WO2018062345A1 - 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 - Google Patents

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 Download PDF

Info

Publication number
WO2018062345A1
WO2018062345A1 PCT/JP2017/035109 JP2017035109W WO2018062345A1 WO 2018062345 A1 WO2018062345 A1 WO 2018062345A1 JP 2017035109 W JP2017035109 W JP 2017035109W WO 2018062345 A1 WO2018062345 A1 WO 2018062345A1
Authority
WO
WIPO (PCT)
Prior art keywords
fuel
hydrocarbon
water
oil
base oil
Prior art date
Application number
PCT/JP2017/035109
Other languages
English (en)
French (fr)
Japanese (ja)
Inventor
青木　文男
Original Assignee
株式会社Ｔｒｉｓｔａｒｈｃｏ
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 株式会社Ｔｒｉｓｔａｒｈｃｏ filed Critical 株式会社Ｔｒｉｓｔａｒｈｃｏ
Priority to US16/337,824 priority Critical patent/US20200032153A1/en
Priority to JP2018542825A priority patent/JP6995373B2/ja
Publication of WO2018062345A1 publication Critical patent/WO2018062345A1/ja

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/32—Liquid carbonaceous fuels consisting of coal-oil suspensions or aqueous emulsions or oil emulsions
    • C10L1/328—Oil emulsions containing water or any other hydrophilic phase
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2200/00—Components of fuel compositions
    • C10L2200/02—Inorganic or organic compounds containing atoms other than C, H or O, e.g. organic compounds containing heteroatoms or metal organic complexes
    • C10L2200/0295—Water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2200/00—Components of fuel compositions
    • C10L2200/04—Organic compounds
    • C10L2200/0407—Specifically defined hydrocarbon fractions as obtained from, e.g. a distillation column
    • C10L2200/0438—Middle or heavy distillates, heating oil, gasoil, marine fuels, residua
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2250/00—Structural features of fuel components or fuel compositions, either in solid, liquid or gaseous state
    • C10L2250/06—Particle, bubble or droplet size
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/14—Injection, e.g. in a reactor or a fuel stream during fuel production
    • C10L2290/146—Injection, e.g. in a reactor or a fuel stream during fuel production of water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/24—Mixing, stirring of fuel components
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/34—Applying ultrasonic energy
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/36—Applying radiation such as microwave, IR, UV

Definitions

  • the present invention relates to a method for producing a hydrocarbon-based synthetic fuel equivalent to the base oil by adding water to the hydrocarbon-based fuel base oil.
  • Patent Document 1 proposes a method for producing a hydrolyzed fuel that increases the transparency of an emulsion state of a mixed solution by contacting with metal, stirring, and mixing. More specifically, Patent Document 1 describes a mixture of fuel oil and water to which catalase has been added while agitating and mixing natural ore or metal in a vibration wave excitation state in contact with the mixture, and further mixing the fuel oil and water that have been agitated and mixed.
  • a method is disclosed in which the liquid is heated to 30 ° C. to 150 ° C. and pressurized at 3 to 10 atm to fuse the fuel and water to increase the transparency of the mixture in the emulsion state.
  • fuel oil and water to which catalase is added are brought into contact with natural minerals or metals excited by vibration waves to subdivide the molecular aggregate of fuel oil and water, and then fuel oil and water. It is described that the fuel oil and water that have been stirred and mixed can be mixed by heating and pressurizing to increase the transparency of the emulsion state of the hydrolyzed fuel.
  • Patent Document 1 describes two examples, Example 1 and Example 2. In any of these Examples, water and fuel oil are mixed in equal amounts and undergo a fusion process. Shows that a transparent fuel oil was obtained.
  • Patent Document 1 states that this manufacturing method can prevent an oil-water separation phenomenon in an emulsion fuel having a hydrolysis rate of 50% or more.
  • Patent Document 1 The manufacturing method described in Patent Document 1 is based on the premise that hydrocarbons that are the source of combustion calories are reduced by adding water to fuel oil.
  • the hydrogen content of fuel oil is increased to compensate. That is, it is possible to increase the ratio of hydrogen contained by catalase by decomposing hydrogen peroxide into hydrogen and oxygen, releasing oxygen into the atmosphere as gas, and leaving hydrogen in the fuel oil.
  • the teaching there is a limit to compensate for the decrease in the hydrocarbon ratio due to water addition only by increasing the hydrogen content ratio, and the method taught in Patent Document 1 cannot be expected to significantly increase the amount of fuel.
  • Patent Document 2 discloses an emulsion fuel having the same quality and calorific value as a raw fuel oil without using a surfactant and without separating fuel oil and water over a long period of time.
  • a method by which can be produced is disclosed. In this method, water is made to come into contact with tourmaline irradiated with far-infrared ray microwaves or ultrasonic waves, and fuel oil is made to come into contact with titanium oxide balls to which an electromagnetic wave-responsive catalyst is applied. It consists of mixing water and fuel oil and applying heat and pressure while circulating the mixture.
  • This Patent Document 2 also describes that the hydrogen content is increased by the addition of catalase.
  • Patent Document 2 does not include technical teaching beyond Patent Document 1.
  • Non-Patent Document 1 A paper titled “An efficient way of producing fuel hydrocarbon from CO 2 and activated water” by Tadayuki Imanaka et al. Published on the web on August 29, 2015 by J-STAGE (Non-Patent Document 1) In the presence of a titanium dioxide catalyst, UV light and black light (wavelength 350 nm to 400 nm) are irradiated to generate activated water, and this activated water is mixed with light oil to make it stronger.
  • a method for producing synthetic oil by stirring is disclosed. In the method described in this paper, active water is mixed with light oil by a special mixer serving as a reaction layer, the mixed solution collides with the wall of the mixer, and the mixed solution is circulated so that the collision is repeated.
  • Tadayuki Imanaka et al. “An efficient way of producing fuel hydrocarbon from CO2 and activated water” J-STAGE August 29, 2015 on the web “Chemical application of cavitation; Application of Cavitation, Induced by Ultrasound” Shinobu Koda, IEICE Journal A Vol. J89-ANo.
  • An object of the present invention is to provide a method for producing a hydrocarbon-based synthetic fuel.
  • 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.
  • a method according to the present invention comprises adding hydrocarbon to a hydrocarbon-based fuel base oil to produce a hydrocarbon-based synthetic fuel oil having a volume larger than the volume of the hydrocarbon-based fuel base oil.
  • the hydrocarbon-based synthetic fuel oil produced by the production method is used as a fuel base oil in the production of the next hydrocarbon-based synthetic fuel oil, and the same steps are sequentially repeated a plurality of times.
  • a hydrocarbon-based synthetic fuel having a high water addition ratio is produced.
  • the method for producing a hydrocarbon-based synthetic fuel oil includes: a) An activated water generating step of performing an activation treatment on water to generate activated activated water; b) an agitation and mixing step of adding the activated water to a hydrocarbon-based fuel base oil that is initially used as a fuel base oil, and stirring and mixing for a predetermined time under a reactive environment; c) a fusion step of fusing the hydrocarbon fuel base oil and the activated water that have undergone the stirring and mixing step under a reactive environment; d) a primary produced hydrocarbon fuel oil collecting step for collecting a hydrocarbon produced fuel obtained from the mixture obtained through the fusion step as a primary produced hydrocarbon fuel oil; And then The primary product hydrocarbon fuel oil is used as a secondary fuel base oil, and the steps b), c) and d) are performed to collect the secondary product hydrocarbon fuel oil.
  • System fuel oil is sequentially used as the fuel base oil, and the process of steps b), c) and d) is repeated a plurality of times, so that water (H 2 O) having a volume larger than that of the initial fuel base oil is obtained. It does not substantially contain, but includes producing a multi-generation hydrocarbon-based synthetic fuel oil composed of a hydrocarbon-based fuel oil having a composition that is substantially equivalent to or close to that of the corresponding initial fuel base oil. .
  • a method for producing a hydrocarbon-based synthetic fuel oil includes: a) An activated water generating step of performing an activation treatment on water to generate activated activated water; b) an agitation and mixing step of adding the activated water to a hydrocarbon-based fuel base oil that is initially used as a fuel base oil, and stirring and mixing for a predetermined time under a reactive environment; c) a fusion step of fusing the hydrocarbon fuel base oil and the activated water that have undergone the stirring and mixing step under a reactive environment; d) A hydrocarbon system having a composition that is not substantially contained in water (H 2 O) and is substantially equivalent to or close to the initial fuel base oil by allowing the mixed solution that has undergone the fusion step to stand.
  • the stirring and mixing step and the fusion step are the steps of the hydrocarbon-based fuel base oil in which the volume of the primary-generated hydrocarbon fuel oil obtained by the primary-generation hydrocarbon-based fuel oil collecting step is used as the initial fuel base oil.
  • a multi-generation hydrocarbon-based synthetic fuel comprising a hydrocarbon-based fuel oil having a composition substantially free of water (H 2 O) and substantially equivalent to or close to the original fuel base oil Including producing oil.
  • the activated water preferably contains microbubble hot spots.
  • generation process is performed by irradiating an ultrasonic wave to this water in the state which heated up water to the temperature of the range of 35 to 45 degreeC, and applied the voltage.
  • the voltage is preferably applied by irradiating tourmaline immersed in water with ultrasonic waves to bring the tourmaline into an excited state.
  • a substance effective to retain the microbubble hot spots is added to the activated water.
  • the generation of hot spots of microbubbles is performed by irradiating water with ultrasonic waves having a frequency different from the frequency of ultrasonic waves irradiated to tourmaline.
  • the reactive environment in the stirring and mixing step can be formed by stirring water while irradiating water to which catalase has been added. Stirring is preferably performed so as to generate a strong wave at the liquid level of the mixture of water and fuel base oil.
  • the reactive environment in the stirring and mixing step can be formed by adding a photocatalyst to water and stirring while irradiating with ultraviolet light.
  • the fuel oil produced by the method of the present invention is a hydrocarbon-based synthetic fuel oil that 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 fuel base oil is a light oil used as a diesel fuel
  • a surprising result is obtained that the resultant synthetic fuel oil 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 synthetic 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 the mixture of the fuel base oil and water, and the carbon dioxide is decomposed and used for the reaction for generating the synthetic fuel. It is conceivable to obtain at least the majority of the carbon required.
  • the agitation and mixing step is performed in an open space to the atmosphere, the mixture is circulated in the agitation and mixing step so as to generate a strong wave at the liquid level of the mixture of fuel base oil and water.
  • 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 synthetic fuel can be obtained by addition.
  • carbon to be added charcoal obtained by carbonizing wood can be used.
  • powdered carbon used for industrial applications can also be used advantageously.
  • carbon monoxide gas or carbon dioxide gas may be added and decomposed in the same manner as in the case of carbon dioxide taken from the air, and used for the production of synthetic fuel.
  • 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 is too large, the reaction time required to produce a synthetic fuel 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 synthetic fuel can be produced in a sufficiently short time even when water is mixed at a ratio of about 1 to the fuel base oil 1 by volume ratio. 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 water is used as a high-speed jet. Is preferably sprayed onto 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 the additive addition step, it is preferable to add catalase in a weight ratio of 0.04 to 0.05% 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 in the range from 40 ° C to 80 ° C.
  • an OHR mixer can be used in the stirring and mixing step.
  • the present invention by the above-described method, it is possible to obtain a hydrocarbon-based synthetic fuel oil that is difficult to be separated into water and oil after being synthesized, or hardly separated. Further, by using the obtained synthetic fuel oil as a base oil, adding water thereto, and further repeating the same steps, a hydrocarbon-based synthetic fuel oil having a high water content can be efficiently produced.
  • the synthetic fuel oil produced by the method 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 will have composition and physical properties.
  • the hydrocarbon-based synthetic fuel oil of the present invention has a calorific value per unit amount equal to or higher than that of the existing fuel oil, and compared with the existing fuel oil, the combustion chamber and exhaust after combustion. There is an effect that there is little deterioration and corrosion of a pipe etc. Furthermore, the synthetic fuel oil of the present invention is excellent in complete combustibility, and it is difficult to produce carbon monoxide, and the effects such as low carbon monoxide emission are achieved.
  • FIG. 4 is a chart showing the results of GC-MS analysis of light oil used as base oil in one example of the present invention. It is a chart which shows the result of the GC-MS analysis about the other synthetic fuel obtained by using A heavy oil as a base oil by the method which concerns on the other Example of this invention.
  • FIG. 9 is a chart showing GC-MS analysis results for A heavy oil used as base oil in the example shown in FIG. 8.
  • 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 synthetic fuel manufacturing method 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 synthetic fuel production apparatus 1 includes a base oil improvement tank 2, a purified water tank 3, a reaction accelerator injection unit 4, a reaction tank 5, a stationary tank 6, and a product receiving tank. 7 is composed. The outline of the apparatus 1 will be described.
  • the fuel base oil is pretreated in the base oil improvement tank 2, the water is activated in the purified water tank 3, and the additive is supplied from the reaction accelerator injection unit 4 to a predetermined tank. throw into. Further, the fuel tank oil and water are stirred and mixed and fused in the reaction tank 5, and unnecessary residues such as scum are removed in the stationary tank 6. If necessary, the oil phase and the water phase are phase-separated. Then, hydrocarbon synthetic fuel oil as a product is introduced from the stationary tank 6 to 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.
  • This base oil improvement tank is intended to make the temperature of the oil suitable for mixing.
  • 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).
  • T thermocouple
  • the fuel base oil in the base oil improvement tank 2 is circulated by being taken out of the base oil improvement tank 2 by the pump 11 and reintroducing into the tank through the header pipe 202. May be. Further, oil molecules may be subdivided as a pretreatment using a catalyst.
  • the purified water tank 3 performs a water activation process.
  • the water used in the method of the present invention is preferably soft water, and therefore water is preferably supplied from the water softening device 301.
  • the purpose of the purified water tank 3 is to maintain the temperature of the water at a temperature suitable for mixing, and to subdivide the water molecules to an active level to obtain activated water containing microbubble spots.
  • 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.
  • the catalyst 9 in the purified water tank 3, it is preferable to use tourmaline or a copper ion generating material 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 action of the catalyst can be promoted by irradiating the catalyst 9 such as tourmaline or copper ion generating material immersed in the purified water tank 3 with ultrasonic waves.
  • the water may be circulated by taking out the water in the tank to the header 302 by the pump 11 and returning it again from the header 302 into the purified water tank 3 so that the activation is performed uniformly.
  • 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.
  • the activation of water can also be performed by plasma arc treatment of water configured to generate a discharge between electrodes connected to a high-voltage transformer and dissociate and ionize water 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 is a substance that achieves the action of decomposing hydrogen peroxide into hydrogen and oxygen and releasing the oxygen into the atmosphere as a gas. By this action, the hydrogen content ratio of the produced fuel oil can be increased to prevent the calorific value from decreasing.
  • catalase, sodium hydroxide, aqueous hydrogen peroxide solution or the like can be 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 the amount of catalase added is less than 0.04% by weight, the effect is weak, and if it exceeds 0.05%, it will not dissolve sufficiently and will increase the scum, which will lower the quality of the fuel oil produced. .
  • 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 container 13 of the reaction tank 5 through the injection pipe 14.
  • the mixed liquid of oil and water is taken out from the discharge port 15 of the container 13 of the reaction tank 5 by the pump 11, and in a pressurized state, passes through the OHR mixer 12 and reacts through the header pipe 502 and the injection pipe 14. It is circulated inside the container 13 of the tank 5.
  • the OHR mixer 12 is for efficiently mixing a plurality of substances.
  • this reaction tank 5 acts on a pressure of about 3 to 9 atm when used in the fusion process, it needs to have a structure that can withstand a higher pressure than other tanks.
  • the stationary tank 6 is a tank that temporarily stores the product solution after the fusion process. In this tank 6, scum generated by additives and the like is precipitated.
  • the synthetic fuel oil in which the oil and water are completely integrated and the impurities are separated by being left in the stationary tank 6, and the synthetic fuel oil as a supernatant is supplied to the product receiving tank 7.
  • the impurities include additives, and these impurities are returned to the reaction vessel 5.
  • the residence time in the stationary tank 6 is preferably about 1 hour.
  • the product receiving tank 7 is a tank for storing synthetic fuel oil produced as a product.
  • the produced synthetic fuel oil is supplied from the product receiving tank 7 to the product storage tank 701 at a stage where it is gathered to some extent.
  • the process for treating water includes a water activation process and an additive charging process.
  • the process of processing the fuel base oil includes a base oil improving process and an additive charging process.
  • the activated water that has undergone the water activation process and additive feeding process and the fuel base oil that has undergone the base oil improvement process and additive feeding process are agitated and mixed in the agitation and mixing process, and the primary production synthetic oil is produced through the fusion process. Is done. If necessary, a filtration step is performed before removal of the primary synthetic oil.
  • the activation process is performed in the purified water tank 3.
  • the water molecule aggregate is subdivided to the active level.
  • the affinity with the fuel base oil molecules is improved, and more water can be used for the production of synthetic fuel.
  • Water is put into the purified water tank 3, and ultrasonic waves are irradiated to the water by the ultrasonic wave generation unit 10, and the water is vibrated at a high frequency, thereby promoting the fragmentation of water molecules.
  • Ultrasonic irradiation can promote subdivision of water by alternately irradiating ultrasonic waves having two different frequencies.
  • 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.
  • the ultrasonic wave generation part 10 when using the ultrasonic wave generation part 10, it is effective to give an electrical stimulus to water using a substance such as tourmaline or a copper ion generating material as a catalyst.
  • a substance such as tourmaline or a copper ion generating material as a catalyst.
  • electrical stimulation is given to the water, and microbubble hot spots are formed in the water.
  • the degree of conversion can be increased.
  • 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 -790 mV, more preferably 30 mV to -600 mV.
  • the normal tap water ORP is 700 mV to 500 mV.
  • oxygen is released from water, and the hydrogen content ratio of water 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 is to increase the hydrogen content ratio of water by adding the additive stored in the reaction accelerator injecting 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 made uniform and are easily fused with water.
  • the activated water is poured from the purified water tank 3 into the reaction tank 5 little by little. This is because water is dispersed as uniformly as possible in the fuel base oil.
  • the activated water supplied from the purified water tank 3 is pressurized by the pump 11 of the purified water tank 3, mixed with the fuel base oil taken out from the discharge port 15 of the reaction tank 5, and 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.
  • the activated water and the fuel base 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 change.
  • the mixture of the activated water and fuel base oil is circulated through a pipe having a pipe size of 15 A to 50 A at a flow rate of 20 L / min to 50 L / min. It is preferable to make it.
  • the mixing time can be about 5 minutes to 1 hour.
  • the fusion process In the fusion process, the input of the activated water from the purified water tank 3 to the reaction tank 5 is completed, and the fusion process is performed by circulating the mixture of the activated water and the fuel base oil through the OHR mixer 12. Is done.
  • the pressure is preferably 3 atm (0.3 MPa) or more, which is the same as in the stirring and mixing step, and the temperature is preferably 40 ° C to 80 ° C.
  • the mixture of activated water and fuel base oil is passed through the OHR mixer 12 for a sufficient period of time, so that the activated water and the oil are fused and the hydrocarbon-based synthetic fuel oil that is not likely to be separated. Can be obtained.
  • the pressure applied to the mixed liquid is 0.3 MPa (3 atm) or more.
  • the temperature may be 70 ° C. or lower. It is most effective that the pressure applied in the fusion process is 0.9 MPa and the temperature is 50 ° C.
  • the reaction time is suitably 20 to 60 minutes after reaching the pressure and temperature.
  • the filtration step is a step of separating the scum-like product from the coagulation of the components of the enzyme and other components when the enzyme is used at the time of production from the completely produced synthetic fuel.
  • the method using the 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 synthetic fuel collects in the upper layer because of its low specific gravity. By sending the upper layer synthetic fuel to the product receiving tank 7, a hydrocarbon-based synthetic fuel oil as a product can be obtained.
  • the mixed liquid residence time in the stationary tank 6 is desirably 1 hour or longer.
  • synthetic fuel and scum can also 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 when passing through a pipe having a pipe size of 20 A to 50 A, but the speed is more moderate. desirable.
  • the number of passes through the filtration filter can be one or more.
  • FIG. 3 is a view showing the structure of a liquid injection pipe to the reaction vessel 5 that can be used in the production apparatus according to the present invention.
  • FIG. 3A is a view seen from above for showing the positional relationship between the reaction vessel 5 and the injection pipe 14.
  • FIG. 3B is a side view of the reaction vessel 5.
  • 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 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.
  • 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 generated synthetic fuel oil 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 by changing by 10 cm. As a result, it was found that when the protrusion amount was 10 cm, the time required for fusion was the shortest and the quality of the produced synthetic fuel oil 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.
  • the reaction of the injection tube 14 is performed. It may be considered that 10 cm is optimal for the amount of protrusion into the tank 5.
  • a natural vortex can be created in the vessel. 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 processing apparatus 20 is arranged so as to surround the center electrode and an electrode 21 (shown by a hexagon in the figure) each connected to a high voltage transformer (not shown).
  • a plurality of (in the figure, 12) 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.
  • 3 kg of tourmaline is immersed in 20 liters of water at room temperature, and ultrasonic waves with a frequency of 30 kHz to 40 kHz are irradiated to tourmaline, and ultrasonic waves with a frequency of 200 kHz to 600 kHz are irradiated to water for 20 minutes.
  • the frequency of ultrasonic waves irradiated to tourmaline was 35 kHz
  • the frequency of ultrasonic waves irradiated to water was 400 kHz.
  • the ultrasonic irradiation was continued, and the temperature was raised to a water temperature of 43 ° C. using a heater while circulating water with a pump.
  • microbubbles mean microbubbles generated by local pressure fluctuation when water is irradiated with ultrasonic waves. Shinobu Koda from the graduate School of Engineering, Nagoya University J89-ANo. 9 (2006), a paper titled “Chemical application of cavitation: Application of cavitation Induced by Ultrasound,” published by Kanto Chemical Co., Ltd.
  • a primary synthetic fuel oil 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). 3kg and 20 liters of tap water were added (a small-sized tourmaline ore imported from New Wave Co., Ltd.) To this water, 20 ml of catalase (Leonet F-35 manufactured by Nagase ChemteX Corporation) was added.
  • the ultrasonic vibrator was actuated, and water circulation was started by a circulation pump while irradiating tourmaline and water under the conditions described in “Formation example 1 of activated water”.
  • 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, when the redox potential of water in the container was measured with an ORP meter, it was 12 mV, and it was confirmed that the water was activated.
  • 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 A heavy oil thus obtained were mixed and stirred as follows, and then the mixed solution was heated and applied with pressure to be fused. That is, in addition to a thermometer, a 1 kW heating heater and a rotary vane type stirrer were provided, and an open system container having a volume of 25 liters opened to the atmosphere, and 10 liters of activated water was obtained. 10 liters of heavy oil was added.
  • the container had a configuration in which a circulation pump and a mixing mixer (OHR mixer manufactured by OHR Fluid Engineering Laboratory Co., Ltd.) were connected. In the container containing the activated water and A heavy oil, the heating heater was turned on so that the temperature of the liquid in the container was maintained at 40 ° C.
  • a synthetic fuel oil was produced in the same manner as in Production Example 1 except that a commercial diesel oil (No. 2 diesel oil purchased from JX Energy Co., Ltd. (ENEOS)) was used as the base oil instead of A heavy oil. Therefore, 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 synthetic fuel oil produced in the primary synthetic fuel oil production examples 1 and 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, when looking at the item of moisture, it can be seen that in both Production Example 1 and Production Example 2, the volume% of moisture in the synthetic fuel oil is 0.00% and substantially does not contain water. Since fuel oil and water are mixed one-to-one and fused, if sufficient fusion is not achieved, the amount of water should be detected.
  • the volume% of water being 0.00% indicates that the fuel base oil and water are completely fused and not analyzed as a water component.
  • the fuel base oil and water can be completely fused to produce a high-quality hydrocarbon-based synthetic fuel oil.
  • a synthetic fuel was produced using an apparatus as shown in FIGS. 2 and 3 and using light oil as the base oil.
  • 150 liters of tap water was injected into a purified water tank filled with the same tourmaline as used in Production 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 Production Example 1 was added.
  • the circulating pump connected to the purified water tank is operated (discharge pressure 0.5 MPa), the ultrasonic generator installed in the purified water tank is operated, and the temperature of the water reaches 40 ° C. for 60 minutes, 40 ° C.
  • ultrasonic waves (frequency: 40 kHz) were irradiated to tourmaline and water for another 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. In this way, activated water was obtained.
  • the activated water and light oil thus obtained were mixed in a reaction vessel and stirred. Further, the activated water and light oil were heated and fused by applying pressure. More specifically, 75 liters of base oil from the base oil improvement tank and 55 liters of activated water from the purified water tank were transferred to the reaction tank (hydration rate of about 42%). 65 ml of the same catalase used in Production Example 1 was added to the reaction vessel. Next, 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 positioned about 8 cm above the liquid level of the mixed liquid in the reaction tank. A sample of synthetic fuel oil for analysis was taken from the resulting liquid. The amount of sample collected was 114 liters.
  • the temperature of the refined water tank, the base oil improvement tank, and the reaction tank is higher than that in Production Example 3, and is set to 42 ° C, 41 ° C, and 44 ° C, respectively, and the circulation time in the refined water tank and the base oil improvement tank
  • a synthetic fuel oil was produced by carrying out the same steps as in Production Example 3 except that it was half of that in Production 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 of synthetic fuel oil for analysis was taken from the liquid obtained in the reaction vessel. The amount of sample collected was 114 liters.
  • a heavy oil (type 1 No. 1 A heavy oil purchased from Fujikosan Co., Ltd.) is used as the base oil, the reaction tank temperature is set to 36 ° C., and the circulation time in the refined water tank and the base oil improvement tank is both 90 minutes.
  • a synthetic fuel was produced in the same manner as in Production Example 3, except that the amounts of catalase added to the purified water tank and the reaction tank were 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 of synthetic fuel oil for analysis was taken from the liquid obtained in the reaction vessel. The amount of sample collected was 114 liters.
  • Table 2 shows the component analysis results of the hydrocarbon-based synthetic fuel oil produced in Production Examples 4 and 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 on the synthetic fuel sample obtained in Production Example 4.
  • the results are shown in FIG.
  • the same qualitative analysis was performed on light oil used as the fuel base oil.
  • the results are shown in FIG.
  • FIG. 5 and FIG. 6 are compared with FIG. 7, the hydrocarbons obtained in Production Examples 3 and 4 have a tendency to reduce the components having a large number of carbon atoms (those larger than C19) compared to the base oil. It was confirmed that the component composition of the system synthetic fuel oil is in good agreement with the base oil.
  • oxidation stability test of primary production synthetic fuel oil An oxidation stability test (test method: ASTM D2274) was performed on samples of the primary production synthetic fuel oil obtained by the method of the present invention using light oil as the base oil in Production Examples 3 and 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.
  • the primary production synthetic fuel oil obtained by the method of the present invention using light oil as the fuel base oil in Production Example 3 was subjected to a JC08 mode running test (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 primary produced synthetic fuel oil obtained by the method of the present invention has a lower CO 2 emission than that of commercially available light oil.
  • the primary production synthetic fuel oil obtained in Production Example 3 is 42% by volume derived from water.
  • Example 1 As an example of the present invention, the synthetic fuel oil produced in the primary fuel oil production example 6 was used as a base oil to produce a secondary synthetic fuel oil. Specifically, 10 liters of the synthetic fuel oil produced in the primary fuel oil production example 6 was adjusted through the base oil improvement tank 2 and then charged into the reaction tank 5. At the same time, 5 liters of activated water formed by the procedure described in “Formation of activated water” was charged into the reaction vessel 5 and the mixing, stirring, and fusion steps were performed under the same conditions as in Production Example 2. . Then, the produced
  • the oil present in the upper oil phase was taken out as a secondary generated synthetic fuel oil.
  • the amount of the secondary production synthetic fuel oil taken out was 11 liters.
  • the amount of water remaining in the aqueous phase was 4 liters.
  • the secondary synthetic fuel oil was increased by 10% compared to the primary synthetic fuel oil used as the base oil.
  • the secondary synthetic fuel oil obtained by the above process was used as a base oil to produce a tertiary synthetic fuel oil.
  • 10 liters of the secondary synthetic fuel oil produced in the above process was adjusted through the base oil improvement tank 2 and then charged into the reaction tank 5.
  • 5 liters of activated water formed by the procedure described in “Formation of activated water” was charged into the reaction vessel 5 and the mixing, stirring, and fusion steps were performed under the same conditions as in Production Example 2. .
  • generated liquid mixture was moved to the stationary tank 6, and left still for 1 hour. As a result, the mixed solution was phase-separated into an upper oil phase and a lower aqueous phase.
  • the oil present in the upper oil phase was taken out as the tertiary production synthetic fuel oil.
  • the amount of the tertiary production synthetic fuel oil taken out was 11 liters.
  • the amount of water remaining in the aqueous phase was 4 liters.
  • the amount of the tertiary generated synthetic fuel oil is increased by 10% compared to the secondary generated synthetic fuel oil used as the base oil.
  • the calorific value measurement and component analysis of the primary product synthetic fuel oil produced in the primary fuel oil production example 6 and the secondary product synthetic fuel oil produced in Example 1 were performed.
  • the results are shown in Table 5 in comparison with the commercially available diesel oil used as the base oil in the primary fuel oil production example 6.
  • the first embodiment is an example in which the primary production synthetic fuel oil produced in the primary fuel oil production example 6 is used as the base oil, but the primary production synthetic fuel oil produced in the primary fuel oil production examples 1 to 5 is used as the base oil.
  • a synthetic fuel oil can be produced.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Liquid Carbonaceous Fuels (AREA)
PCT/JP2017/035109 2016-09-30 2017-09-28 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 WO2018062345A1 (ja)

Priority Applications (2)

Application Number Priority Date Filing Date Title
US16/337,824 US20200032153A1 (en) 2016-09-30 2017-09-28 Method for Producing HydroCarbon-Based Synthetic Fuel By Adding Water to Hyrocarbon-Based Fuel Oil
JP2018542825A JP6995373B2 (ja) 2016-09-30 2017-09-28 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

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2016193904 2016-09-30
JP2016-193904 2016-09-30

Publications (1)

Publication Number Publication Date
WO2018062345A1 true WO2018062345A1 (ja) 2018-04-05

Family

ID=61759831

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/JP2017/035109 WO2018062345A1 (ja) 2016-09-30 2017-09-28 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

Country Status (4)

Country Link
US (1) US20200032153A1 (zh)
JP (1) JP6995373B2 (zh)
TW (1) TW201827582A (zh)
WO (1) WO2018062345A1 (zh)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
JP6976016B1 (ja) * 2021-05-11 2021-12-01 ガルファ株式会社 化石資源増量装置

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2013216794A (ja) * 2012-04-10 2013-10-24 Shinji Hasegawa 燃料油と水との混合による改質燃料の製造方法及び製造装置
WO2013186936A1 (ja) * 2012-06-15 2013-12-19 Kobayashi Hiroshi 新燃料及び新燃料の製造方法
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
WO2016159254A1 (ja) * 2015-04-01 2016-10-06 株式会社Ｔｒｉｓｔａｒｈｃｏ 加水燃料の製造方法及び製造装置
JP6128453B1 (ja) * 2016-09-09 2017-05-17 古山　幹雄 加水燃料の製造方法及び製造装置

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20140101532A (ko) * 2013-02-12 2014-08-20 가부시키가이샤 클라이막스 쟈판 연료유에 물을 가하면서 개질연료를 제조하는 제조방법과 그 제조장치
KR101328151B1 (ko) * 2013-04-11 2013-11-13 고천일 개질연료 제조장치 및 제조방법
US20180037823A1 (en) * 2016-08-02 2018-02-08 Bio Hitech Energy Co. Manufacturing apparatus and method for fuel hydrocarbon

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2013216794A (ja) * 2012-04-10 2013-10-24 Shinji Hasegawa 燃料油と水との混合による改質燃料の製造方法及び製造装置
WO2013186936A1 (ja) * 2012-06-15 2013-12-19 Kobayashi Hiroshi 新燃料及び新燃料の製造方法
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
WO2016159254A1 (ja) * 2015-04-01 2016-10-06 株式会社Ｔｒｉｓｔａｒｈｃｏ 加水燃料の製造方法及び製造装置
JP6128453B1 (ja) * 2016-09-09 2017-05-17 古山　幹雄 加水燃料の製造方法及び製造装置

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
JP6976016B1 (ja) * 2021-05-11 2021-12-01 ガルファ株式会社 化石資源増量装置
WO2022239258A1 (ja) * 2021-05-11 2022-11-17 ガルファ株式会社 化石資源増量装置

Also Published As

Publication number Publication date
JP6995373B2 (ja) 2022-01-14
TW201827582A (zh) 2018-08-01
US20200032153A1 (en) 2020-01-30
JPWO2018062345A1 (ja) 2019-10-10

Similar Documents

Publication Publication Date Title
Kaptakov Catalytic Desulfuration of Oil Products under Ultrasonic Treatment.
US9493709B2 (en) Hybrid fuel and method of making the same
Bulychev et al. Hydrogen production by low-temperature plasma decomposition of liquids
US9567542B2 (en) Hybrid fuel and method of making the same
JP4682287B1 (ja) 加水燃料の製造方法及び製造装置
Cako et al. Cavitation based cleaner technologies for biodiesel production and processing of hydrocarbon streams: A perspective on key fundamentals, missing process data and economic feasibility–A review
JP6146789B2 (ja) 加水燃料の製造方法及び製造装置
WO2018062345A1 (ja) 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
JP2017209646A (ja) 液体処理装置
Cherpozat et al. Ultrasonic pretreatment of soft wood biomass prior to conventional pyrolysis: Scale-up effects and limitations
JP2016003297A (ja) 加水燃料の製造方法及び加水燃料
CA2952768A1 (en) Hybrid fuel and method of making the same
JP2017119775A (ja) 新燃料、新燃料製造装置及び新燃料の製造方法
CN104692484A (zh) 一种采用钛铝双金属电极进行微等离子体弧放电催化水处理方法
RU2422493C1 (ru) Способ крекинга углеводородов и плазменный реактор для его осуществления
JP6541230B2 (ja) 油水融合燃料の製造方法
Jiang et al. Study on synergistic catalytic degradation of wastewater containing polyacrylamide catalyzed by low-temperature plasma-H2O2
JPH11140470A (ja) 水−化石燃料混合エマルジョン
JP2014047229A (ja) 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
RU2451715C1 (ru) Способ и установка плазмотермической переработки углеродсодержащих промышленных и сельскохозяйственных отходов для получения плазмогаза
JP2019189870A (ja) 加水燃料の製造方法及び製造装置
Li et al. High efficiency and rapid treatment of naproxen sodium wastewater by dielectric barrier discharge coupled with catalysis
WO2005009607A1 (fr) Procede permettant de lancer des reactions en chaine de dissociation et de polycondensation d'hydrocarbures, et dispositif permettant sa mise en oeuvre
WO2016022090A1 (en) Hybrid fuel and method of making the same
JP2022046394A (ja) 水または燃料油改質装置

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 17856294

Country of ref document: EP

Kind code of ref document: A1

ENP Entry into the national phase

Ref document number: 2018542825

Country of ref document: JP

Kind code of ref document: A

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 17856294

Country of ref document: EP

Kind code of ref document: A1