WO2016159254A1 - Procédé et appareil de production d'un combustible hydraté - Google Patents

Procédé et appareil de production d'un combustible hydraté 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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Prior art keywords
water
fuel
stirring
tank
base oil
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PCT/JP2016/060712
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English (en)
Japanese (ja)
Inventor
青木　文男
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株式会社Ｔｒｉｓｔａｒｈｃｏ
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Priority to JP2016523340A priority Critical patent/JP6146789B2/ja
Priority to US15/563,413 priority patent/US20180086997A1/en
Publication of WO2016159254A1 publication Critical patent/WO2016159254A1/fr

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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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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Liquid Carbonaceous Fuels (AREA)

Abstract

L'invention concerne un procédé de production d'un combustible hydraté et un appareil de production capable de produire un combustible hydraté ayant essentiellement ou approximativement la même composition et les mêmes propriétés physiques que le mazout-source, qui est le combustible avant hydratation, et ayant également des propriétés similaires au mazout-source en termes de séparation huile-eau. Le procédé de production de combustible hydraté comprend au moins : une étape d'activation de l'eau pour activer les molécules d'eau par application d'une stimulation électrique à l'eau à l'aide d'un procédé tel qu'une application d'électricité à haute tension; une étape d'agitation/mélange pour mélanger et agiter le mazout-source avec l'eau qui a subi l'étape d'activation de l'eau, tout en ajoutant, à titre d'additif à l'eau, au moins une solution de catalase et/ou d'hydroxyde de sodium et/ou une solution aqueuse de peroxyde d'hydrogène; et une étape de fusion pour porter à fusion le mazout-source et l'eau, à une température élevée et pression élevée, pendant ou après l'étape d'agitation/mélange.
PCT/JP2016/060712 2015-04-01 2016-03-31 Procédé et appareil de production d'un combustible hydraté WO2016159254A1 (fr)

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WO2018062345A1 (fr) * 2016-09-30 2018-04-05 株式会社Ｔｒｉｓｔａｒｈｃｏ Procédé de production de combustible synthétique à base d'hydrocarbure par ajout d'eau à une huile combustible à base d'hydrocarbure
JP2020029483A (ja) * 2018-08-20 2020-02-27 株式会社アイティー技研 液体炭化水素の製造方法及び装置

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WO2021009910A1 (fr) 2019-07-18 2021-01-21 日本電信電話株式会社 Panneau aveugle

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JP4682287B1 (ja) * 2010-06-11 2011-05-11 佳右 長尾 加水燃料の製造方法及び製造装置
JP2014047229A (ja) * 2012-08-29 2014-03-17 Kiyozo Okada 水と油との混合物であるエマルジョン燃料の製造方法、エマルジョン燃料、及びエマルジョン燃料の製造装置
JP2016003297A (ja) * 2014-06-18 2016-01-12 合同会社ネクストエナジー 加水燃料の製造方法及び加水燃料

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JPS5867325A (ja) * 1981-10-16 1983-04-21 宝栄工業株式会社 エマルジヨン生成装置
JP2009191261A (ja) * 2008-01-15 2009-08-27 Yoshisuke Nagao エマルジョン燃料の製造方法
JP4682287B1 (ja) * 2010-06-11 2011-05-11 佳右 長尾 加水燃料の製造方法及び製造装置
JP2014047229A (ja) * 2012-08-29 2014-03-17 Kiyozo Okada 水と油との混合物であるエマルジョン燃料の製造方法、エマルジョン燃料、及びエマルジョン燃料の製造装置
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WO2018062345A1 (fr) * 2016-09-30 2018-04-05 株式会社Ｔｒｉｓｔａｒｈｃｏ Procédé de production de combustible synthétique à base d'hydrocarbure par ajout d'eau à une huile combustible à base d'hydrocarbure
JPWO2018062345A1 (ja) * 2016-09-30 2019-10-10 株式会社Ｔｒｉｓｔａｒｈｃｏ 炭化水素系燃料油に水を添加して炭化水素系合成燃料を製造する方法
JP6995373B2 (ja) 2016-09-30 2022-01-14 株式会社Tristarhco 炭化水素系燃料油に水を添加して炭化水素系合成燃料を製造する方法
JP2020029483A (ja) * 2018-08-20 2020-02-27 株式会社アイティー技研 液体炭化水素の製造方法及び装置

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JP6146789B2 (ja) 2017-06-14
JP2017155244A (ja) 2017-09-07

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