WO2021148673A1 - Système et procédé de production d'une dispersion stable d'hydrocarbures et d'eau pour améliorer les processus de combustion, et une dispersion eau-hydrocarbure qui est facilement séparable en au moins deux phases en tant que partie du processus de nettoyage à des emplacements d'accident - Google Patents

Système et procédé de production d'une dispersion stable d'hydrocarbures et d'eau pour améliorer les processus de combustion, et une dispersion eau-hydrocarbure qui est facilement séparable en au moins deux phases en tant que partie du processus de nettoyage à des emplacements d'accident Download PDF

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Publication number
WO2021148673A1
WO2021148673A1 PCT/EP2021/051598 EP2021051598W WO2021148673A1 WO 2021148673 A1 WO2021148673 A1 WO 2021148673A1 EP 2021051598 W EP2021051598 W EP 2021051598W WO 2021148673 A1 WO2021148673 A1 WO 2021148673A1
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WO
WIPO (PCT)
Prior art keywords
dispersion
hydrocarbon
water
disperser
medium
Prior art date
Application number
PCT/EP2021/051598
Other languages
German (de)
English (en)
Inventor
Dimitrij Bieren
Jürgen Gärtner
Kerstin SELKA
Sergej Nikolaeviz TUMAKOV
Original Assignee
Raptech Eberswalde Gmbh
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Publication date
Application filed by Raptech Eberswalde Gmbh filed Critical Raptech Eberswalde Gmbh
Priority to EP21703372.9A priority Critical patent/EP4093535B1/fr
Publication of WO2021148673A1 publication Critical patent/WO2021148673A1/fr

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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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/40—Mixing liquids with liquids; Emulsifying
    • B01F23/41—Emulsifying
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/40—Mixing liquids with liquids; Emulsifying
    • B01F23/45—Mixing liquids with liquids; Emulsifying using flow mixing
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/70—Pre-treatment of the materials to be mixed
    • B01F23/711—Heating materials, e.g. melting
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/10—Mixing by creating a vortex flow, e.g. by tangential introduction of flow components
    • B01F25/102—Mixing by creating a vortex flow, e.g. by tangential introduction of flow components wherein the vortex is created by two or more jets introduced tangentially in separate mixing chambers or consecutively in the same mixing chamber
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/20—Measuring; Control or regulation
    • B01F35/22—Control or regulation
    • B01F35/221—Control or regulation of operational parameters, e.g. level of material in the mixer, temperature or pressure
    • B01F35/2213—Pressure
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/71—Feed mechanisms
    • B01F35/717—Feed mechanisms characterised by the means for feeding the components to the mixer
    • B01F35/7176—Feed mechanisms characterised by the means for feeding the components to the mixer using pumps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/75—Discharge mechanisms
    • B01F35/754—Discharge mechanisms characterised by the means for discharging the components from the mixer
    • B01F35/7544—Discharge mechanisms characterised by the means for discharging the components from the mixer using pumps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/90—Heating or cooling systems
    • B01F2035/99—Heating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F2101/00—Mixing characterised by the nature of the mixed materials or by the application field
    • B01F2101/505—Mixing fuel and water or other fluids to obtain liquid fuel emulsions
    • 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
    • C10L2250/00—Structural features of fuel components or fuel compositions, either in solid, liquid or gaseous state
    • C10L2250/08—Emulsion details
    • C10L2250/082—Oil in water (o/w) emulsion
    • 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
    • C10L2290/46—Compressors or pumps
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02M—SUPPLYING COMBUSTION ENGINES IN GENERAL WITH COMBUSTIBLE MIXTURES OR CONSTITUENTS THEREOF
    • F02M25/00—Engine-pertinent apparatus for adding non-fuel substances or small quantities of secondary fuel to combustion-air, main fuel or fuel-air mixture
    • F02M25/022—Adding fuel and water emulsion, water or steam
    • F02M25/0228—Adding fuel and water emulsion

Definitions

  • the present invention relates to a plant for producing a stable hydrocarbon-water dispersion and a method for producing such a dispersion using thermal cavitation and supercavitation
  • the present invention relates to a plant for the production of a water-hydrocarbon dispersion which can easily be separated into at least two phases, as well as a process for the production of this dispersion and subsequent phase separation.
  • emulsifiers which the two Coupling heterogeneous phases
  • WO 01/55282 describes an emulsifier system for fuel-water emulsions which comprises alkoxyals of polyisobutene.
  • alcohols, peroxides and surfactants as additives for the production of microemulsions in internal combustion engines is known from WO 2011/042432.
  • the object of the present invention is to provide a stable hydrocarbon-water dispersion, in particular a stable fuel-water dispersion, the use of additives such as emulsifiers being dispensed with.
  • UADA versions without and with an integrated premixer.
  • the first version does not contain an integrated premixer for mixing the media.
  • the media are mixed with one another directly in the pre-mixer of the UADA body, which is integrated in the pre-sonic camera.
  • the first embodiment is used. More information on the two modifications can be found in patent RU 2130503 C1, RU 2462301 C1 and the patent for the useful technical model RU 134076 U1. The technical description of the UADA body and the acoustic panel are shown in FIGS.
  • upstream of the at least one unit for producing a hydrocarbon-water dispersion at least one premixing unit for producing a coarse dispersion from the at least one medium 1 and medium 2 is connected upstream.
  • the coarse disperser consists of at least two supply lines for two different media, each with a heat exchanger, an adjustment device for the media ratio and a premixer.
  • the premixer or coarse disperser is covered in claim 3.
  • the coarse disperser is the preliminary stage of the fine disperser (claim 2) or ultrafine disperser (claim 5).
  • a plant for the production of a stable hydrocarbon-water fine dispersion or a water-hydrocarbon separating dispersion (a water-hydrocarbon dispersion easily separable into at least two phases, or unstable separating dispersion) is provided, the plant having at least one unit to produce a hydrocarbon-water dispersion in the fine disperser from at least medium 1 as a hydrocarbon-containing medium and medium 2 as water (deionized water) and this unit has at least one premixer (coarse disperser), at least one first pump, for increasing pressure in the feed of the hydrocarbon-water mixture into the ultrasonic acoustic flow unit (UADA as part of the fine disperser); at least one ultrasonic acoustic flow unit (UADA) for the production of a hydrocarbon-water fine dispersion by means of hydrodynamic cavitation and at least one second pump for generating a negative pressure behind the UADA, or at least one unit for producing an unstable water-hydro
  • the present system thus comprises in the first aspect a fine disperser consisting of a coarse disperser, a UADA module and a pump upstream of the UADA and a pump downstream of the UADA and separating disperser consisting of a UADA module and a pump upstream of the UADA and a pump downstream of the UADA.
  • a plant for producing a stable hydrocarbon-water ultrafine dispersion comprises the ultrafine disperser downstream at least one unit for producing an ultrafine dispersion, from at least medium 1 as a hydrocarbon-containing medium and medium 2 as water (fully demineralized water) and at least one unit a heating device for initiating thermal cavitation, at least one first pump, for increasing the pressure in the inflow of the fine dispersion into the ultrasonic acoustic flow unit (UADA as part of the ultrafine disperser); at least one ultrasonic acoustic flow unit (UADA) for the production of a hydrocarbon-water ultrafine dispersion by means of hydrodynamic cavitation and at least one second pump for generating a negative pressure behind the ultrafine UADA or a unit of at least one premixer (coarse disperser), at least a heating device for initiating thermal cavitation, at least one first pump, for increasing the pressure in the inflow of the fine dispersion into the ultrasonic acoustic flow unit
  • the present system thus comprises in a second aspect a combination of an ultrafine disperser consisting of a heating device (heating cartridge with a screw-in heater) and UADA, the structure being as follows: heating device- first pump- first UADA- second pump (claims 8 and 8) 9) or consisting of a premixer (coarse disperser), a heating device (heating cartridge with a screw-in heater) and UADA, the structure being as follows: coarse disperser heating device - first pump - first UADA - second pump.
  • the object of the present invention is also achieved with a method having the features of claim 4, FIG. 5.
  • at least one ultrasonic acoustic flow unit (UADA) for producing a hydrocarbon-water fine dispersion by means of hydrodynamic cavitation, at least one heating device for initiating thermal cavitation,
  • at least one second pump for increasing the pressure in the inflow of the fine dispersion into the ultrasonic acoustics -Flow-through unit (UADA as part of the ultrafine disperser);
  • at least one second ultrasonic acoustic flow unit (UADA) for producing a hydrocarbon-water ultrafine dispersion by means of hydro
  • the present system thus comprises in a third aspect a combination of a coarse disperser, a fine disperser and a downstream ultrafine disperser.
  • the object of the present invention is also achieved with a method having the features of claim 6, FIG. 2.
  • the basis of the present system and the process is the principle of cavitation. Cavitation is the formation and implosive dissolution of vapor bubbles in liquids.
  • the UADA is used to produce a hydrocarbon-water dispersion by means of cavitation.
  • the principle of dispersion generation using the system according to the invention is based on the fact that a mixture of at least two different media is pressed through special nozzles in a UADA.
  • the at least two different media are premixed with one another.
  • the further steps in the production of a hydrocarbon-water dispersion by means of cavitation take place in at least one or two UADA modules.
  • a first UADA module supercavitation, as an individual case of hydrodynamic cavitation, takes place in the other, second UADA module, thermal and supercavitation.
  • the two UADA modules are connected one behind the other.
  • the size of the water droplets in the dispersion is varied by the type and intensity of the cavitation. Stronger cavitations result in a smaller diameter of the enclosed drop.
  • the present process enables the production of a hydrocarbon-water dispersion with a droplet size in the range from 10 to 100 ⁇ m. The stability of the dispersion increases with decreasing droplet diameter.
  • the droplet size in the dispersion is regulated by varying degrees of cavitation.
  • the droplet size, phase distribution and morphology in turn have an influence on the stability of the dispersion.
  • the cavitation is set, varied and controlled.
  • the droplet size, phase division and morphology have an influence on the stability (quality) of the dispersion.
  • the cavitation is set, varied and controlled.
  • the droplet size in the dispersion is regulated by varying degrees of cavitation. For the quality of the hydrocarbon-water dispersion to be produced with the present system, it is important to set the optimal intensity of the cavitation.
  • Droplet diameter in the coarse dispersion larger than 1 mm.
  • Droplet diameter in the fine dispersion smaller than 1 mm and larger than 100 ⁇ m
  • the present system makes it possible to keep the water content and the process parameters pressure, temperature and throughput constant in order to ensure a constant quality of the water-oil dispersion produced.
  • the developed process can be built up in two or three procedural stages. On the one hand, there is a technological implementation of coarse and fine dispersion. The other technological solution for deeper dispersion consists of coarse, fine and ultra dispersion.
  • a coarse dispersion of the pre-tempered medium 1 as a hydrocarbon-containing medium and the pre-tempered medium 2 as water is provided by mixing medium 1 and medium 2 in at least one pre-mixing unit (coarse disperser) before the fine dispersion is made (claim 13).
  • a method for producing a hydrocarbon-water dispersion (fine dispersion), or a water-hydrocarbon dispersion (separating dispersion) that can easily be separated into at least two phases is provided, the method being carried out in particular in a plant described above and comprising the following steps :
  • UADA ultrasonic acoustic flow unit
  • a pressure is set in front of the UADA module (pre-pressure) and a pressure behind the UADA (claim 11).
  • the pre-sonic velocity is a transversal deformation of currents through the formation of vortex-ring currents. In the range of the speed of sound, the resulting flow becomes so great that cavitation occurs. Furthermore, long-chain entangled hydrocarbons are torn apart thermomechanically. The inflow is accelerated tangentially in the radial direction, in which the chamber flows are sheared against one another and the relative speed is thus doubled. The high speed creates the vapor bubbles and the displaced eddy currents balance each other out. This creates constant, stable eddies that are separated according to hydrodynamic properties.
  • the ultrasonic velocity occurs after the currents meet and the energy of the currents in the confined volume is concentrated. With the help of the concentrated energy, the energy-mass exchange is promoted and the physical-chemical conversion is accelerated. The dispersion formed is discharged from the module through the drain.
  • the steam pressure of water must be undercut with the operating pressure by means of hydrostatic pressure and temperature setting (steam pressure curve) by increasing the speed (energy conversion / kinetic pressure component). This results from the vapor pressure curve for water as shown in FIG.
  • the type, strength and form of cavitation in the UADA is influenced by the pressure ratio between the pre-pressure and the negative pressure in the fine disperser or in the separating disperser. The more pronounced the cavitation, the smaller the diameter of the droplets in the dispersion,
  • the hydrocarbon-water fine dispersion is introduced into at least one further unit for producing an ultrafine dispersion (ultrafine disperser) after leaving the fine disperser, this unit at least one further ultrasonic acoustic flow unit (UADA ) for the production of a hydrocarbon-water ultrafine dispersion by means of a combination of thermodynamic and hydrodynamic cavitation,
  • thermocavitation catalyzes the hydrodynamic cavitation in the downstream UADA and thus intensifies the mixing of the dispersion.
  • the procedural insert is set up in such a way that there is negative pressure in the meat processing device.
  • the procedural insert is set up in such a way that there is negative pressure in the meat processing device.
  • thermodynamic and hydrodynamic or super cavitation creates better conditions for producing the ultra-stable and ultra-fine dispersion.
  • the type, strength and form of cavitation in the UADA is influenced by the pressure ratio between the pre-pressure and the negative pressure in the ultrafine disperser. The more pronounced the cavitation, the smaller the diameter of the droplets in the dispersion,
  • pre-pressure the pressure before the UADA of the ultrafine disperser
  • negative pressure the pressure after the UADA of the ultrafine disperser
  • the ultrafine dispersion can be achieved technologically either after the coarse dispersion or after the fine dispersion.
  • the object of the present invention is also achieved with a method having the features of claims 2 and 5.
  • the cavitation process used in the developed system in an ultrasonic acoustic flow unit (UADA) is known from the patents RU 2130503 C1, RU 2462301 C1 and the patent for the useful technical model RU 134076 U1 and enables the production of a stable dispersion Fuel and water.
  • this UADA is expanded in combination with heat exchangers and pressure boosting devices, so that the stability of the hydrocarbon-water dispersion formed is significantly increased.
  • the heat exchangers installed in the present system allow a separately temperature-controlled hydrocarbon and water supply.
  • a moisture sensor can also be installed in the feed line of the mixing device (UADA) in order to continuously check and control the water content.
  • there are control or metering valves in the hydrocarbon and water addition which allow the mixing ratio to be changed.
  • the technology developed is used to produce a long-term stable dispersion of water and hydrocarbons.
  • the long-term stability is significantly influenced by the droplet size. With a drop size of less than 100 ⁇ m, a stability of at least 1 year up to 7 years can be achieved. For example, the stability of bunker oils is increased, which means that the use of additives can be dispensed with. There are fewer or no unwanted reactions in the storage or transport fuel tank and the flocculation of paraffins can be reduced or even suppressed.
  • the fuel can be burned more optimally, as these evaporate suddenly in the combustion chamber and the combustion of the fuel takes place more homogeneously due to the increase in surface area to volume. Fewer soot particles are produced during combustion. The efficiency of the combustion, based on the primary energy introduced, is increased, with the fuel being converted almost entirely into energy.
  • the pollutants are decimated when the dispersion is burned compared to when the pure fuel is burned. With a water content of more than 10%, the combustion temperature is reduced, which in turn can minimize the emission of pollutants such as NO x.
  • liquid media with a viscosity of 1 mm 2 / s to 1,000 mm 2 / s, preferably from 100 mm 2 / s to 800 mm 2 / s, in particular from 300 mm 2 / s to 500 mm 2 / s are processed (claim 15).
  • Medium 1 (as the main medium) denotes the hydrocarbon-containing, oil-containing component which, in combustion processes, corresponds to over 60 wt% of the dispersion.
  • the proportion of medium 1 is less than 40 wt%.
  • Medium 2 (as the second medium) corresponds to the water-containing component, which corresponds to less than 40 wt% of the dispersion in combustion processes.
  • the effective proportion of medium 2 in separation processes is over 60 wt%.
  • demineralized (deionized) water is used to produce the hydrocarbon-water dispersion.
  • normal tap water or so-called brackish water can also be used. Premixing / coarse dispersion
  • the fine disperser can be preceded by a premixing unit.
  • the at least one premixing unit comprises at least one heat exchanger for medium 1, at least one heat exchanger for medium 2 and at least one mixing apparatus for premixing medium 1 and medium 2.
  • the heat exchangers for setting the temperature and, indirectly, the viscosity of the hydrocarbon the medium 1 can be designed as a heat exchanger with a bypass.
  • Medium 1 and medium 2 are heated to temperatures between 30 and 90 ° C., preferably between 40 and 80 ° C., and introduced into the premixer.
  • at least two different preheated media are mixed with one another in the coarse dispersion (claim 14).
  • the prerequisite for the optimal production of the coarse dispersion are identical absolute inlet pressures of the media.
  • devices for measuring the temperature and volume flow of the fuel in the fuel supply line can also be provided.
  • At least one filter for removing dirt particles from the medium 1 is provided on or in the supply line of medium 1 as a hydrocarbon-containing medium.
  • a pressure sensor is installed upstream of the filter and a pressure sensor is installed downstream.
  • At least one heat exchanger for adapting the water temperature to the temperature of the oil-containing component is provided in or on the supply line for medium 2 as water, in particular desalinated and deionized water.
  • Devices e.g. sensors
  • for measuring the volume flow and the temperature of the water are preferably provided upstream and downstream of the heat exchanger in the water pipe.
  • the premixing apparatus already mentioned above is used to premix the components described above.
  • This mixing apparatus is designed for media of different viscosity. With the help of a static mixer, the water is laminated into the oil flow Layers introduced. This coarse mixing optimizes the actual mixing process and protects the pump from the UADA, as a sudden change of hydrocarbon and water is prevented.
  • devices for measuring the temperature and pressure of the hydrocarbon-water coarse dispersion are provided downstream behind the premixer.
  • the temperature-controlled mixture with the preset volume or percentage is then passed to the next stage for fine dispersion after coarse dispersion.
  • the stable hydrocarbon-water dispersion is produced in the subsequent step.
  • the at least one fine disperser comprises at least one first pump for a first pressure increase in the feed of the coarse hydrocarbon-water dispersion; the at least one first ultrasonic acoustic flow unit (UADA) and at least one second pump.
  • UADA ultrasonic acoustic flow unit
  • the hydrocarbon-water coarse dispersion is, before entering at least one first ultrasonic acoustic flow unit (UADA), to pressures of up to 2.5 MPa, preferably to pressures between 0.1 MPa and 2 MPa, particularly preferably between 1 MPa and brought to 1.5 MPa using a first pump.
  • UADA ultrasonic acoustic flow unit
  • the pre-pressure built up before the first UADA can, for example, be between 0.6 and 2.5 MPa (claim 16).
  • the pump used for this can be used for high-volume refueling processes or for continuous low-volume production processes, e.g. for volume flows between 5 m 3 / h and 100 m 3 / h, preferably between 10 m 3 / h and 80 m 3 / h, particularly preferably between 20 m 3 / h h and 60 m 3 / h.
  • Typical volume flows can be, for example, 6 m 3 / h; 20 m 3 / h and 100 m 3 / h.
  • the system has a device arranged downstream of this first pump for measuring the water content in the coarse hydrocarbon-water dispersion.
  • This device for measuring the humidity can be designed in the form of a bypass, and allows in the event of deviations a readjustment of the water content of the desired water content, e.g. via a control valve from the water pipe.
  • the setting of the water content is preferably automated, which enables inline and more precise water metering as well as regulation of the volume flow and the temperature. These are prerequisites for a consistent quality of the dispersion to be produced. Furthermore, the amount of water in the fuel can be varied easily. The amount of water, the throughput of hydrocarbons, the temperature and the pressure in the cavitation area are important for consistent quality.
  • the water content in the dispersion can be set and measured variably.
  • the water content is important for the later use and properties of the combustion and is in a range from 1 wt% to 40 wt%, preferably 5 to 30 wt%, particularly preferably 10-15 wt% (based on the total volume of the dispersion to be produced) .
  • the device for measuring and adjusting the water content in the hydrocarbon-water coarse dispersion is followed downstream by further measuring devices (e.g. sensors) for temperature and pressure before entering the first ultrasonic-acoustic flow-through unit (UADA).
  • further measuring devices e.g. sensors
  • UADA ultrasonic-acoustic flow-through unit
  • the fine dispersion is produced in an ultrasonic acoustic flow unit (UADA) in that the cavitation is not actively introduced, but rather arises due to the currents in the UADA.
  • UADA ultrasonic acoustic flow unit
  • a pre-pressure between 0.6 and 2.5 MPa is set upstream of the UADA module (as described above) and approx. 0.06 MPa downstream of the UADA module.
  • the pressure setting of the fine dispersion on the ultrasonic acoustic flow unit in the fine disperser should therefore have the following pressure ratio:
  • the fine dispersion can be discharged from the system.
  • the present case is a two-stage process for producing the stable hydrocarbon-water dispersion by coarse dispersion (premixing to produce the mixture) and fine dispersion, with a determination of the procedural regime of the ultrasonic-acoustic flow-through units making a significant contribution .
  • the fine dispersion can also subsequently be converted into the ultrafine dispersion.
  • At least one unit for producing a stable hydrocarbon-water dispersion in the fine disperser downstream of the at least one unit for producing a stable hydrocarbon-water dispersion in the fine disperser, at least one unit for producing a stable hydrocarbon-water dispersion in the ultrafine disperser can be arranged, this unit at least a second Ultrasonic acoustic flow unit (UADA) for producing a stable hydrocarbon-water ultrafine dispersion by means of a combination of thermal and hydrodynamic cavitation (claim 17).
  • UADA Ultrasonic acoustic flow unit
  • the ultrafine disperser comprises at least one meat device for heating the fine dispersion flowing under negative pressure, at least one pump (downstream) for generating the negative pressure in the meat device and for increasing the pressure in the inlet of the heated hydrocarbon-water fine dispersion; (downstream) at least one second ultrasonic acoustic flow unit (UADA) and (downstream) at least one pump for setting the negative pressure, which leads to the setting, variation and control of the cavitation regime.
  • UADA ultrasonic acoustic flow unit
  • a three-stage process for producing the ultra-stable hydrocarbon-water dispersion by large-scale dispersion, fine dispersion and ultra-fine dispersion can be provided, with the recording of the procedural regime of the ultrasonic-acoustic flow-through units making a significant contribution, whereby the following applies: - the ratio of the pre-pressure before the UADA and the negative pressure after the UADA in the fine disperser is at least 10, according to
  • the ratio of the pre-pressure before the UADA and the pressure after the UADA of the negative pressure in the ultrafine disperser is at least 12, according to
  • the at least one heating device preferably consists of at least one heating cartridge. It is also possible to use several heating cartridges that can be switched on in parallel.
  • the at least one heating cartridge consists of a heating jacket and a screw-in heater.
  • the hydrocarbon-water fine dispersion is heated in the at least one heating device, in particular a heating cartridge, to up to 80 ° C. before entering the at least second ultrasonic acoustic flow unit (UADA) (claim 18).
  • UADA ultrasonic acoustic flow unit
  • thermal cavitation is combined with hydrodynamic cavitation to increase effectiveness and stability.
  • the conditions for initiating thermal cavitation are created in a low pressure heater.
  • the local heating in the heating device creates small vapor bubbles on the surface, which are released by the flow and collapse again in the liquid as a result of a drop in temperature.
  • This thermal cavitation intensifies the hydrodynamic cavitation in the downstream UADA and thus supports the mixing of the dispersion.
  • the procedural insert is designed in such a way that there is negative pressure in the heating device.
  • a renewed pressure build-up takes place in front of the UADA and the setting of the negative pressure behind the UADA.
  • the synergism of the effect of thermodynamic and hydrodynamic cavitation creates ideal conditions for the production of the stable and ultra-fine hydrocarbon-water dispersion.
  • At least one further pump is provided downstream of the second UADA for controlling the cavitation regime.
  • this additional pump serves to convey the hydrocarbon-water dispersion formed to the discharge line and further to the measuring section and to the storage tanks.
  • This pump is also equipped with a pump protection, which consists of a negative pressure sensor in front of and an overpressure sensor behind the pump.
  • At least one filter is provided downstream of the at least one additional pump for conveying the hydrocarbon-water dispersion formed.
  • the filter is arranged in particular in front of the measuring section in order to filter out coarse particles and thus protect sensitive sensors in the measuring section.
  • Pressure sensors are installed in front of and behind the filter, which allow the differential pressure to be measured in order to detect clogging of the filter at an early stage.
  • the aforementioned measuring section is used to record the temperature, pressure and volume flow of the hydrocarbon-water dispersion formed.
  • a branch is provided behind the measuring section, which makes it possible to guide the dispersion in an inner circle over the UADA modules during the start-up and shutdown process of the system.
  • a built-in control technology enables a smooth switchover from internal recirculation to production.
  • the recirculation line is also equipped with a check valve, a pressure sensor and a volume flow monitor.
  • the ultrafine dispersion can be achieved technologically either after the coarse dispersion or after the fine dispersion. Separation process
  • the separating disperser (unit constructed identically to the fine disperser, but either without or with a premixer - coarse disperser integrated in the UADA body) has at least one separation tank for separating the easily into at least two phases separable water-hydrocarbon dispersion (separating dispersion) in hydrocarbon and water connected downstream (claim 20).
  • a system for separating a water-carbon-hydrogen dispersion comprising the following elements:
  • At least one unit for producing a water-hydrocarbon separating dispersion comprising at least one first ultrasonic acoustic flow-through unit for producing a water-hydrocarbon separating dispersion by means of hydrodynamic cavitation and
  • At least one separation tank for separating the water-hydrocarbon separating dispersion into hydrocarbon and water.
  • the proportion of medium 1 as a hydrocarbon-containing medium is the water-hydrocarbon separation dispersion below 50 wt%.
  • the effective proportion of medium 2 as water in separation processes is over 50 wt%.
  • the one-step process for cleaning accordingly comprises the production of the water-hydrocarbon separating dispersion by dispersing it in the separating disperser on the ultrasonic-acoustic flow-through unit, whereby the following applies:
  • the separating dispersion is stored for subsequent separation until the at least two phases of the original media separate.
  • the phase formation takes place by means of coalescence of the hydrocarbon droplets. This creates the aggregates of the hydrocarbon droplets. According to Stokes's equation, gravity forces the hydrocarbon aggregates to form a hydrocarbon phase. After separation, the separated media are recycled.
  • the optimal water content is over 60 wt%.
  • the water-hydrocarbon dispersion thus formed shows instability.
  • the mobility of the separation system enables the emergency medium, contaminated water, to be fed directly into the separation disperser for the production of the water-hydrocarbon separation dispersion and then for phase separation. This allows the technology to be used as a separation process at the accident site.
  • An essential aspect of the present system is its modular structure, which enables several combinations in terms of system and process implementation.
  • Fine disperser consisting of a coarse disperser (premixer), a UADA module and upstream and downstream pumps,
  • Ultrafine disperser consisting of heating device, first pump, UADA module, second pump.
  • the fine disperser can be used individually.
  • FIG. 2 shows a schematic representation of a first embodiment of the dispersion plant according to the invention
  • Figure 3 is a schematic representation of an embodiment of a coarse
  • FIG. 4 shows a schematic representation of an embodiment of a fine disperser
  • Figure 5 is a schematic representation of an embodiment of an ultrafine
  • FIG. 6 shows a schematic representation of an embodiment of the separating disperser according to the invention.
  • FIG. 7 shows a detailed representation of an ultrasound acoustic flow unit used according to the invention.
  • FIG. 8 is a detailed view of an acoustic panel used in the assembly of FIG.
  • Figure 2 shows the schematic representation of a dispersion plant. The overall system is divided into three different areas: the coarse disperser, the fine disperser and the ultrafine disperser.
  • the main component of the system is the ultrasonic acoustic flow unit (UADA).
  • UADA ultrasonic acoustic flow unit
  • a UADA is always designed for a specific flow rate (6 m 3 / h; 20 m 3 / h and 100 m 3 / h).
  • the structure of the UADA module is shown in FIG.
  • the module consists of an inlet, pre-acoustic chamber, acoustic chamber, ultrasonic chamber and outlet.
  • the acoustic plate shown in FIG. 8, is located in the pre-acoustic chamber and is made up of the axial annular chamber and tangential vortex grooves.
  • the vortex tubes open into the ultrasonic chamber, which is connected to the drain.
  • filters are installed between the coarse and fine disperser and after the ultrafine disperser.
  • Coarse disperser In the coarse disperser area ( Figure 3), the system consists of at least two feed lines for two different media, each with a heat exchanger, a device for adjusting the media ratio and a premixer.
  • the temperature of the media can be regulated via the control technology of the system.
  • the media ratio is automatically set and monitored. This is transferred to the fine disperser plant area.
  • the coarse disperser is the preliminary stage of the fine disperser.
  • Fine disperser The fine disperser area in Figure 4 consists of two pumps (pre-pressure and vacuum pump), the UADA enclosed by these pumps and the associated control technology. After the fine disperser comes the ultrafine disperser.
  • the ultrafine disperser shown in FIG. 5, consists of a heating device, two pumps (pre-pressure and vacuum pump) and the UADA enclosed by these.
  • the design of the heating device (heating cartridge) consists of a heating jacket with an integrated screw-in heater.
  • the results are evaluated using an online viscometer via three measuring points after the coarse disperser, fine disperser and ultrafine disperser.
  • a branch is provided behind the measuring section, which enables the dispersion to be conducted in an inner circle over the UADA units during the start-up and shutdown process of the system.
  • the control enables a smooth switchover from internal recirculation to production.
  • the dispersion system is used to mix at least two different preheated media.
  • the first step is the rough physical premixing.
  • the second step involves fine dispersion based on the hydrodynamic and super- Cavitation. In a combination of thermo-, hydrodynamic and super-cavitation, the dispersion is refined in the last step.
  • the system In the event of a water disaster, the system is used to separate the media.
  • the system as shown in Figure 6, consists of two pumps (pre-pressure and vacuum pump), the UADA enclosed by these pumps and the associated control technology.
  • the system is fed by a collecting tank in which the damaged dispersion is located.
  • the separation tank is located behind the system, which is connected to at least two tanks (e.g. oil and water tank) for at least two already separated media.
  • the quality control purity control then takes place in the tanks.
  • the separation system is used to separate the water-hydrocarbon mixture at disaster sites and is constructed identically to the fine dispersion area.
  • Embodiment example 1 is a diagrammatic representation of Embodiment example 1
  • the principle of dispersion generation is based on the fact that a mixture of fuel and water is pressed through special nozzles in a UADA (ultrasonic acoustic flow unit) developed for this purpose.
  • UADA ultrasonic acoustic flow unit
  • the resulting flow velocities favor the development of cavitation.
  • the result is a very fine, stable dispersion which is flammable.
  • the UADA module can be shut off manually on the inlet side with manual shut-off valves and on the outlet side with manual shut-off valves.
  • the following safety shut-off valves are installed at the entrance, which automatically shut off the system in the event of a serious malfunction.
  • Safety valves are installed at the outlet, which separate the modules from the tank farm in the event of a serious malfunction.
  • the safety shut-off valves automatically separate the UADA module from the rest of the system in the event of an emergency stop, fire, power failure and unforeseen critical operating conditions.
  • the UADA module begins behind the fuel supply line in which the temperature and volume flow of the educt are measured.
  • the fuel line that continues is provided with a non-return valve that prevents backflow to the educt store.
  • a temperature sensor for monitoring the pour point and flash point is installed after the recirculation line.
  • a filter is then installed to keep dirt particles away from the system.
  • a pressure sensor is installed in front of and behind the filter in order to be able to detect an excessive pressure drop. If this rises too high, the filter must be changed or cleaned.
  • a heat exchanger with bypass is then installed. This should adjust the temperature in the input and bring it to the desired values (the current safety surcharges must be observed for the flash and ignition point temperatures). This adjusted temperature is continuously checked by the temperature sensor.
  • the oil flow is roughly premixed with the water content.
  • the desalinated (deionized) water is fed into the process from the water treatment via separate lines.
  • the addition of water is dosed with the control valve.
  • the volume flow and the temperature of the water are measured and recorded.
  • the water can be adjusted to the temperature of the hydrocarbon with the built-in heat exchanger.
  • a non-return valve is installed to prevent hydrocarbons from entering the water pipe.
  • the mixture temperature and the resulting pressure are measured in order to identify deviating operating conditions.
  • the mixture then comes into the first pressure increase.
  • the pressure is increased to up to 2.5 MPa.
  • the humidity is measured in a bypass behind the pump. If there are deviations from the desired water content, readjustment is carried out via the control valve from the water pipe.
  • the first ultrasonic acoustic flow unit UADA
  • the temperature and pressure are measured and recorded.
  • the dispersion is produced in this UADA, and the pressure built up by the pressure increase drops completely.
  • the temperature and pressure are measured and recorded behind the UADA.
  • a heating cartridge with a temperature sensor is then installed in order to be able to build up a subsequent thermal cavitation behind the UADA.
  • the second pressure increase is followed by the second pressure increase.
  • An additional function of the second pressure increase is the setting of the negative pressure behind the first UADA. This has a significant influence on the type, strength and form of cavitation in the first UADA.
  • the first UADA works optimally when the pressure behind it is set at 0.05 MPa.
  • the pump for the second pressure increase is equipped with a pressure sensor for monitoring the negative pressure in front of the UADA and a pressure sensor for monitoring the overpressure behind the UADA. This makes it possible to run the system in a targeted manner with the required negative and positive pressure.
  • the pressure sensors built into this section of the route give an alarm before a critical negative or positive pressure arises. The control can thus counteract this event.
  • This pump is also equipped with a pump protection, which again consists of a pressure sensor for monitoring the negative pressure in front of and a pressure sensor for monitoring the overpressure behind the pump.
  • a filter is installed to ensure that no coarse particles get into the measuring section and thus protect the sensitive sensors.
  • Pressure sensors are installed in front of and behind the filter, which allow the differential pressure to be measured in order to detect clogging of the filter at an early stage. The following data is recorded in the measuring section: the temperature, the pressure, the volume flow.
  • the control valve is built in for this purpose. This enables a smooth switchover from internal recirculation to production.
  • the control valve is paired with a check valve in order to prevent mixing of faulty batches in the event of recirculation from the product store from the line and finished dispersion from the line.
  • the recirculation line is equipped with a check valve, a pressure sensor and a volume flow monitor.
  • Embodiment 2 Method for making the dispersion Example 1: Storage tank, coarse disperser, fine disperser, product tank
  • Example 2 Storage tank, coarse disperser, fine disperser, ultrafine disperser, product tank
  • Example 3 Separation process
  • Example 3 Collection tank, fine disperser, oil tank and water tank.
  • Viscosity 180 mm 2 / s (DIN EN ISO 3104)
  • Predicted Product Three different levels of fineness of the droplets are achieved with the present system:
  • the droplet diameter in the coarse dispersion is greater than 1 mm

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  • Organic Chemistry (AREA)
  • Liquid Carbonaceous Fuels (AREA)

Abstract

La présente invention concerne un système de production d'une dispersion fine d'hydrocarbure-eau stable ou d'une dispersion de séparation eau-hydrocarbure instable, comprenant au moins une unité pour produire une dispersion stable d'hydrocarbures-eau dans le dispositif de dispersion fin à partir d'au moins un milieu 1 en tant que milieu contenant des hydrocarbures et du milieu 2 en tant qu'eau, ladite unité comprenant : au moins une première pompe pour une première augmentation de pression dans l'entrée de la dispersion grossière d'hydrocarbure-eau ; au moins une machine à écoulement acoustique à ultrasons destinée à produire une dispersion d'hydrocarbures-eau au moyen d'une cavitation hydrodynamique, et au moins une seconde pompe pour générer une pression négative pour établir le régime de cavitation dans la machine à écoulement acoustique ultrasonore ; au moins un appareil de chauffage en amont de la seconde pompe pour générer la thermocavitation ; au moins une deuxième machine à écoulement acoustique ultrasonore pour produire une dispersion stable d'hydrocarbures-eau au moyen de la combinaison d'une cavitation thermomécanique et hydrodynamique et d'au moins une troisième pompe pour générer une pression négative pour établir le régime de cavitation dans la deuxième machine à écoulement acoustique ultrasonore. La présente invention concerne en outre un procédé de production d'une dispersion fine d'hydrocarbure-eau stable ou d'une dispersion de séparation eau-hydrocarbure instable à l'aide d'un tel système.
PCT/EP2021/051598 2020-01-23 2021-01-25 Système et procédé de production d'une dispersion stable d'hydrocarbures et d'eau pour améliorer les processus de combustion, et une dispersion eau-hydrocarbure qui est facilement séparable en au moins deux phases en tant que partie du processus de nettoyage à des emplacements d'accident WO2021148673A1 (fr)

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US4259021A (en) * 1978-04-19 1981-03-31 Paul R. Goudy, Jr. Fluid mixing apparatus and method
DE4139782A1 (de) 1991-12-03 1993-06-09 Roland 7076 Waldstetten De Steinmaier Emulgiervorrichtung zum emulgieren von dieselkraftstoff und wasser
DE4137179C2 (de) 1991-11-12 1997-02-27 Hdc Ag Vorrichtung zum Erzeugen einer Wasser-in-Öl Emulsion und Verwendung der Vorrichtung an einem Dieselmotor
EP0674941B1 (fr) 1994-03-12 1997-10-29 MTU Motoren- und Turbinen-Union Friedrichshafen GmbH Dispositif pour la fabrication d'une émulsion huile-eau
RU2130503C1 (ru) 1998-06-17 1999-05-20 Красноярский государственный технический университет Устройство для электромагнитного рафинирования электропроводных расплавов
WO2001055282A1 (fr) 2000-01-25 2001-08-02 Basf Aktiengesellschaft Emulsions carburant-eau contenant des emulsifiants a base de polyisobutene
EP2281626A2 (fr) * 2009-08-07 2011-02-09 Cannon Deutschland GmbH Dispositif et procédé destinés à l'émulsification de liquides
WO2011042432A1 (fr) 2009-10-05 2011-04-14 Universität Zu Köln Procédé de confection in-situ de mélanges eau/carburant dans des moteurs thermiques
RU2462301C1 (ru) 2011-03-10 2012-09-27 Овченкова Оксана Анатольевна Устройство для тепломассоэнергообмена
RU134076U1 (ru) 2013-06-05 2013-11-10 Сергей Николаевич Тумаков Устройство для тепломассоэнергообмена
WO2014040918A1 (fr) * 2012-09-14 2014-03-20 Spx Flow Technology Danmark A/S Procédé, utilisation et appareil destinés à inverser ou à casser en continu un produit alimentaire à émulsion huile-dans-l'eau au moyen d'une cavitation hydrodynamique
EP3184164A1 (fr) * 2014-08-22 2017-06-28 Johokagaku Kenkyusyo Co. Ltd. Procédé de fabrication de bulles ultrafines ayant un radical oxydant ou un radical réducteur par moussage par résonance et cavitation sous vide, et dispositif de fabrication d'eau à bulles ultrafines
WO2019161852A2 (fr) * 2018-02-26 2019-08-29 Kmitta Kurt Procédé destiné à faire fonctionner un moteur à combustion interne, système de mise en œuvre du procédé et dispositif de production d'une émulsion

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2433653A1 (de) * 1973-07-12 1975-01-30 Patrick Burke Verfahren und vorrichtung zum behandeln von fluiden
US4259021A (en) * 1978-04-19 1981-03-31 Paul R. Goudy, Jr. Fluid mixing apparatus and method
DE4137179C2 (de) 1991-11-12 1997-02-27 Hdc Ag Vorrichtung zum Erzeugen einer Wasser-in-Öl Emulsion und Verwendung der Vorrichtung an einem Dieselmotor
DE4139782A1 (de) 1991-12-03 1993-06-09 Roland 7076 Waldstetten De Steinmaier Emulgiervorrichtung zum emulgieren von dieselkraftstoff und wasser
EP0674941B1 (fr) 1994-03-12 1997-10-29 MTU Motoren- und Turbinen-Union Friedrichshafen GmbH Dispositif pour la fabrication d'une émulsion huile-eau
RU2130503C1 (ru) 1998-06-17 1999-05-20 Красноярский государственный технический университет Устройство для электромагнитного рафинирования электропроводных расплавов
WO2001055282A1 (fr) 2000-01-25 2001-08-02 Basf Aktiengesellschaft Emulsions carburant-eau contenant des emulsifiants a base de polyisobutene
EP2281626A2 (fr) * 2009-08-07 2011-02-09 Cannon Deutschland GmbH Dispositif et procédé destinés à l'émulsification de liquides
WO2011042432A1 (fr) 2009-10-05 2011-04-14 Universität Zu Köln Procédé de confection in-situ de mélanges eau/carburant dans des moteurs thermiques
RU2462301C1 (ru) 2011-03-10 2012-09-27 Овченкова Оксана Анатольевна Устройство для тепломассоэнергообмена
WO2014040918A1 (fr) * 2012-09-14 2014-03-20 Spx Flow Technology Danmark A/S Procédé, utilisation et appareil destinés à inverser ou à casser en continu un produit alimentaire à émulsion huile-dans-l'eau au moyen d'une cavitation hydrodynamique
RU134076U1 (ru) 2013-06-05 2013-11-10 Сергей Николаевич Тумаков Устройство для тепломассоэнергообмена
EP3184164A1 (fr) * 2014-08-22 2017-06-28 Johokagaku Kenkyusyo Co. Ltd. Procédé de fabrication de bulles ultrafines ayant un radical oxydant ou un radical réducteur par moussage par résonance et cavitation sous vide, et dispositif de fabrication d'eau à bulles ultrafines
WO2019161852A2 (fr) * 2018-02-26 2019-08-29 Kmitta Kurt Procédé destiné à faire fonctionner un moteur à combustion interne, système de mise en œuvre du procédé et dispositif de production d'une émulsion

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