料元油１００Ｌと混合する場合には、水と燃料元油の混合物は、２０Ｌ／ｍｉｎ～５０Ｌ／ｍｉｎの流量で配管サイズ１５Ａ～５０Ａのものを通して循環させることが好ましい。混合時間は、５分～１時間程度とすることができる。 Next, the stirring and mixing step will be described. In the stirring and mixing step, the water after being activated in the purified water tank 3 and charged with the additive is mixed with the fuel base oil. First, only the fuel base oil is charged into the reaction tank 5. This base fuel oil is circulated through the OHR mixer 12 in the reaction vessel 5. By passing through the OHR mixer 12, the molecules of the fuel base oil are also made uniform and can be easily fused with water. When the circulation is completed to some extent, water is poured into the reaction tank 5 from the purified water tank 3 little by little. This is because water is dispersed as uniformly as possible in the fuel base oil. The water supplied from the purified water tank 3 is pressurized by the pump 11 of the purified water tank 3, mixed with oil from the discharge port 15, pressurized by the pump 11 of the reaction tank 5, and mixed by the OHR mixer 12. . The pressure of the OHR mixer 12 is preferably 3 atm (0.3 MPa) or more, and the temperature is preferably 40 ° C. to 80 ° C. Therefore, the pressure of the pump 11 of the purified water tank 3 and the reaction tank 5 is set to a pressure corresponding to that, and the heating of the heater 8 of the purified water tank 3 and the reaction tank 5 is also set to the pressure. Water and oil mixed in the OHR mixer 12 are reintroduced into the reaction tank 5 from the injection pipe 14 through the header pipe 502. The efficiency and quality of mixing vary depending on the angle of the injection tube 14 with respect to the reaction tank 5 and the amount of protrusion inside the reaction tank 5.
For example, when 100 L of water is mixed with 100 L of fuel base oil, the mixture of water and fuel base oil is preferably circulated through a pipe size of 15 A to 50 A at a flow rate of 20 L / min to 50 L / min. The mixing time can be about 5 minutes to 1 hour.
　次に、融合工程について説明する。融合工程では、水の精製水槽３から反応槽５への投入は完了しており、該融合工程は、ＯＨＲミキサ１２を通して、循環させることにより遂行される。圧力は、攪拌混合工程と同じ３気圧（０．３ＭＰａ）以上、温度は４０℃から８０℃が好適である。この工程において、ＯＨＲミキサ１２を十分に通すことで、水と油の融合が行われ、分離する恐れのない加水燃料とすることができる。
　例えば、水１００Ｌを油１００Ｌに融合させる場合には、加圧圧力は、０．３ＭＰａ（３気圧）以上、温度は７０℃以上とすることが望ましいが、それ以上の加圧圧力、及びそれ以下の温度でもよく、加圧圧力０．９ＭＰａ、温度５０℃が最も有効である。反応時間は、この加圧圧力及び温度に到達してから２０分～６０分が適当である。 Next, the fusion process will be described. In the fusion process, the introduction of water from the purified water tank 3 to the reaction tank 5 is completed, and the fusion process is performed by circulating through the OHR mixer 12. The pressure is preferably 3 atm (0.3 MPa) or more as in the stirring and mixing step, and the temperature is preferably from 40 ° C to 80 ° C. In this step, by sufficiently passing through the OHR mixer 12, the water and oil are fused, and the fuel can be obtained without any fear of separation.
For example, when fusing 100 L of water with 100 L of oil, the pressurizing pressure is preferably 0.3 MPa (3 atm) or higher, and the temperature is preferably 70 ° C. or higher, but higher pressurizing pressure and lower The pressure of 0.9 MPa and the temperature of 50 ° C. are the most effective. The reaction time is suitably 20 minutes to 60 minutes after reaching this pressure and temperature.
　次に、ろ過工程について説明する。ろ過工程では、完全に生成された加水燃料から、生成時に酵素を使用した場合に酵素の成分やその他の成分が凝固してスカム状となったものを分離する工程である。改善油静置槽６を用いる方法は、生成物を静置させ、比重分離する方法である。比較的比重の重いスカムなどは底に溜まり、加水燃料は、比重が軽いので上層に集まる。上層の加水燃料を製品受槽７に送り、製品の完成となる。改善油静置槽６での滞留時間は１時間以上とることが望ましい。
　また、ろ過フィルターを通過させることによっても、加水燃料とスカムなどを分離できる。ろ過フィルターは、１０μｍ～３０μｍ程度のものを用いる。ろ過フィルターを通過させる温度は４０℃以下が好ましく、通過時間は、配管２０Ａ～５０Ａで流量２０Ｌ／ｍｉｎ～５０Ｌ／ｍｉｎ程度が望ましいが、速度は穏やかな方がより望ましい。ろ過フィルター通過の回数は１回以上であればよい。 Next, the filtration process will be described. The filtration step is a step of separating a scum-like product obtained by coagulating an enzyme component and other components when the enzyme is used at the time of production from the completely produced water fuel. The method using the improved oil stationary tank 6 is a method in which the product is allowed to stand and the specific gravity is separated. Scum, which has a relatively high specific gravity, accumulates at the bottom, and the water is concentrated in the upper layer because of its low specific gravity. The upper layer hydrolyzed fuel is sent to the product receiving tank 7 to complete the product. The residence time in the improved oil stationary tank 6 is desirably 1 hour or longer.
Also, the water fuel and scum can be separated by passing through a filtration filter. A filtration filter having a size of about 10 μm to 30 μm is used. The temperature for passing through the filtration filter is preferably 40 ° C. or less, and the passage time is preferably about 20 L / min to 50 L / min in the pipes 20A to 50A, but the speed is more preferable. The frequency | count of filtration filter should just be 1 time or more.
　このように、上記の工程を行うことによって、水と燃料油を完全に混合し、時間が経過しても分離せず、且つ、短時間で水と燃料油の融合処理を行うことができる。 Thus, by performing the above-described steps, water and fuel oil are completely mixed, and even if time elapses, the water and fuel oil can be fused in a short time.
　本発明の他の実施形態について図３を用いて説明する。前述の実施形態と同様の部分は省略する。図３は、本発明に係る製造装置の反応槽への噴射管の構造図である。図３（ａ）は、反応槽５と噴射管１４の関係を上部から見た図である。図３（ｂ）は、反応槽５の側面図である。
　前述の実施形態において、加水燃料製造のための各工程について説明したが、そのなかで、攪拌混合工程及び融合工程で、どのように水と燃料元油の混合物を循環させるかが重要である。循環は、図２に示す装置において、基本的に、反応槽５の排出口１５から排出された混合物を、ポンプ１１及びＯＨＲミキサ１２から、噴射管１４を経て、反応槽５の上部側面から、再び反応槽５内に噴射状態で投入することにより行われる。循環では、混合物のすべてが均等に循環されることが理想である。しかし、反応槽５内への再投入の方法が適当でないと、混合物の一部のみがより多く循環され、他の部分は、あまり循環されないこととなり、全体が均一の加水燃料とならないか、又は均一にするまでの時間が非常にかかることになる。 Another embodiment of the present invention will be described with reference to FIG. Parts similar to those of the above-described embodiment are omitted. FIG. 3 is a structural diagram of the injection pipe to the reaction tank of the production apparatus according to the present invention. FIG. 3A is a view of the relationship between the reaction tank 5 and the injection pipe 14 as viewed from above. FIG. 3B is a side view of the reaction vessel 5.
In the above-described embodiment, each process for producing the hydrolyzed fuel has been described. Among them, how to circulate the mixture of water and fuel base oil in the stirring and mixing process and the fusion process is important. In the apparatus shown in FIG. 2, basically, the mixture is discharged from the discharge port 15 of the reaction tank 5 from the pump 11 and the OHR mixer 12 through the injection pipe 14 and from the upper side surface of the reaction tank 5. It is carried out by charging the reaction vessel 5 again in an injection state. In circulation, ideally all of the mixture is circulated evenly. However, if the method of recharging into the reaction vessel 5 is not appropriate, only a part of the mixture will be circulated more and the other part will not be circulated so much, or the whole will not be a uniform hydrofuel, or It takes a very long time to make it uniform.
　そこで、本発明の発明者は、反応槽５へ混合物を再投入する噴射管１４と反応槽５との関係について検討した。図３（ｂ）に示すように、反応槽５は、上部が円筒体、下部が円錐体である。上部の側面には、噴射管１４が４つ配置され、図３（ａ）に示すように、４方向から、油水混合物を反応槽５内に噴射することができる。図３（ｃ）に示すように、反応槽５の円筒部の中心軸と噴射管１４が反応槽５に取り付けられる取付点とを結ぶ直径線に対する、噴射管１４の長さ方向の角度を、該噴射管１４の取付角又は噴射方向と定めた。そして、この取付角を、０度から９０度まで変えた際の、融合に必要な時間、生成された加水燃料の品質について検討した。図３（ｃ）において、取付角が０度の場合が噴射管１４ａ１である。以下１４ａ２、１４ａ３、１４ａ４と軸からの角度を大きくした。角度が１５度ごとに検討した。結果、軸からの角度が４５度のときが最も融合に必要な時間が短く、生成された加水燃焼の品質もよいことが確認された。この結果から、噴射管１４の取付角は、上述の直径線に対し、約４０度から約５０度までの範囲が好ましいことが分かる。 Therefore, the inventor of the present invention examined the relationship between the injection tube 14 for recharging the mixture into the reaction vessel 5 and the reaction vessel 5. As shown in FIG. 3B, the reaction vessel 5 has a cylindrical body at the top and a cone at the bottom. Four injection pipes 14 are arranged on the upper side surface, and the oil / water mixture can be injected into the reaction tank 5 from four directions as shown in FIG. As shown in FIG. 3 (c), the angle in the length direction of the injection tube 14 with respect to the diameter line connecting the central axis of the cylindrical portion of the reaction vessel 5 and the attachment point where the injection tube 14 is attached to the reaction vessel 5, The mounting angle or the injection direction of the injection pipe 14 was determined. And when this attachment angle was changed from 0 degree to 90 degree | times, the time required for a fusion and the quality of the produced | generated water fuel were examined. In FIG.3 (c), the case where an attachment angle is 0 degree | times is the injection pipe 14a1. Below, the angle from 14a2, 14a3, 14a4 and the axis was enlarged. The angle was examined every 15 degrees. As a result, it was confirmed that when the angle from the axis was 45 degrees, the time required for fusion was the shortest, and the quality of the produced hydro-combustion was good. From this result, it can be seen that the mounting angle of the injection tube 14 is preferably in the range of about 40 degrees to about 50 degrees with respect to the above-described diameter line.
　次に、図３（ｄ）のように、噴射管１４の、直径が６０ｃｍの反応槽５内部への突出量と融合に必要な時間、生成された加水燃料の品質について検討した。図３（ｄ）において、突出量が０の場合が噴射管１４ｂ１である。以下１４ｂ２、１４ｂ３、１４ｂ４と突出量を大きくした。突出量は１０ｃｍ単位で検討した。結果、突出量は１０ｃｍのときが最も融合に必要な時間が短く、生成された加水燃焼の品質もよかった。なお、さらに大きい反応槽を使用する場合、反応槽の直径に応じて噴射管の突出量を大きくするのが好ましく、また、噴射管の数を増やすのが望ましいと考えられる。 Next, as shown in FIG. 3 (d), the amount of protrusion of the injection tube 14 into the reaction vessel 5 having a diameter of 60 cm, the time required for fusion, and the quality of the produced hydrofuel were examined. In FIG.3 (d), when the protrusion amount is 0, it is the injection pipe 14b1. Below, the amount of protrusion was increased to 14b2, 14b3, 14b4. The amount of protrusion was examined in units of 10 cm. As a result, when the protrusion amount was 10 cm, the time required for fusion was the shortest, and the quality of the produced hydrocombustion was good. When a larger reaction tank is used, it is preferable to increase the protruding amount of the injection pipe according to the diameter of the reaction tank, and it is desirable to increase the number of injection pipes.
　以上のことから、反応槽５への噴射管１４による混合物の投入は、円筒の直径線に対して４５度の角度で、噴射管１４の反応槽５内部への突出量は、１０ｃｍが最適である。円筒の軸に対して角度を持たせることによって、槽内に自然な渦を作ることができる。そのため、混合も効率的にできる。また、噴射管１４の反応槽５内部への突出量を所定の量とすることによって、混合物の円周付近又は、中心付近のみに循環した混合物が集まってしまうことを避けることができる。噴射管１４は、反応槽５内の液面から少なくとも８ｃｍ、好ましくは少なくとも１０ｃｍだけ上方に位置するように配置し、混合物は、高速で噴射管１４から噴射されるようにすることが好ましい。 In view of the above, the mixture is injected into the reaction vessel 5 through the injection tube 14 at an angle of 45 degrees with respect to the diameter line of the cylinder, and the projection amount of the injection tube 14 into the reaction vessel 5 is optimally 10 cm. is there. By providing an angle with respect to the axis of the cylinder, a natural vortex can be created in the tank. Therefore, mixing can be performed efficiently. Further, by setting the amount of protrusion of the injection tube 14 into the reaction tank 5 to a predetermined amount, it is possible to avoid the mixture that has circulated around the circumference of the mixture or only near the center. It is preferable that the injection tube 14 is disposed so as to be located at least 8 cm, preferably at least 10 cm above the liquid level in the reaction vessel 5, and the mixture is injected from the injection tube 14 at a high speed.
　このように、噴射管１４の反応槽５に対する配置を調整することによって、水と燃料元油を完全に混合し、時間が経過しても分離せず、且つ、短時間で水と燃料油の融合処理を行うことができる。 In this way, by adjusting the arrangement of the injection pipe 14 with respect to the reaction tank 5, water and the fuel base oil are completely mixed, do not separate even after a long time, and the water and fuel oil can be mixed in a short time. Fusion processing can be performed.
　本発明のさらに別の実施形態について図４を用いて説明する。
　図４は、本発明に係る製造装置の活性化装置として使用可能なプラズマアーク処理装置の一例を示す概略図である。このプラズマアーク処理装置２０は、それぞれが高圧トランス（図示せず）に接続されている、装置の中心に配置された（図中六角形で示されている）電極２１と、この中心電極を取り囲むように配置された複数の（図では１２本の）電極２２を備えている。電極に電力を供給することにより、電極間にアーク放電が発生する。図２に示されている製造装置１中の精製水槽３において、精製水槽３とポンプ１１との間にプラズマアーク処理装置２０を設置して、精製水槽からの水をプラズマアーク処理装置２０に通すことにより、水をプラズマアーク処理によって活性化することができる。このようなプラズマアーク処理装置としては、例えば、株式会社日本理水研社製のウルトラＵ－ＭＡＮに使用されているようなプラズマアーク処理装置を好適に使用することができる。 Still another embodiment of the present invention will be described with reference to FIG.
FIG. 4 is a schematic diagram showing an example of a plasma arc processing apparatus that can be used as an activation apparatus of a manufacturing apparatus according to the present invention. The plasma arc treatment device 20 surrounds the central electrode with an electrode 21 (shown as a hexagon in the figure) disposed at the center of the device, each connected to a high voltage transformer (not shown). A plurality of (in the figure, twelve) electrodes 22 are provided. By supplying power to the electrodes, arc discharge occurs between the electrodes. In the purified water tank 3 in the production apparatus 1 shown in FIG. 2, a plasma arc treatment apparatus 20 is installed between the purified water tank 3 and the pump 11, and water from the purified water tank is passed through the plasma arc treatment apparatus 20. Thus, water can be activated by plasma arc treatment. As such a plasma arc processing apparatus, for example, a plasma arc processing apparatus used for Ultra U-MAN manufactured by Nippon Risuiken Co., Ltd. can be preferably used.
（実施例１）
　次のとおりの方法により、Ａ重油を元油とする加水燃料を製造した。
　まず、トルマリンを収容する部分と超音波発生装置（３５ｋＨｚの超音波振動子）、及び温度計を備え、循環ポンプ（２４リットル／分×０．５Ｍｐａ）を接続した容積２５リットルの容器に、トルマリン（有限会社ニュー・ウェーブから購入したブラジル・トカチン州鉱山直輸入トルマリン原石　サイズ小）３ｋｇと水道水を２０リットルとを入れた。この水に、カタラーゼ（ナガセケムテックス株式会社製　レオネットＦ－３５）を２０ミリリットル添加した。次いで、超音波振動子を作動させ、循環用ポンプにより水の循環を開始した。水の循環経路中に設けた３ｋＷのラインヒータの設定温度を４０℃とし、容器内の水の温度が４０℃以上になったことを確認した時点から１時間、循環を続けた。１時間経過後、ＯＲＰ計によって容器中の水の酸化還元電位を測定したところ、１２ｍＶであった。 (Example 1)
A water-added fuel using A heavy oil as a base oil was produced by the following method.
First, a tourmaline container with a volume of 25 liters equipped with a part for accommodating tourmaline, an ultrasonic generator (35 kHz ultrasonic transducer), and a thermometer and connected with a circulation pump (24 liters / minute × 0.5 Mpa). (Small size tourmaline imported directly from New Wave, Co., Ltd.) 3 kg and 20 liters of tap water were added. To this water, 20 ml of catalase (Leonet F-35 manufactured by Nagase ChemteX Corporation) was added. Next, the ultrasonic vibrator was activated, and water circulation was started by a circulation pump. The set temperature of the 3 kW line heater provided in the water circulation path was set to 40 ° C., and the circulation was continued for 1 hour from the time when it was confirmed that the temperature of the water in the container became 40 ° C. or higher. After 1 hour, the redox potential of the water in the container was measured with an ORP meter, and it was 12 mV.
　次に、上記容器と同様に温度計を備え、循環ポンプを接続した容積２５リットルの容器に、市販のＡ重油（富士興産株式会社から購入した１種１号Ａ重油）を２０リットル入れた。循環ポンプによりＡ重油の循環を開始した。Ａ重油の循環経路中に設けた３ｋＷのラインヒータの設定温度を４０℃とし、容器内のＡ重油の温度が４０℃以上になったことを確認した時点から１時間、循環を続けた。 Next, 20 liters of commercially available A heavy oil (Type 1 No. 1 A heavy oil purchased from Fujikosan Co., Ltd.) was placed in a 25 liter container equipped with a thermometer and connected to a circulation pump, as in the above container. Circulation of heavy oil A was started by a circulation pump. The set temperature of the 3 kW line heater provided in the circulation path of A heavy oil was set to 40 ° C., and the circulation was continued for 1 hour from the time when it was confirmed that the temperature of the A heavy oil in the container became 40 ° C. or higher.
　このようにして得られた活性化した水及びＡ重油を、次のように混合し且つ攪拌し、さらに温度と圧力を印加して融合させた。すなわち、温度計に加えて１ｋＷの加温ヒータとプロペラ式の攪拌機とを備え、循環ポンプを接続し、さらに混合ミキサ（株式会社ＯＨＲ流体工学研究所製ＯＨＲミキサ）を接続した容積２５リットルの上部を大気に開放した開放系の容器に、活性化した水を１０リットル、得られたＡ重油を１０リットル入れた。加温ヒータの電源を入れ、容器内の液体の温度が４０℃で維持されるようにした。ここに、上記と同じカタラーゼを１０ミリリットル添加した。４０分経過した後、攪拌機の電源を入れ、水とＡ重油を混合、撹拌した。次いで、循環ポンプを作動させるとともに、混合ミキサへの供給圧力が０．５ＭＰａ程度となるように調整して、混合液体を循環させた。その際、循環経路から容器に液体を投入する循環配管が、容器内の混合液体の液面から８ｃｍ程度上方に位置するようにした。混合液体を１時間循環させた後、攪拌機、循環ポンプ及び加温ヒータを停止した。このようにして得られた液体（加水燃料）を約３日間静置した後、分析のため試料を採取した。採取した試料の量は、２０リットルであった。 The activated water and heavy oil A obtained in this way were mixed and stirred as follows, and were further fused by applying temperature and pressure. In other words, in addition to a thermometer, a 1 kW heating heater and a propeller type stirrer are connected, a circulation pump is connected, and a mixing mixer (OHR mixer manufactured by OHR Fluid Engineering Laboratory Co., Ltd.) is connected to an upper part of a 25 liter 10 liters of activated water and 10 liters of the obtained heavy fuel oil A were placed in an open system container opened to the atmosphere. The heater was turned on so that the temperature of the liquid in the container was maintained at 40 ° C. Here, 10 ml of the same catalase as described above was added. After 40 minutes, the stirrer was turned on, and water and A heavy oil were mixed and stirred. Next, the circulating pump was operated, and the supply pressure to the mixing mixer was adjusted to be about 0.5 MPa, and the mixed liquid was circulated. At that time, the circulation pipe for introducing the liquid into the container from the circulation path was positioned about 8 cm above the liquid level of the mixed liquid in the container. After the mixed liquid was circulated for 1 hour, the stirrer, the circulation pump and the heating heater were stopped. The liquid (hydrolyzed fuel) thus obtained was allowed to stand for about 3 days, and a sample was taken for analysis. The amount of sample collected was 20 liters.
（実施例２）
　元油として、Ａ重油に代えて市販の軽油（ＪＸエネルギ株式会社（ＥＮＥＯＳ）から購入した２号軽油）を使用したことを除き、実施例１と同様にして加水燃料を製造し、分析のため試料を採取した。採取した試料の量は、２０リットルであった。 (Example 2)
As a base oil, a hydro fuel was produced in the same manner as in Example 1 except that a commercially available light oil (No. 2 light oil purchased from JX Energy Co., Ltd. (ENEOS)) was used instead of A heavy oil. A sample was taken. The amount of sample collected was 20 liters.
　表１に、本発明の実施例１及び実施例２で生成された加水燃料の成分分析結果を示す。水と油を１対１で混合、融合したものである。
　比較のため、元油として使用したＡ重油及び軽油についても同様の成分分析を行った。
　まず、総発熱量、真発熱量を見ると、実施例１、実施例２とも、元油を上回っており、本発明の効果が出ていることが分かる。
　次に、水分の項目を見ると、実施例１、実施例２とも水分の容積％は０．００％である。燃料油と水を１対１で混合、融合したものであるから、十分な融合ができていなければ、水分量として検出されるはずである。しかるに、水分の容積％が０．００％であるということは、燃料油と水が完全に融合し、水成分として、分析されなかったことである。
　このように、本発明によれば、燃料元油と水を完全融合し、高品質の加水燃料を生成することができる。 Table 1 shows the component analysis results of the water fuel produced in Example 1 and Example 2 of the present invention. It is a mixture of water and oil, mixed one-on-one.
For comparison, the same component analysis was performed on the A heavy oil and light oil used as the base oil.
First, looking at the total calorific value and the true calorific value, it can be seen that both Example 1 and Example 2 exceed the base oil, and the effect of the present invention is obtained.
Next, looking at the item of moisture, the volume% of moisture in both Example 1 and Example 2 is 0.00%. Since fuel oil and water are mixed and fused one-on-one, if sufficient fusion is not achieved, the amount of water should be detected. However, the volume% of water being 0.00% means that the fuel oil and water were completely fused and were not analyzed as water components.
Thus, according to the present invention, the fuel base oil and water can be completely fused to produce a high-quality water-added fuel.
Figure JPOXMLDOC01-appb-T000001
Figure JPOXMLDOC01-appb-T000001
（実施例３）
　図２及び図３に示したような装置を使用し、元油として軽油を使用して、加水燃料を製造した。
　まず、トルマリンを収容する部分に実施例１で使用したものと同じトルマリンを充填した精製水槽に、水道水を１５０リットル注入した。精製水槽に設置されたヒータの電源を入れ、温度を４０℃に設定した。実施例１で使用したものと同じカタラーゼを１５０ミリリットル添加した。精製水槽に接続された循環ポンプを作動させ（吐出圧力０．５ＭＰａ）、精製水槽に設置された超音波発生装置を作動させて、水の温度が４０℃に達するまで６０分間、４０℃に達した後さらに６０分間、超音波（周波数４０ｋＨｚ）を照射した。水を精製水槽に投入する際、４本の噴射管のうち１本のみを使用（３本を閉止）して、噴射管先端部での流速を３．３ｍ／ｓとした。ＯＲＰ計によって得られた水の酸化還元電位を測定したところ、２０ｍＶであった。 (Example 3)
The apparatus as shown in FIG.2 and FIG.3 was used, and the fuel oil was manufactured using light oil as base oil.
First, 150 liters of tap water was injected into a purified water tank filled with the same tourmaline as that used in Example 1 in a portion containing tourmaline. The heater installed in the purified water tank was turned on and the temperature was set to 40 ° C. 150 ml of the same catalase used in Example 1 was added. The circulation pump connected to the purified water tank is operated (discharge pressure 0.5 MPa), and the ultrasonic generator installed in the purified water tank is operated to reach 40 ° C. for 60 minutes until the water temperature reaches 40 ° C. After that, ultrasonic waves (frequency: 40 kHz) were further irradiated for 60 minutes. When water was introduced into the purified water tank, only one of the four injection tubes was used (three were closed), and the flow velocity at the tip of the injection tube was 3.3 m / s. It was 20 mV when the oxidation reduction potential of the water obtained by the ORP meter was measured.
　次に、元油改善槽に、市販の軽油（ＪＸエネルギ株式会社（ＥＮＥＯＳ）から購入した２号軽油）を１５０リットル注入した。元油改善槽に設置されたヒータの電源を入れ、温度を４０℃に設定した。元油改善槽に接続された循環ポンプを作動させ（吐出圧力０．３ＭＰａ）、軽油の温度が４０℃に達するまで６０分間、４０℃に達した後さらに６０分間、循環させた。軽油を元油改善槽に噴射する際、４本の噴射管のうち１本のみを使用（３本を閉止）して、噴射管先端部での流速を２．０ｍ／ｓとした。 Next, 150 liters of commercially available light oil (No. 2 light oil purchased from JX Energy Corporation (ENEOS)) was injected into the base oil improvement tank. The heater installed in the base oil improvement tank was turned on, and the temperature was set to 40 ° C. A circulation pump connected to the base oil improvement tank was operated (discharge pressure 0.3 MPa), and the oil was circulated for 60 minutes until the temperature of the light oil reached 40 ° C., and after reaching 40 ° C. for another 60 minutes. When light oil was injected into the base oil improvement tank, only one of the four injection pipes was used (three were closed), and the flow velocity at the tip of the injection pipe was 2.0 m / s.
　このようにして得られた活性化した水及び軽油を、次のように混合し且つ攪拌し、さらに温度と圧力を印加して融合させた。すなわち、反応槽に、元油改善槽中の元油を７５リットル、精製水槽中の活性化した水を５５リットル移送した（加水率約４２％）。ここに、上記と同じカタラーゼを６５ミリリットル添加した。ヒータの電源を入れ、容器内の液体の温度が４０℃となるようにした。液温が４０℃に達した後、循環ポンプを作動させるとともに、混合ミキサへの供給圧力が０．５ＭＰａ程度となるように調整して、混合液体を６０分間循環させた。混合液を反応槽に投入する際、４本の噴射管のうち１本のみを使用（３本を閉止）して、噴射管先端部での流速を２．０ｍ／ｓとした。また、噴射管が、反応槽中で混合液中に没しないようにした。具体的には、噴射管が、反応槽内の混合液の液面から８ｃｍ程度上方にくるようにした。得られた液体から、分析のため試料を採取した。採取した試料の量は、１１４リットルであった。 The activated water and light oil thus obtained were mixed and stirred as follows, and were further fused by applying temperature and pressure. That is, 75 liters of the base oil in the base oil improvement tank and 55 liters of the activated water in the purified water tank were transferred to the reaction tank (hydration ratio of about 42%). Here, 65 ml of the same catalase as described above was added. The heater was turned on so that the temperature of the liquid in the container was 40 ° C. After the liquid temperature reached 40 ° C., the circulation pump was operated, and the supply pressure to the mixing mixer was adjusted to be about 0.5 MPa, and the mixed liquid was circulated for 60 minutes. When the mixed solution was charged into the reaction tank, only one of the four injection tubes was used (three were closed), and the flow rate at the tip of the injection tube was 2.0 m / s. In addition, the injection tube was not submerged in the mixed solution in the reaction vessel. Specifically, the injection tube was arranged to be about 8 cm above the liquid level of the mixed solution in the reaction tank. A sample was taken from the resulting liquid for analysis. The amount of sample collected was 114 liters.
（実施例４）
　精製水槽、元油改善槽、及び反応槽の温度を、実施例３の場合よりも高く、それぞれ４２℃、４１℃、及び４４℃に設定する一方、精製水槽及び元油改善槽での循環時間を実施例３の場合の半分（すなわちいずれも６０分）としたことを除き、実施例３と同様に加水燃料を製造した。なお、ＯＲＰ計によって精製水槽で得られた水の酸化還元電位を測定したところ、２６ｍＶであった。反応槽で得られた液体から、分析のため試料を採取した。採取した試料の量は、１１４リットルであった。 Example 4
While the temperatures of the purified water tank, the base oil improvement tank, and the reaction tank are higher than those in Example 3, they are set to 42 ° C., 41 ° C., and 44 ° C., respectively, while the circulation time in the purified water tank and the base oil improvement tank Was made in the same manner as in Example 3 except that the fuel was reduced to half of that in Example 3 (that is, 60 minutes). In addition, it was 26 mV when the oxidation reduction potential of the water obtained with the ORP meter in the purified water tank was measured. A sample was taken from the liquid obtained in the reaction vessel for analysis. The amount of sample collected was 114 liters.
（実施例５）
　元油としてＡ重油（富士興産株式会社から購入した１種１号Ａ重油）を使用し、反応槽温度を３６℃に設定する一方、精製水槽及び元油改善槽での循環時間をいずれも９０分とするとともに、カタラーゼの精製水槽及び反応槽での添加量をそれぞれ２３０ミリリットル及び１３０ミリリットルとしたことを除き、実施例３と同様に加水燃料を製造した。なお、ＯＲＰ計によって精製水槽で得られた水の酸化還元電位を測定したところ、１８ｍＶであった。反応槽で得られた液体から、分析のため試料を採取した。採取した試料の量は、１１４リットルであった。 (Example 5)
While using A heavy oil (type 1 No. 1 A heavy oil purchased from Fujikosan Co., Ltd.) as the base oil and setting the reaction tank temperature to 36 ° C, the circulation time in the refined water tank and the base oil improvement tank is both 90 The hydrolyzed fuel was produced in the same manner as in Example 3 except that the amount of catalase added to the purified water tank and the reaction tank was 230 ml and 130 ml, respectively. In addition, it was 18 mV when the redox potential of the water obtained in the purified water tank was measured with the ORP meter. A sample was taken from the liquid obtained in the reaction vessel for analysis. The amount of sample collected was 114 liters.
　表２に、本発明の実施例４及び実施例５で生成された加水燃料の成分分析結果を示す。 Table 2 shows the component analysis results of the water fuel produced in Example 4 and Example 5 of the present invention.
Figure JPOXMLDOC01-appb-T000002
Figure JPOXMLDOC01-appb-T000002
［加水燃料の定性分析］
　実施例３において軽油を燃料元油として本発明の方法により得られた加水燃料の試料について、ガスクロマトグラム質量分析法（ＧＣ－ＭＳ）による定性分析を行った。分析試料として、実施例３で得られた試料をｎ－ヘキサンで１０００倍に希釈したものを準備した。カラムはＨＰ－５ＭＳ（長さ３０ｍ、内径２．５ｍｍ、膜厚０．２５μｍ）を使用し、キャリアーガスはＨｅとした。分析試料の注入量は１マイクロリットル、注入方法はスプリットレスモードとし、オーブン温度は５０℃で３分間保持、そこから１００℃まで毎分５℃で昇温し、さらにそこから３００℃まで毎分１５℃で昇温し、３００℃で３分間保持した。結果として得られたＧＣ－ＭＳのチャートを図５に示す。（ａ）はＴＩＣクロマトグラム、（ｂ）は１８．４分付近のピークのマススペクトルである。
　実施例４で得られた加水燃料の試料についても、同様の定性分析を行った。結果を図６に示す。
　比較のため、燃料元油として使用した軽油についても、同様の定性分析を行った。結果を図７に示す。
　図５及び図６を図７と対比すると、炭素数の多い成分（Ｃ１９よりも大きいもの）が、元油に比べて減少する傾向が認められるものの、実施例３及び実施例４で得られた加水燃料は、その成分組成が元油とよく一致することが確認された。 [Qualitative analysis of water fuel]
A qualitative analysis by gas chromatogram mass spectrometry (GC-MS) was performed on a sample of the hydrolyzed fuel obtained by the method of the present invention using light oil as the fuel base oil in Example 3. As an analytical sample, a sample obtained by diluting the sample obtained in Example 3 1000-fold with n-hexane was prepared. The column was HP-5MS (length 30 m, inner diameter 2.5 mm, film thickness 0.25 μm), and the carrier gas was He. The injection volume of the analytical sample is 1 microliter, the injection method is splitless mode, the oven temperature is maintained at 50 ° C. for 3 minutes, from there it is raised to 100 ° C. at 5 ° C. per minute, and then from there to 300 ° C. per minute. The temperature was raised at 15 ° C. and held at 300 ° C. for 3 minutes. The resulting GC-MS chart is shown in FIG. (A) is a TIC chromatogram, and (b) is a mass spectrum of a peak around 18.4 minutes.
The same qualitative analysis was performed for the sample of the hydrolyzed fuel obtained in Example 4. The results are shown in FIG.
For comparison, the same qualitative analysis was performed on light oil used as the fuel base oil. The results are shown in FIG.
When FIG. 5 and FIG. 6 are compared with FIG. 7, the components having a large number of carbon atoms (those larger than C19) tend to decrease compared to the base oil, but were obtained in Example 3 and Example 4. It was confirmed that the component composition of the water fuel was in good agreement with the base oil.
　実施例５でＡ重油を元油として本発明の方法により得られた加水燃料の試料についても、同様の定性分析を行った。結果を図８に示す。
　比較のため、元油として使用したＡ重油についても、同様の定性分析を行った。結果を図９に示す。
　図８を図９と対比すると、実施例５で得られた加水燃料も、その成分組成が元油とよく一致することが確認された。 The same qualitative analysis was performed on the sample of the hydrofuel obtained by the method of the present invention using A heavy oil as the base oil in Example 5. The results are shown in FIG.
For comparison, the same qualitative analysis was performed on heavy oil A used as the base oil. The results are shown in FIG.
Comparing FIG. 8 with FIG. 9, it was confirmed that the component composition of the water fuel obtained in Example 5 also coincided well with the base oil.
［加水燃料の性状試験］
　実施例３及び実施例４で軽油を元油として本発明の方法により得られた加水燃料の試料について、性状試験を行った。性状試験の項目と方法は、次のとおりとした。
　・密度（振動式１５℃）：　JIS K2249
　・動粘度（３０℃）：　JIS K2283
　・窒素定量分析：　JIS K2609
　・硫黄分（紫外蛍光法）：　JIS K2541-6
　・酸素分：　ASTM D5622
　・軽油組成分析（JPI法）：　JPI-5S-49
　比較のため、元油として使用した軽油についても、同様の性状試験を行った。
　結果を表３に示す。
　表３から、本発明の方法により得られた加水燃料では、元油に比べて芳香族分が減少し、飽和分が増加していることが認められる。芳香族分が少なく飽和分が多い軽油は、効率や排ガスの毒性分及びＰＭの削減の観点から望ましいとされている。 [Characteristic test of water fuel]
In Example 3 and Example 4, the property test was conducted on the samples of the hydrofuel obtained by the method of the present invention using light oil as the base oil. The property test items and methods were as follows.
・ Density (vibration type 15 ℃): JIS K2249
・ Kinematic viscosity (30 ℃): JIS K2283
・ Nitrogen quantitative analysis: JIS K2609
・ Sulfur content (ultraviolet fluorescence method): JIS K2541-6
・ Oxygen content: ASTM D5622
-Light oil composition analysis (JPI method): JPI-5S-49
For comparison, the same property test was performed on light oil used as base oil.
The results are shown in Table 3.
From Table 3, it can be seen that the water content obtained by the method of the present invention has a reduced aromatic content and an increased saturated content compared to the base oil. A light oil with a small aromatic content and a high saturation content is desirable from the viewpoints of efficiency, toxic content of exhaust gas, and reduction of PM.
Figure JPOXMLDOC01-appb-T000003
Figure JPOXMLDOC01-appb-T000003
［加水燃料の酸化安定度試験］
　実施例３及び実施例４で軽油を元油として本発明の方法により得られた加水燃料の試料について、酸化安定度試験（試験方法：ASTM D2274）を行った。比較のため、元油として使用した軽油についても、同様の酸化安定度試験を行った。
　測定されたスラッジ量は、いずれの試料についても、測定限界である０．１ｍｇ／１００ミリリットルを下回っていた。 [Oxidation stability test of water fuel]
An oxidation stability test (test method: ASTM D2274) was conducted on the hydrofuel samples obtained by the method of the present invention using light oil as base oil in Example 3 and Example 4. For comparison, the same oxidative stability test was performed on light oil used as the base oil.
The measured amount of sludge was below the measurement limit of 0.1 mg / 100 ml for any sample.
［加水燃料による走行試験］
　実施例３で軽油を燃料元油として本発明の方法により得られた加水燃料について、ＪＣ０８モード走行試験を行った（使用車：日産自動車　ＮＶ３５０　型式ＬＤＦ－ＶＷ２Ｅ２６　重量１８４０ｋｇ）。比較のため、市販の軽油（ＪＩＳ２号）についても、同様の走行試験を行った。
　結果を表４に示す。参考のため、排ガス規制値も併記した。
　表４から、本発明の方法により得られた加水燃料では、特にＣＯ2排出量が市販の軽油に比べて低い点が注目される。
　実施例３で得られた加水燃料は、体積比率で４２％が水由来である。燃料元油に混合した水の燃料への転換率は、これまでの実験結果から略７０％と推定され、生成された燃料の総量のうち、水由来の燃料の体積比率は、式
　〔水由来の燃料の体積比率〕＝（４２×０．７）／（５８＋４２×０．７）＝３４％
により求めることができる。このことから、実施例３の場合には、得られた燃料のうち、３４％は石油由来でないと評価できる。したがって、実施例３により得られた燃料は、炭素排出量を３４％程度削減していると見ることができる。 [Running test with water fuel]
A JC08 mode running test was conducted on the hydrofuel obtained by the method of the present invention using light oil as a fuel base oil in Example 3 (vehicle used: Nissan Motor NV350 model LDF-VW2E26 weight 1840 kg). For comparison, a similar running test was performed on a commercially available light oil (JIS No. 2).
The results are shown in Table 4. For reference, emission control values are also shown.
From Table 4, it is noted that the hydrofuel obtained by the method of the present invention has a particularly low CO 2 emission compared to commercially available light oil.
The hydrous fuel obtained in Example 3 is 42% by volume derived from water. The conversion rate of water mixed with fuel base oil to fuel is estimated to be approximately 70% from the results of previous experiments, and the volume ratio of water-derived fuel out of the total amount of fuel produced is given by the formula [water-derived Fuel volume ratio] = (42 × 0.7) / (58 + 42 × 0.7) = 34%
It can ask for. From this, in Example 3, it can be evaluated that 34% of the obtained fuel is not derived from petroleum. Therefore, it can be seen that the fuel obtained in Example 3 has reduced carbon emissions by about 34%.
Figure JPOXMLDOC01-appb-T000004
Figure JPOXMLDOC01-appb-T000004
１　加水燃料製造装置
２　元油改善槽
３　精製水槽
４　反応促進剤注入部
５　反応槽
６　改善油静置槽
７　製品受槽
８　ヒータ
９　触媒
１０　超音波発生部
１１　ポンプ
１２　ＯＨＲミキサ
１３　反応槽容器
１４　噴射管
１５　排出口
２０　プラズマアーク処理装置
２１、２２　電極 DESCRIPTION OF SYMBOLS 1 Hydrolyzed fuel production apparatus 2 Original oil improvement tank 3 Purified water tank 4 Reaction accelerator injection | pouring part 5 Reaction tank 6 Improved oil stationary tank 7 Product receiving tank 8 Heater 9 Catalyst 10 Ultrasonic generator 11 Pump 12 OHR mixer 13 Reaction tank container 14 Injection tube 15 Discharge port 20 Plasma arc treatment device 21, 22 Electrode

Claims (21)

  1. 　燃料油と水とを混合して加水燃料を生成する加水燃料の製造方法であって、
    　水に電気的刺激を与えることによって水を活性化する水活性化工程と、
    　前記水活性化工程の前、前記水活性化工程中、又はその後で、水に添加剤として、カタラーゼ、水酸化ナトリウム、過酸化水素水溶液の少なくとも一つを添加する添加剤投入工程と
    　前記水活性化工程と前記添加剤投入工程とを経た水を燃料元油と混合し攪拌する攪拌混合工程と、
    　前記攪拌混合工程を経た燃料元油と水を、高温及び高圧のもとで融合する融合工程と、
    を少なくとも含む処理によって、水（Ｈ2Ｏ）を実質的に含まず、前記燃料元油と実質的に同等であるか、又はこれに近似する組成の加水燃料を生成する
    ことを特徴とする加水燃料の製造方法。     A method for producing a hydrolyzed fuel by mixing fuel oil and water to produce a hydrolyzed fuel,
    A water activation step of activating water by applying electrical stimulation to the water;
    Before the water activation step, during or after the water activation step, an additive charging step of adding at least one of catalase, sodium hydroxide, and aqueous hydrogen peroxide as an additive to water, and the water activity A stirring and mixing step of mixing and stirring the water that has undergone the conversion step and the additive charging step with the fuel base oil; and
    A fusion step of fusing the fuel base oil and water that have undergone the stirring and mixing step under high temperature and high pressure;
    The hydrous fuel having a composition substantially free of water (H 2 O) and substantially equivalent to or close to the fuel base oil is produced by the treatment containing at least water. Fuel manufacturing method.
  2. 　前記燃料元油に混合される前記水の比率は、体積比で、前記燃料元油１に対し水は約１以下であることを特徴とする請求項１に記載の加水燃料の製造方法。 The ratio of the water mixed with the fuel base oil is a volume ratio, and water is about 1 or less with respect to the fuel base oil 1.
  3. 　前記攪拌混合工程において、
    　まず、燃料元油のみを攪拌混合タンクに投入し、攪拌しながら、前記水活性化工程と添加剤投入工程を経た水を少量ずつ該燃料元油の液面に噴射して、該液面に強い波立ちを生じさせることにより、水を燃料元油に添加混合することを特徴とする請求項１又は請求項２に記載の加水燃料の製造方法。     In the stirring and mixing step,
    First, only the fuel base oil is charged into the stirring and mixing tank, and while stirring, the water that has passed through the water activation step and the additive charging step is injected little by little onto the liquid level of the fuel base oil. The method for producing a water-added fuel according to claim 1 or 2, wherein water is added to and mixed with the fuel base oil by generating strong undulations.
  4. 　前記攪拌混合工程において、
    　撹拌のために使用する前記攪拌混合タンクには、
    　円筒部分と、
    　前記イオン化工程と添加剤投入工程を経た水を該タンク内に噴射状態で投入する少なくとも一つの噴射管と、
    を備えるものを使用し、
    　該噴射管による前記水の噴射方向は、該円筒部分の中心軸と該噴射管が該円筒部分に取り付けられる取付点とを通る該円筒部分の直径線に対して約４０度から約５０度の範囲内となる角度を持つようにすることを特徴とする請求項１から３までのいずれか１項に記載の加水燃料の製造方法。     In the stirring and mixing step,
    In the stirring and mixing tank used for stirring,
    A cylindrical portion;
    At least one injection pipe for injecting water that has undergone the ionization step and the additive addition step into the tank in an injection state;
    Use the one with
    The direction of water injection by the spray tube is about 40 degrees to about 50 degrees with respect to the diameter line of the cylindrical portion passing through the central axis of the cylindrical portion and the attachment point where the spray tube is attached to the cylindrical portion. The method for producing a hydrolyzed fuel according to any one of claims 1 to 3, characterized in that the angle is within a range.
  5. 　前記攪拌混合タンクは複数個の前記噴射管を備えるものであり、複数の前記噴射管のそれぞれは、円筒部分の中心軸と該噴射管が該円筒部分に取り付けられる取付点とを通る該円筒部分の直径線に対する角度がほぼ同一となるように配置されたことを特徴とする請求項４に記載の加水燃料の製造方法。 The stirring and mixing tank includes a plurality of the injection pipes, and each of the plurality of injection pipes passes through a central axis of the cylindrical part and an attachment point where the injection pipe is attached to the cylindrical part. 5. The method for producing a hydrolyzed fuel according to claim 4, wherein the water is disposed so that the angles with respect to the diameter line are substantially the same.
  6. 　前記噴射管による前記水の噴射方向は、前記直径線に対して約４５度であることを特徴とする請求項４又は５に記載の加水燃料の製造方法。 The method for producing a water-added fuel according to claim 4 or 5, wherein the water injection direction of the injection pipe is about 45 degrees with respect to the diameter line.
  7. 　前記噴射管は、前記タンクの内部に突出する突出部を持つことを特徴とする請求項４から６までのいずれか１項に記載の加水燃料の製造方法。 The method for producing a water-added fuel according to any one of claims 4 to 6, wherein the injection pipe has a protruding portion protruding into the tank.
  8. 　前記突出部の長さは約１０ｃｍであり、該突出部の噴射口が前記タンク内の液面から少なくとも約８ｃｍ上方に離れて位置させられることを特徴とする請求項７に記載の加水燃料の製造方法。 The length of the protrusion is about 10 cm, and the injection port of the protrusion is positioned at least about 8 cm above the liquid level in the tank. Production method.
  9. 　前記添加剤投入工程において、カタラーゼを水に対する重量比で０．０４から０．０５％添加することを特徴とする請求項１から８までのいずれか１項に記載の加水燃料の製造方法。 9. The method for producing a hydrolyzed fuel according to any one of claims 1 to 8, wherein in the additive charging step, catalase is added in an amount of 0.04 to 0.05% by weight with respect to water.
  10. 　前記水活性化工程において、活性化された水は、ＯＲＰ値が１６０ｍＶから－２００ｍＶとなるようにすることを特徴とする請求項１から９までのいずれか１項に記載の加水燃料の製造方法。 The method for producing a water-added fuel according to any one of claims 1 to 9, wherein the water activated in the water activation step has an ORP value of 160 mV to -200 mV. .
  11. 　前記水活性化工程において、トルマリン又は銅イオン発生材料を水に接触させた状態にして、１０ＫＨｚから６０ＫＨｚまでと２００ＫＨｚ以上の２つの周波数の超音波を交互に水に照射することを特徴とする請求項１から１０までのいずれか１項に記載の加水燃料の製造方法。 In the water activation step, tourmaline or a copper ion generating material is brought into contact with water, and ultrasonic waves of two frequencies of 10 KHz to 60 KHz and 200 KHz or more are alternately irradiated to water. Item 11. A method for producing a water-added fuel according to any one of Items 1 to 10.
  12. 　前記融合工程において、加圧条件は約０．３Ｍｐａ以上とし、加熱条件は約４０℃から約８０℃までの範囲とすることを特徴とする請求項１から１１までのいずれか１項に記載の加水燃料の製造方法。 12. The fusion process according to claim 1, wherein in the fusion step, the pressurizing condition is about 0.3 Mpa or more, and the heating condition is in the range of about 40 ° C. to about 80 ° C. 12. A method for producing water.
  13. 　前記攪拌混合工程は、ＯＨＲミキサーを用いて行うことを特徴とする請求項１から１２までのいずれか１項に記載の加水燃料の製造方法。 The method for producing a hydrolyzed fuel according to any one of claims 1 to 12, wherein the stirring and mixing step is performed using an OHR mixer.
  14. 　燃料油と水とを混合して加水燃料を生成する加水燃料の製造装置において、
    　水に電気的刺激を与えて該水を活性化する水活性化装置と、
    　水に添加剤として、カタラーゼ、水酸化ナトリウム、過酸化水素水溶液の少なくとも一つを添加する添加剤投入装置と、
    　燃料元油と、前記水活性化装置と添加剤投入装置を経た水とを混合し攪拌する攪拌混合装置と、
    　前記攪拌混合装置を経た燃料元油と水の混合物を、高温及び高圧のもとで融合させる融合装置と、
    を備えた加水燃料の製造装置。     In the manufacturing apparatus of the water fuel which mixes fuel oil and water and produces | generates water fuel,
    A water activation device for activating the water by applying electrical stimulation to the water;
    An additive charging device for adding at least one of catalase, sodium hydroxide, and aqueous hydrogen peroxide as an additive to water;
    An agitation and mixing device that mixes and stirs fuel base oil and water that has passed through the water activation device and the additive charging device;
    A fusion device for fusing a mixture of fuel base oil and water that has passed through the stirring and mixing device under high temperature and high pressure;
    An apparatus for producing water-containing fuel.
  15. 　前記水活性化装置は、超音波発生装置を備えることを特徴とする請求項１４に記載の製造装置。 15. The manufacturing apparatus according to claim 14, wherein the water activation device includes an ultrasonic generator.
  16. 　前記水活性化装置は、触媒を収容する部分を備え、該触媒はトルマリンであることを特徴とする請求項１５に記載の製造装置。 The manufacturing apparatus according to claim 15, wherein the water activation device includes a portion for accommodating a catalyst, and the catalyst is tourmaline.
  17. 　前記水活性化装置は、プラズマアーク処理装置を備えることを特徴とする請求項１４又は１５に記載の製造装置。 The manufacturing apparatus according to claim 14 or 15, wherein the water activation device includes a plasma arc treatment device.
  18. 　前記水活性化装置は、触媒を収容する部分を備え、該触媒はアルミニウムであることを特徴とする請求項１７に記載の製造装置。 The manufacturing apparatus according to claim 17, wherein the water activation device includes a portion for accommodating a catalyst, and the catalyst is aluminum.
  19. 　前記攪拌混合装置は、大気に開放した開放系の攪拌混合タンクを備えることを特徴とする請求項１５から１８までのいずれか１項に記載の製造装置。 The manufacturing apparatus according to any one of claims 15 to 18, wherein the stirring and mixing apparatus includes an open-type stirring and mixing tank that is open to the atmosphere.
  20. 　前記攪拌混合装置は、攪拌混合すべき液体を前記攪拌混合タンクに噴射状態で投入する噴射管を備え、該噴射管は、前記攪拌混合タンク中の液面から上方に少なくとも８ｃｍ離れた高さに配置されていることを特徴とする請求項１９に記載の製造装置。 The stirring and mixing device includes an injection pipe for injecting the liquid to be stirred and mixed into the stirring and mixing tank in an injection state, and the injection pipe is at a height of at least 8 cm upward from the liquid level in the stirring and mixing tank. The manufacturing apparatus according to claim 19, wherein the manufacturing apparatus is arranged.
  21. 　前記融合装置は、ＯＨＲミキサーを備えることを特徴とする請求項１４から２０までのいずれか１項に記載の製造装置。 The manufacturing apparatus according to any one of claims 14 to 20, wherein the fusion apparatus includes an OHR mixer.
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