WO2001009031A1 - Transformateur de plasma de combustibles fossiles en gaz riche en hydrogene - Google Patents

Transformateur de plasma de combustibles fossiles en gaz riche en hydrogene Download PDF

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Publication number
WO2001009031A1
WO2001009031A1 PCT/ES2000/000040 ES0000040W WO0109031A1 WO 2001009031 A1 WO2001009031 A1 WO 2001009031A1 ES 0000040 W ES0000040 W ES 0000040W WO 0109031 A1 WO0109031 A1 WO 0109031A1
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WIPO (PCT)
Prior art keywords
fuel
reactor
hydrogen
heater
plasma
Prior art date
Application number
PCT/ES2000/000040
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English (en)
Spanish (es)
Inventor
Fateev Vladimir
Boris Potapkin
Victor K. Jivotov
Ricardo Blach Vizoso
Original Assignee
David Systems Technology, S.L.
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
Priority claimed from ES009901720A external-priority patent/ES2168040B1/es
Priority claimed from ES200000027U external-priority patent/ES1045040Y/es
Application filed by David Systems Technology, S.L. filed Critical David Systems Technology, S.L.
Priority to JP2001514239A priority Critical patent/JP2003506300A/ja
Priority to BR0012831-7A priority patent/BR0012831A/pt
Priority to CA002379892A priority patent/CA2379892A1/fr
Priority to MXPA02001038A priority patent/MXPA02001038A/es
Priority to AU22951/00A priority patent/AU2295100A/en
Priority to KR1020027001141A priority patent/KR20020039326A/ko
Publication of WO2001009031A1 publication Critical patent/WO2001009031A1/fr
Priority to HK03101157.4A priority patent/HK1050885A1/zh

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/342—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents with the aid of electrical means, electromagnetic or mechanical vibrations, or particle radiations
    • H—ELECTRICITY
    • H05—ELECTRIC TECHNIQUES NOT OTHERWISE PROVIDED FOR
    • H05H—PLASMA TECHNIQUE; PRODUCTION OF ACCELERATED ELECTRICALLY-CHARGED PARTICLES OR OF NEUTRONS; PRODUCTION OR ACCELERATION OF NEUTRAL MOLECULAR OR ATOMIC BEAMS
    • H05H1/00—Generating plasma; Handling plasma
    • H05H1/24—Generating plasma
    • H05H1/46—Generating plasma using applied electromagnetic fields, e.g. high frequency or microwave energy
    • H—ELECTRICITY
    • H05—ELECTRIC TECHNIQUES NOT OTHERWISE PROVIDED FOR
    • H05H—PLASMA TECHNIQUE; PRODUCTION OF ACCELERATED ELECTRICALLY-CHARGED PARTICLES OR OF NEUTRONS; PRODUCTION OR ACCELERATION OF NEUTRAL MOLECULAR OR ATOMIC BEAMS
    • H05H1/00—Generating plasma; Handling plasma
    • H05H1/24—Generating plasma
    • H05H1/46—Generating plasma using applied electromagnetic fields, e.g. high frequency or microwave energy
    • H05H1/461—Microwave discharges
    • H05H1/4622—Microwave discharges using waveguides

Definitions

  • the object of the present invention is a plasma converter of fossil fuels in a gas rich in hydrogen.
  • This converter comprises a heater, a mixing chamber, a reactor all connected in series and a microwave energy source (MCN) for the reactor, this converter being able to produce a high content gas from traditional fossil fuels in hydrogen in order to increase the performance of an internal combustion engine.
  • MN microwave energy source
  • This invention relates to the production of a hydrogen rich gas from hydrocarbons.
  • Hydrogen is attractive for use as a fuel, as an additive for internal combustion engine fuels because its presence can significantly change the chemical properties of the fuel and can significantly reduce the contamination of combustion products [the effect of use The addition of hydrogen to the fuel is to increase the performance of an internal combustion engine by 10-50%. See Mishchenko, et al., Proc. Vil World Hydrogen Energy Conference, Vol 3
  • the energy for the conversion process can be provided either by preheating the gas mixture or by exothermic reactions (for example, the total or partial oxidation of hydrocarbons) or by heating with electrical energy.
  • plasma can be used as a catalyst for chemical processes (plasma treatment of preheated reactants). See VD Rusanov, K. Etivan, AI Babaritskii, IE Baranov, SA Demkin, VK Jivotov, BV Potapkin and EI Ryazantsev, The Effect of Plasma Catalys ⁇ s by the Example of Methane Dissociation into Hydrogen and Coal (The effect of plasma catalysis by the example of dissociation of methane into hydrogen and carbon), Dokl.
  • Hydrogen is a highly flammable substance that requires complex and expensive storage systems.
  • implementation of a Global distribution network of hydrogen implies economic costs and a timescale that are unapproachable even by developed countries.
  • the second is "the instant response”: how quickly a car responds when the driver steps on the accelerator.
  • a gasoline engine responds in thousandths of a second, but a reformer who reacts slowly would be considered a slow car and the driver would reject it.
  • Phase 1 of this program includes an analysis of the various fuel reformers, on-board hydrogen storage technologies and hydrogen infrastructure needs.
  • Phase 2 will involve the development and testing of a 10 kW reformer and a 1 kg capacity hydrogen storage unit.
  • Alternatives to the direct supply of hydrogen to the fuel cell include: liquefied hydrogen, compressed hydrogen, carbon absorption and storage in the form of hydrides.
  • Liquefied hydrogen has been tested in several vehicles since the 1970s in the United States and other countries.
  • the volume and density density of liquefied hydrogen when used with a fuel cell is the same or better than diesel fuel used with an internal combustion engine.
  • the disadvantages are the high liquefaction energy, handling problems and the inevitable release of evaporated gas.
  • Compressed hydrogen is the simplest on-board technology to conceptualize and would benefit from recent advances in composite materials and improvements in the costs of progress in natural gas vehicles.
  • High-pressure tanks constructed with advanced materials would provide a reasonable weight behavior, although only marginally volumetric behavior.
  • the technical aspects to be solved include cylinder permeability, tank design standards for higher pressures and hydrogen compressor design for refueling.
  • Steam reforming This process basically represents a catalytic conversion of methane and water (steam) into hydrogen and carbon dioxide through three main stages.
  • SR Steam reforming
  • Partial oxidation It is an exothermic process by which hydrogen and carbon dioxide are produced from hydrocarbon fuels (gasoline and others) and oxygen (or air). PO processes have a number of important advantages over SR processes. Companies such as Arthur D. Little (EPYX), Chrysler Corp. and Hydrogen Burner Technologies (all from the USA) have announced plans to develop PO converters.
  • the stages of the EPYX PO converter are: 1 .- vaporization of the fuel (gasoline) by the application of heat, 2.- the vaporized fuel is combined with a small amount of air in a partial oxidation reactor, producing hydrogen and carbon monoxide , 3.- the vapor on carbon monoxide reacts with a catalyst to convert most of the carbon monoxide into carbon dioxide and additional hydrogen, 4.- in the referred oxidation stage, the injected air reacts with the remaining carbon monoxide on the catalyst forming carbon dioxide and water vapor, producing hydrogen rich gases.
  • Autothermal reforming In this exothermic process, the hydrocarbon fuel reacts with a mixture of water and oxygen. The energy released by the oxidation reaction of the hydrocarbon activates the steam reforming process. Companies such as Roll-Royce / Johnson-Matthew (UK) and International Fuel Cell / ONSI (USA) are working on the development of the AR process.
  • Plasma-assisted hydrocarbon conversion There is another concept of plasma-assisted hydrocarbon conversion.
  • a cold non-thermal plasma is used as a source of active species, in order to accelerate chemical reactions.
  • the energy needs of the process can be met, in this case, through thermal energy (low temperature) and thus the plasma acts as a catalyst.
  • Plasma can be produced by the action of very high temperatures, and intense electric fields, or intense magnetic fields. In these discharges, free electrons acquire energy from an imposed electric field and lose this energy due to collisions.
  • the plasma of an incandescent discharge is characterized by high electron temperatures and low gas temperatures and has electron concentrations of approximately 109 to 1012 cm 3 and has an absence of thermal equilibrium that makes possible a plasma in which the gas temperature It may be close to the environment in order to obtain a plasma in which the electrons are sufficiently excited to cause the breakage of the molecular bonds.
  • Cold non-thermal plasma In a cold non-thermal plasma, only charged particles (electrons, ions) acquire energy from the applied electric field and the neutral particles remain at approximately the same temperature.
  • Cold non-thermal plasma can be created by an incandescent electric shock normally operated under reduced pressure.
  • Incandescent discharge plasmas are also suitable for promoting chemical reactions involving thermally sensitive materials. Relatively few basic experimental papers have been published. on the structure / rejected correlation of polymerization membranes with modified surface. The power used to prepare the membranes varies from 30 to 150 W, with the polymerization time being 60 to 3,000 s).
  • the electrical energy necessary to maintain the plasma state can be transmitted to a gas by resistive coupling with internal electrodes, by capacitive coupling with external electrodes, or by inductive coupling with an external bovine or, in the case of microwave discharge, by means of a slow wave structure. Because of the many reactive species in different plasmas, it has not been possible to fully explain the mechanisms of chemical reactions in a plasma. It is well known that fossil fuels and the methods currently used to obtain useful energy (electricity, mechanical movement, etc.) are very inefficient. The most efficient internal combustion engines used for daily transport achieve maximum yields of 32%. This implies that 68% of the available fuel energy is not used to obtain mechanical energy (movement), but is lost.
  • thermodynamics which is set (for a four-stroke engine that uses gasoline) at 43%.
  • the best engines used are still far from maximum performance.
  • the amount of pollution generated by the combustion (oxidation) of fossil fuels has become a growing problem that affects the entire biosphere.
  • the MPCR proposes a better solution to the use of fuels Fossils being a system that can reform / convert fossil fuels into a synthetic fuel (SF), by a chemical process that requires little energy and does not produce undesirable by-products.
  • the improved fuel is characterized in that it is safer from an environmental point of view, as well as suitable for more types of energy conversion processes that, in addition, can be more effective.
  • the MPCR will have great commercial implications.
  • the reduction of pollutant emissions would encourage environmental protection agencies, such as the US EPA and the California Air Resources Board, to adopt zero emission standards, already required by California, using a process similar to proposed by DAVID, within this decade. Which, in turn, would drive the rapid and widespread use of such a system in nations with a high density of vehicles such as the United States and Canada.
  • the DAVID patent differs from those known in the application of a special type of discharge (frequency, voltage, etc.), the process conditions (reaction time, flow rates of the reactants, etc.) and the special construction of the system (shape of the electrodes, reactor, etc.).
  • the main difference between the MPCR and other patented technologies to date is the formation in the MPCR of a specific cold plasma, with an electron temperature greater than the gas temperature.
  • This plasma is achieved by a combination of a special microwave discharge in electrodes of a special design.
  • the two components of the synthesis fuel (SF), H 2 and CO, produced by cold plasma processes in a non-equilibrium state, are good fuels for an internal combustion engine.
  • the emissions of C0 2 and NOx are 90% lower than those driven by gasoline, in the case of a fuel cell, a CO separation membrane (or a converter of special catalytic type).
  • the sulfur content (and its typical compounds) in liquid fossil fuels partially evaporates and takes part in the MPCR process.
  • the emissions will be lower in higher oxides but higher in sulfur compounds at a lower oxidation stage (lower emissions of sulfur alkali and hydrogen sulfide that are easier and more economical to eliminate with existing catalytic converters).
  • synthesis fuel SF
  • MPCR Catalytic Plasma Reactor / Reformer
  • the immediate start of the engine is one of the main aspects to solve.
  • the fuel system fueled with gasoline looks complemented by an injection system with a modified controller, based on the principle of "Injection System with Programmed Admission", suitable for engines driven by the ignition of a hydrogen spark.
  • the SF power system is based on the use of an electronic control assembly that transforms the output signals of the sensors of the engine cycle parameters that determine the optimal air-to-fuel ratio.
  • a very simple technique to mount the injectors on the ICE for the SF allows their installation without changing the cylinder head.
  • the modified ICE is an economical (low cost) way to adapt a conventional ICE to work with SF, while maintaining the normal fuel supply.
  • the initial operation until the MPCR begins to produce the hydrogen necessary for the operation of the fuel cell can be the electrical energy accumulated in batteries.
  • the batteries would provide power to the MPCR. (electrical and thermal energy through electrical energy.
  • the installation consists of an arc plasmatron integrated with a chemical reactor, a heat exchanger, internal combustion engine and electricity generator for the plasmatron.
  • the fuel is vaporized and heated to 1000 ° C during the passage through the heat exchanger. Heating to a higher temperature can cause fuel to decompose and resinous precipitation on the relatively cold walls of the fuel supply channels.
  • the development of the heat exchanger with a working temperature exceeding 1400 ° C is an extremely complex problem and can produce an essential increase in the cost of the system.
  • the fuel vapors, heated in the heat exchanger are directed inside the arc plasmatron. Preheated steam is also supplied inside the arc plasmatron. Cold water is used for cooling the plasmatron walls. During this process, the water is heated and vaporized.
  • the water vapor is heated to 1300 ° C and is directed into the plasmatron.
  • water and fuel vapors gain the energy necessary for heating at 2400 ° C, perform the chemical vapor conversion reaction and, after mixing well, enter the chemical reactor
  • the vapors are converted into synthetic gas, which leaves at a temperature of 1400 ° C.
  • the temperature reduction is a result of the endothermic reaction that takes place.
  • Excess heat is removed by water that cools the walls of the chemical reactor.
  • the hot synthetic gas which passes through the heat exchanger, provides heat to the fuel and water vapors and, after cooling to 400 ° C, enters the internal combustion engine.
  • the plasmatron energy supply is obtained by the internal combustion engine.
  • the approximate installation parameters estimated based on thermodynamic calculations, are indicated below.
  • the installation is calculated for an internal combustion engine with a power of 50 kW.
  • Arc plasma with chemical reactor Power 2.5 kW
  • Plasmatron power essentially reduces engine power, so that an important load is not needed to cool the system.
  • Hot gas flow (1400 ° C) 1, 1 l / sec.
  • the installation aims to produce synthetic gas from gasoline with the subsequent use of an electrochemical generator (ECG) for electricity generation.
  • ECG electrochemical generator
  • the installation consists of an arc plasmatron in which the water and gasoline vapors are heated, a chemical reactor, in which the steam conversion reaction takes place, and a heat exchanger, in which the hot synthetic gas It passes its thermal energy to the fuel and water vapors.
  • water vapors and gasoline vapors, heated and well mixed in the plasmatron are directed into the chemical reactor.
  • Synthetic gas is formed in the reactor.
  • the temperature of the synthetic gas is reduced due to the endothermic chemical reaction. With the help of water cooling, the temperature of the synthetic gas is reduced to 1400 ° C and at that temperature the synthetic gas is directed into the heat exchanger.
  • the thermal energy of the synthetic gas in the chemical reactor is sufficient to produce the evaporation of all the water required for the reaction.
  • the water and gasoline vapors are heated to 1000 ° C because of the thermal energy of the synthetic gas and then enter the arc plasmatron. one .
  • Arc Plasmatron Power 45 kW
  • Hot gas flow (1400 ° C) 12 l / sec.
  • the installation intends to produce synthetic gas with the subsequent use of an ECG.
  • the basic blocks of the installation are arc plasmatron, chemical reactor and heat exchanger.
  • the plasmatron power can be reduced by almost 40%.
  • the flow of gasoline increases at the same time to 30%.
  • the synthetic gas obtained is diluted in half with nitrogen.
  • the absence of water in the process requires the application of a different system for the plasmatron walls and the chemical reactor.
  • the cooling system must be able to cover 40 kW of thermal power.
  • Plasmatron power supply 2.1 Transformer Dimensions: 2.0 x 2.0 x 1.5 m
  • the exhaust gases of internal combustion engines have a temperature of approximately 800 ° C. Thermodynamic calculations show that this temperature is sufficient to perform the vapor conversion reaction for a considerable part of the gasoline. But the kinetic restrictions do not allow the conversion in a reasonable time.
  • the periodic pulse MCW discharge treatment in methane previously heated to 800 ° C increases the degree of methane conversion three times, although the average MCW energy discharge consists of only 10% of the preliminary heating. The degree of methane conversion achieves the thermodynamic equilibrium value.
  • the installation consists of an internal combustion engine whose heat is used to heat gasoline vapors and water vapors.
  • the fumes they enter the chemical reactor, where they are treated by the periodic discharge of MCW pulses.
  • MCW pulses Under the influence of the discharge, a considerable part of the gasoline-vapor mixture is converted into synthetic gas which, together with the unreacted hydrocarbon vapors, enters the internal combustion engine.
  • this scheme does not require the total conversion of the gasoline-steam mixture. Only 10% of the hydrogen present in the fuel mixture significantly increases engine performance, reducing toxic emissions and improving engine efficiency.
  • the facility aims to produce synthetic gas on board cars for use in ECG. It consists of a chemical reactor in which the conversion of gasoline with steam is carried out at the expense of the energy of partial oxidation.
  • a microwave generator is used for the acceleration of the reaction. Microwave radiation is directed inside the reactor, where chemically active particles are generated under the influence of microwave radiation. Active particles, which participate in chain processes, essentially accelerate the conversion of gasoline.
  • the heat exchanger is used to recover heat from the generated synthetic gas.
  • Hot gas flow (1000 ° C) 17 l / sec.
  • the scheme of the installation differs from the previous one only by the productivity and change of air by oxygen.
  • the amount of water is selected so that, under stoichiometric conditions, the temperature of the chemical reactor is 1000 ° K.
  • the content of the installation, its approximate parameters and the flow of reactants are shown for a productivity of 10,000 m 3 of synthetic gas per hour.
  • Average radiation power 200W large equipment content a) high voltage and power transformers; b) rectifier and power regulators; c) generator blocks with magnetrons; d) MCW channels; e) control console.
  • the power equipment requires for its placement 150 m 2 of open area. Other equipment is placed in a covered compartment with an area of 70 m 2 . Pulse power 600 kW
  • the main disadvantages of the thermal plasma technique are a fairly high energy consumption and a high operating temperature.
  • Discharge model to determine the primary discharge parameters, which are essential for chemical reactions in the plasma reactor.
  • the first stage is closely linked to the analysis of the available experimental results and provides the exhaustive construction of a physical model of the evolution of the discharge, which is in accordance with the experimental facts.
  • the second stage will determine the contributions of the different hydrocarbon conversion mechanisms to the predefined discharge conditions through the development of a physical-chemical discharge model. The results of this model generation can be used to improve the specific performance of a reactor by changing the discharge parameters.
  • the physical model of microwave discharge evolution will provide the primary plasma parameters, such as electron and ion concentrations, their average energies, the temperature of the gas as a function of time and their spatial distributions. It is useful to subdivide the evolution of the download into three different stages:
  • stage of quasi-equilibrium discharge in which there are filaments with a plasma almost in equilibrium
  • this model provides the value of the quasi-stationary field in the channel. These values can be compared with the experimental data for the intensity of the electric field and electron concentrations. Since the concentration of electrons in the channel provided by the frontal plane theory is relatively small ( ⁇ e of approximately 3 * 10 14 1 / cm 3 ), it is quite difficult to measure this amount from spectroscopic studies. However, the value quoted before ⁇ e agrees with the estimation of ⁇ e ⁇ 10 15 1 / cm 3 of the hydrogen line dispersion analysis. It should be mentioned that hydrogen plasma is more suitable for experimental measurements due to the more precise structure and well-known affordable kinetics and deviation parameters, not only for the fundamental state, but also for required excited states. This is the reason for the use of a hydrogen plasma in the first stage as a convenient sample environment for the discharge model.
  • the deviation in the case of hydrogen plasma may be due to impurities in the bulk gas, such as 1% water.
  • the temperatures of the electrons, which correspond to these field intensities are approximately 2eV.
  • An alternative way to determine this quantity is the population analysis of excited states of hydrogen, based on line intensities.
  • the rate of heating of gas in the plasma can determine the onset of the quasi-liquid state due to the heat instability of the ionization in the streamer channel.
  • the gas heating rate was determined by solving the kinetic equation for the energy of electrons and finding the contribution of each elementary process in the heating of the gas, taking into account the conservation of energy in some degrees of freedom.
  • the vibration energy can be expected to be stored without relaxation in translational and rotational degrees at least at low temperatures.
  • the simulation gives a temperature increase of approximately 100 K in the course of the first 100 ns. This value is sufficient to initiate heat instability of the ionization in the channel if pressure relaxation occurs fairly quickly.
  • the characteristic hydrodynamic time is approximately 100 ns for hydrogen and somewhat longer for methane.
  • the instability of the ionization in the streamer channel seems to be responsible for the thermalization of the channel by approximately 100 ns in hydrogen, since the experiment shows a sharp increase in gas temperature and electron concentration after approximately 200 ns in hydrogen and 400 ns in methane.
  • the concentration of electrons in the quasi-equilibrium state is determined from the assumption that the thickness of the skin layer is approximately the radius of the streamer. This assumption produces a concentration of electrons of approximately 10 16 1 / cm 3 , which reasonably matches the experimental value of approximately 5 * 10 16 1 / cm 3 .
  • the temperature of the experiment gas (approximately 5000 K in methane) is slightly lower than the equilibrium temperature for this concentration (approximately 6000 K) and thus provides the quasi-equilibrium state of the plasma.
  • the "cover" region near the channel is quite difficult to measure due to the small concentrations of electrons in it.
  • the concentration of electrons in this region depends on the concentrations of impurities in the gas (which can take part in the process of photoionization and ionization by association). This fact creates serious restrictions on the discharge model near the hot runner.
  • Figure 7 shows the dependence of the process time on the temperature at which the process is carried out.
  • the process time is the same as in the case of methane decomposition (see previous report), only at temperatures below 1500 K.
  • the limiting stage is the dissociation of methane CH4 ⁇ CH3 + H and at temperatures above 1500 K the limiting stage is the decomposition of acetylene.
  • This reaction is endothermic, but if oxygen is added to the incoming mixture, the reforming process is exothermic.
  • This process can be used to receive hg, which will burn in an internal combustion engine or on-board fuel cell.
  • reaction mixture was initially heated and after passing through the reactor, where a periodic discharge of high voltage pulses starts and stimulates the steam reforming reaction, there is also a reformer design that can be used for hg generation , where the h.g. burns in a fuel cell
  • the object of the invention is a plasma converter to convert hydrocarbons into hydrogen-rich gas.
  • the converter includes a heater, a mixer, reactor and microwave source connected to the reactor.
  • a periodic pseudo-corona impulse discharge of Microwave is used to accelerate the conversion process inside the reactor.
  • a pseudo-corona discharge is generated by a set of metal edges introduced into the microwave resonator in the region of maximum electric field.
  • Pulse duration, period-pulse pulse duration ratio, specific energy input, temperature at the reactor inlet a plasma-catalytic character is generated to the conversion process.
  • a plasma-catalytic conversion process is distinguished by its high specific productivity and its low electrical energy requirement at the lower temperature limit.
  • the proposed reactor makes it possible to carry out the process of converting fuel (petroleum, kerosene, diesel fuel, etc.) with steam, with steam-oxygen (steam-air) and also partial oxidation with air in hydrogen-rich gas.
  • fuel petroleum, kerosene, diesel fuel, etc.
  • steam-oxygen steam-air
  • Most of the energy, thermodynamically required to carry out a given process, is supplied to the system as thermal energy from the heater at the expense of heat recovery at the reactor outlet, and also (in case of vapor-oxygen conversion or partial oxidation) at the expense of partial combustion of fuel in the mixer.
  • the heater may include (in case of steam conversion) an arc plasmatron.
  • Supersonic injectors can be used in the mixer, which provide an effective mixture of the initial reactants in less than 10 "3 -1 0 " 5 sec
  • Modern technology allows the proposed device to be built for both a high-production stationary system and the compact design for installation in vehicles.
  • the use of hydrogen-rich gas production equipment from hydrocarbons on board vehicles makes it possible to avoid the use of hydrogen deposits at board.
  • the combined use of the proposed devices (use of adapted internal combustion engines for mixing hydrogen-rich gas and gasoline) on board allows the significant decrease of pollution and increase engine performance.
  • the engine performance characteristics are improved without radical changes in its design.
  • the application of the proposed equipment is its use with the fuel cell to generate electricity that is supplied to the electric motor of the vehicle.
  • the experimental setup shown in Figure 8, consists of: technological block (represented by the dashed line in Figure 1); reagent feed system (fuel, water, air); water supply system modulator, MCW generator, waveguide
  • Water and fuel evaporate in Evaporator 1 and Evaporator 2 and at temperatures greater than their corresponding boiling temperatures, they are fed: water - at the entrance of the heater 2 (arc plasmatron), the fuel - at the entrance of the mixer.
  • the temperature of the water vapor should be sufficient to avoid the condensation of steam during the feeding in the heater 2.
  • the temperature of the steam fuel should be sufficient to avoid the condensation of steam during the feeding in the mixer.
  • the air is heated to a temperature greater than the boiling temperature of the water and is fed with steam at the inlet of the heater 2.
  • the air temperature should be sufficient to prevent condensation of water vapor in the mixture at the inlet of heater 2.
  • the water vapor and the air mixture are heated to an average temperature of the fixed mass depending on the regime chosen (see Tables 2, 3, 4 and 5) and fed into the mixer inlet.
  • the operating regimes of the technology block are determined by the change in power of the heater 2 and / or the changes in the consumption of initial reactants.
  • the heated mixture of reactants is treated by a pseudo-corona microwave discharge of periodic impulse.
  • the products of the process are cooled in the heat exchanger, the condensed phase is separated (water and unreacted fuel, and in some cases coal) in the cyclone heat exchanger.
  • the synthetic gas obtained is sent to the chromatographic analysis. At point “16", the consumption of gas phase products is determined. Necessarily, the consumption of unreacted water and fuel in the liquid phase is determined in item "17".
  • the discharge trigger and the MCW input device constructively enter the technology block.
  • the discharge trigger is a pivot of pointed tungsten, introduced into the reactor in the MCW field, to initiate the microwave discharge of pseudo-corona effect.
  • the measuring points (points "4-1 5") of the main parameters of the technology block are shown in Figure 1.
  • the nominal values of the parameters of the technological block (consumption of reactants, temperature regimes) for the basic regimes of the reaction scheme are shown in Tables 1, 2, 3 and 4.
  • the MCW installation modulator produces a series of periodic voltage pulses, essential for the operation of the MCW generator with the MCW input device.
  • the main parameters of MCW radiation duration of the radiation pulse - 0.1, 1 mks; pulse repetition frequency up to 1 kHz; impulse power - up to 50 kW; medium power - up to 50 W; radiation wavelength - 3 cm
  • the input reactants are fed into the input of the technology block under normal conditions (points 1, 2, and 3 in Figure 1).
  • the cooling water has nearby parameters at the inlet, pressure - 3 atm. temperature - 15 ° - 25 ° C
  • FIG. 9 A diagram of the arrangement of nearby elements of the technological block is shown in Figure 9: heater 2 (arc plasmatron), mixer, reactor, discharge trigger, MCW input device and TC thermocouple group, (the index corresponds to the measurement point in the diagram) for the control of the temperature regime of the block.
  • heater 2 arc plasmatron
  • mixer mixer
  • reactor reactor
  • discharge trigger MCW input device
  • TC thermocouple group the index corresponds to the measurement point in the diagram
  • the diameter of the pipe is 20 mm.
  • the power of the plasmatron is 300 W - without considering the coefficient of plasmatron performance, losses, etc.
  • Work gas water vapor, water vapor mixture with air.
  • thermocouples TC 4 and TC 5 are incorporated in the plasmatron.
  • the TC 9 thermocouple is active and measures the radial temperature distribution at the plasmatron outlet - at the mixer inlet. The possibility of removing the thermocouple from the cross section of the pipe is provided.
  • the parameters of a mixed component are set by the working regime of the arc plasmatron.
  • the mixing time is 10 "4 s.
  • the temperature of the gas after mixing is 500-1560 K.
  • the TC 6 thermocouple is incorporated in the mixer.
  • the TC 10 thermocouple controls the temperature of the gas after mixing in the center of the pipe. The possibility of removing the thermocouple from the cross section of the pipe is provided.
  • the head end reactor is closed by the metal wall MC with holes for the spectral diagnosis of the discharge and a GW sight glass of vacuum glass.
  • the MC wall serves to reflect the MW radiation in the direction of the MCZ DZ discharge zone.
  • the distance between MC and the axes of the MCW radiation entering the device is of the order of 5-10 cm.
  • the "cyclonic" heat exchanger may be connected to - 5?
  • the arrangement of the technology block in this case is horizontal.
  • the reflection of the MCW radiation in the direction of the discharge zone of the mixing zone is obtained by reducing the cross-section of the pipe at the mixer outlet from 20 mm to 15 mm.
  • the MCW radiation input device is a rectangular waveguide that has a cross section of 24 x 11 mm.
  • the wide waveguide wall is oriented along the pipe.
  • the wide wall is 150 mm long.
  • the sealant made of material transparent to the radiation of MW has been arranged.
  • the wheelbase of the input device and the discharge area of MW is of the order of 5 to 10 cm.
  • the initiator of the discharge is a pointed tungsten bar that has a diameter of the order of 2 mm.
  • the initiator is active in the radius of the pipe and there is the possibility of removing the tungsten bar from the cross section of the pipe.
  • the TC ⁇ thermocouple controls the radial temperature distribution of the pipe.
  • the temperature range is 300 to 1 560 K.
  • the thermocouple is active in the radius of the pipe and there is the possibility of removing the thermocouple from the cross section of the pipe.
  • the distance from the discharge zone DZ to the inlet to the reactor-outlet of the mixer is minimal and is defined by particularities of construction of the block elements.
  • the nominal parameters of the process were calculated for the characteristic regimes of the experimental investigations, in order to determine the pattern of consumption of reactants. This data is used for the design of the installation project.
  • the energy input defines the process temperature regime and the value of the degree of equilibrium of the conversion. In the experimental investigations two main regimes are given: varying the power W 4 to a constant consumption of initial reactants Q (Table 1) and varying the consumption of the initial reactants Q at constant heating power W 4 (Table 2).
  • the W MCW ev / W 4 ratio is constant and equal to approximately 15%.
  • the degree of conversion ⁇ corresponds to the degree of conversion of the fuel.
  • the device of our invention serves to carry out the piasmacatalytic processes for the conversion of fossil fuels into synthetic gas rich in hydrogen (mixture of hydrogen with carbon monoxide)
  • the main processes of fuel conversion are:
  • the reagents, before entering the plasmacatalytic reactor area, are preheated to the temperature at which the scale and equilibrium of conversion is sufficient for the reactor. This temperature, as a rule, is too low for the process to be carried out in an acceptable time (kinetic braking).
  • the treatment of reagents previously heated by plasma allows, through chain processes with the participation of the particles chemically active, eliminate kinetic limitations and reach the equilibrium value of the reagent conversion scales.
  • the main part of the device object of the invention is the plasmacatalytic reactor ( Figure 10), in which the previously heated reagents are treated by the periodic microwave pulse discharge of pseudo corona effect.
  • the reactor is a metal tube (1 in Figure 10) of round section which serves both to transport the gas and as a waveguide for the propagation of microwave radiation.
  • Microwave radiation enters the reactor through a standard rectangular waveguide (2) (wave type H01) through the communication hole (3).
  • the communication hole is closed by the hermeticizer (8), transparent for microwave radiation to avoid disturbance of the gas dynamics parameters and to isolate the waveguide conduit from the reactor volume.
  • the wide wall of the rectangular waveguide is along the axis of the tube in which the wave type H1 1 is excited in the round waveguide. The distribution of the electric field E in the rectangular and round waveguides is described in drawings 2 and 3.
  • the diameter of the reactor is chosen under the condition that other (higher) types of waves are not excited in the round waveguide, except the wave of the main type H 1 1.
  • the next type of wave is type E01. Compliance with the condition indicated above leads to the need to maintain the following relationships for diameter D:
  • Lo is the wavelength of microwave radiation in free space
  • Icr the critical wavelengths in the round waveguide for the corresponding wave types
  • the condition for the diameter of the reactor is taken from the indicated ratios:
  • the heated reagents enter the reactor from the mixing block (1 1 in Figure 10) through the reagent inlet element (4).
  • the mixer represents an apparatus with three reagent input systems.
  • the first reagent input system (10) is installed on the system axis. Through it, the heated water vapor (process j), or the heated steam-air mixture (k), or the heated air (I) is sent to the mixer in different variants of the process and conversion.
  • the second and third reagent inlets (9 and 10) represent concentric systems of supersonic nozzles. The use of such nozzles in the construction of the device takes time to mix the reagents at the molecular level of 10-3-10-4 seconds.
  • oxidation of the fuel by the oxygen of the air takes place. The energy produced in the oxidation process heats reagents even more.
  • the input element of the reactants to the reactor (4) represents a part of the tube that narrows towards the mixer.
  • the narrowing scale must be sufficient for the reagent input element to be outside the limit for the H1 1 wave, in other words, for microwave radiation to be reflected from this element to the communication hole (3). This condition leads to the following correlation for the transverse characteristic dimension of the reagent input element - diameter d:
  • Process products leave the reactor through the plug holes (5).
  • the plug is intended to reflect microwave radiation towards the communication hole (3).
  • Another variant for organizing the output system of the products of the reactor process may be a piece of tube analogous to the reagent inlet element (4), but narrowing in the opposite direction.
  • the reactor (L in Figure 10) must equal an integer n of the half-wavelengths lwg / 2 of the microwave radiation in the waveguide:
  • the discharge is initiated by crown element - a sharp bar (6) of little fusible metal, introduced into the waveguide.
  • the tip of the bar increases the value of the microwave electric field E around it and with that the stage of the pseudo corona effect of the discharge is achieved.
  • the bar is oriented along the force lines of field E within the waveguide (figure 12).
  • the position of the tip and the bar (H in Figure 12) is approximately half the radius of the waveguide.
  • the bar In the longitudinal direction (L2 in figure 10) the bar is located in place where the field of the fixed wave in the resonator without download is maximum:
  • the pseudo corona discharge stage estreamers are transformed into the microwave field in the plasma streamer system and propagated in the form of a microwave estreamer filling the tube cross-section and creating the microwave impulse discharge zone (7 in figure 10).
  • the destination of the stage of the discharge of the pseudo corona effect is the generation of plasma at atmospheric pressure with high average electron energy.
  • the fate of the microwave estreamer stage is the creation of a plasma formation developed in space for the catalytic plasma treatment of the reagents.
  • the source of the microwave radiation operates in the impulse-periodicity regime.
  • the duration of the radiation pulse t1 is defined by the time required to perform both stages of the discharge (stage of the pseudo corona effect and stage of the microwave estreamer) under specific conditions.
  • the period of the repetition of the radiation pulses t2 is given based on the optimal coordination of the following quantities: time of existence of the active particles generated by plasma in the passive phase of the discharge after the cessation of the radiation pulse of the radiation super high frequency; linear speed of reagents passing through the discharge zone; energy contribution to the discharge:
  • W " is the average power of the microwave radiation
  • W PULSE - is the impulse power
  • Q - is the consumption of reagents.
  • the pulse power of microwave radiation W PULSE , (h), (i) defines the plasma energy input J PLASMA -
  • the pulse power depends on the magnitude of the electric field in the round waveguide without plasma, which has to have a lower value of the disruptive discharge and, at the same time, be sufficient for the initiation of the stage of the pseudo corona effect of the discharge on the crown element.
  • the thermal energy contribution (energy contribution from the previous heating of the reagents) J heat must be sufficient for the heating of reagents up to the given temperature and for the compensation of the energy consumptions for the realization of the endogenous processes in the system that lead to realization of the
  • Preheating reagents can be done in the following ways:
  • heater with independent power source eg arc plasmatron
  • incineration of a part of the fuel in the combustion chamber e.g arc plasmatron
  • the ratio of plasma energy contribution to the heat energy contribution J p ⁇ asrna / J heat is of the order 1-10%.
  • the following temperatures are characteristic of the fuel vapor conversion process (j) with the 35% transformation scale: heating temperature of water vapors 1450 K, mixing temperature of water vapors ITUTORIA vapors RULE 26 fuels after mixing 890 K-, temperature of process products after completion 620 K.
  • the following temperatures are characteristic for the process of converting fuel vapor (j) with the 65% transformation scale: heating temperature of water vapors 2180 K, mixing temperature of water vapors fuel vapors after mixing 1 150 K, temperature of process products after completion 665 K
  • temperatures are characteristic for the process of the conversion of fuel vapor (j) with the 99% transformation scale: heating temperature of water vapors 3750 K (not counting the processes of dissociation of water molecules ), temperature of the mixture of water vapors-fuel vapors after mixing 1560 K, temperature of process products after completion 800 K.
  • temperatures are characteristic for the process of converting fuel vapor-oxygen (k) with the 65% transformation scale (mole-water ratio; air equivalent to 2.5): temperature of the heating of the mixture steam-air 1390 K, temperature of reagents after mixing 890 K, temperature of process products after completion 650 K.
  • the following temperatures are characteristic: heating temperature of the steam-air mixture 1110 K, TITUTORY RULE 26) reagent temperature after mixing 896 K, temperature of process products after completion 1611 K.
  • the device proposed can perform the conversion processes of fossil fuel with steam, steam-oxygen and fuel vapor in H 2 -gas enriched, and the partial oxidation process stimulated fuel
  • Water vapor is sent to the heater, from there it goes to the first inlet of the mixing chamber and the fuel goes to the second and third inlets of the mixing chamber. According to the required regime, the ratio of the amount of fuel to the second and third inputs of the mixing chamber can be changed in the 0- fingerboard
  • SUBSTITUTE SHEET RULE 26 As a heater, as indicated in Figure 14, a recovery heat exchanger can be used that uses the heat from the reactor outlet and the arc plasmatron connected in series.
  • the temperature of the water vapors, necessary for the process of the conversion of fuel vapor, at the outlet of the heater is in the ranges of 1400-3000 K ° , and the temperature of reagents at the entrance to the reactor is at 900-1500 K °.
  • the general energy balance for the plasmacatalytic process of steam conversion consists of the energy consumption for evaporation of reagents (J steam ), reagent heating and the chemical process.
  • the dependence given is presented in the following table (energy input J SUM is presented in the form of a ratio of the power to the quantity by weight of the liquid reagents).
  • the water vapor mixed with the air is sent to the heater and the fuel is sent to inputs 2 and 3 in the proportion 0.5-2.
  • the temperature at the outlet of the heater is equivalent to 500-600 K and at the entrance to the reactor 800-1500 K °.
  • the mole ratio of water / air vapor and water / fuel vapor varies in the range of 0.3-2 and 3-7 respectively.
  • the air is sent to the heater, and to the second and third inlets of the mixing chamber the fuel in the proportion of 0.5-2 and the molar ratio of air / fuel at the entrance to the reactor equals 8-12.
  • the temperature, necessary for the process of partial oxidation of the fuel, at the outlet of the heater is in the ranges of 500-600 K ° and the temperature at the entrance to the reactor is between 900-1100 K °
  • the magnitude of the J SUM energy contribution is necessary (see p. 3.1.) 1000-1500 kJ / kg. With which the scale of the transformation of the reagents reaches 100%.
  • FIGURE 10- DEVICE CONSTRUCTION
  • FIGURE 11 COORDINATION OF THE DISTRIBUTIONS OF THE ELECTRICAL FIELD IN RECTANGULAR AND ROUND GUIASONDAS.
  • FIGURE 12 BARRA GUIDE ENTRY SYSTEM
  • SUBSTITUTE SHEET (RULE 26 3 - lines of force of the electric field in waveguides of the bar and the discharge. Below is the distribution of the amplitude of the microwave electric field.
  • FIGURE 13 SCHEME OF THE CONVERSION PROCESS OF
  • FIGURE 15- FUEL VAPOR-AIR CONVERSION PROCESS SCHEME

Abstract

L'invention concerne un dispositif permettant la production de gaz riche en hydrogène à partir de combustibles fossiles. Ce dispositif comprend un élément chauffant, un mélangeur et un réacteur à plasma de micro-ondes montés en série ainsi qu'une source d'énergie de micro-ondes. Une décharge d'impulsion périodique pseudo-couronne à pression atmosphérique se produit dans le réacteur et entraîne un processus plasma-catalytique de transformation du combustible à basse température. Ce dispositif permet d'effectuer les réactions de transformation avec de la vapeur, de transformation avec de la vapeur-air et d'oxydation partielle des combustibles fossiles pour l'obtention d'un gaz riche en hydrogène à forte productivité spécifique (rapport volumétrique) et à consommation minimale d'énergie électrique. Le réchauffement préalable des réactifs fournit une grande partie de l'énergie nécessaire à la thermodynamique. Une partie de l'énergie thermique est récupérée à la sortie du réacteur à plasma. Ce dispositif peut se présenter sous forme suffisamment compacte pour être utilisé dans les moteurs à combustion interne de véhicules de transport et peut aussi être utilisé dans des systèmes stationnaires pour la production de gaz riche en hydrogène (centrales génératrices d'énergie électrique, etc.). L'invention trouve aussi une application dans les secteurs de la construction d'équipement à plasma par micro-ondes (réacteur à plasma) et de la construction de moteurs de véhicules. L'invention concerne en outre le procédé de transformation des combustibles fossiles à gaz riche en hydrogène (gaz synthétique) moyennant l'utilisation de plasma généré par des micro-ondes avec addition d'oxygène (ou d'air) et l'éventuelle addition d'eau.
PCT/ES2000/000040 1999-07-29 2000-02-09 Transformateur de plasma de combustibles fossiles en gaz riche en hydrogene WO2001009031A1 (fr)

Priority Applications (7)

Application Number Priority Date Filing Date Title
JP2001514239A JP2003506300A (ja) 1999-07-29 2000-02-09 化石燃料を水素リッチガスに転化するプラズマ転化器
BR0012831-7A BR0012831A (pt) 1999-07-29 2000-02-09 Conversor a plasma de combustìveis fósseis em gás rico em hidrogênio
CA002379892A CA2379892A1 (fr) 1999-07-29 2000-02-09 Convertisseur de plasma de combustibles fossiles en gaz riche en hydrogene
MXPA02001038A MXPA02001038A (es) 1999-07-29 2000-02-09 Convertidor de plasma de combustibles fosiles en un gas rico en hidrogeno.
AU22951/00A AU2295100A (en) 1999-07-29 2000-02-09 Plasma transformer for the transformation of fossil fuels into hydrogen-rich gas
KR1020027001141A KR20020039326A (ko) 1999-07-29 2000-02-09 화석 연료를 고농도 수소 가스로 변환시키는 플라즈마변환기
HK03101157.4A HK1050885A1 (zh) 1999-07-29 2003-02-18 化石燃料轉化成富氫氣體的等離子體轉化器

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
ES009901720A ES2168040B1 (es) 1999-07-29 1999-07-29 Convertidor de plasma de combustibles fosiles en un gas rico en hidrogeno.
ESP9901720 1999-07-29
ES200000027U ES1045040Y (es) 2000-01-07 2000-01-07 Juguete lanzaburbujas.
ESP200000027 2000-01-07

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WO2001089988A1 (fr) * 2000-05-24 2001-11-29 Yasushi Sekine Procede et appareil destine au reformage a la vapeur d'une chaine d'hydrocarbure
WO2002089536A1 (fr) * 2001-04-27 2002-11-07 David Systems & Technology, S.L. Procede permettant de convertir en gaz synthetique par voie plasma catalytique des combustibles susceptibles d'etre utilises dans un moteur a combustion interne ou dans une turbine a gaz et convertisseur plasma catalytique correspondant
US7384619B2 (en) 2003-06-30 2008-06-10 Bar-Gadda, Llc Method for generating hydrogen from water or steam in a plasma
EP2196258A1 (fr) * 2008-12-03 2010-06-16 NGK Insulators, Ltd. Réacteur
CN102536460A (zh) * 2010-12-20 2012-07-04 西安航科等离子体科技有限公司 等离子体废热电能循环利用方法及系统
US8574422B2 (en) 2006-04-07 2013-11-05 Qinetiq Limited Hydrogen production
US9767992B1 (en) 2017-02-09 2017-09-19 Lyten, Inc. Microwave chemical processing reactor
US9812295B1 (en) 2016-11-15 2017-11-07 Lyten, Inc. Microwave chemical processing
US9997334B1 (en) 2017-02-09 2018-06-12 Lyten, Inc. Seedless particles with carbon allotropes
US10428197B2 (en) 2017-03-16 2019-10-01 Lyten, Inc. Carbon and elastomer integration
US10502705B2 (en) 2018-01-04 2019-12-10 Lyten, Inc. Resonant gas sensor
US10644368B2 (en) 2018-01-16 2020-05-05 Lyten, Inc. Pressure barrier comprising a transparent microwave window providing a pressure difference on opposite sides of the window
US10756334B2 (en) 2017-12-22 2020-08-25 Lyten, Inc. Structured composite materials
US10920035B2 (en) 2017-03-16 2021-02-16 Lyten, Inc. Tuning deformation hysteresis in tires using graphene
RU2779848C1 (ru) * 2021-09-14 2022-09-14 Общество с ограниченной ответственностью "ДЕЙЗИНСК" Установка первичной переработки нефти с очисткой ее от серы и пластовой воды

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CN115354098B (zh) * 2022-08-15 2023-07-28 新疆八一钢铁股份有限公司 一种富氢碳循环高炉煤气等离子加热的冶炼方法

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Cited By (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001089988A1 (fr) * 2000-05-24 2001-11-29 Yasushi Sekine Procede et appareil destine au reformage a la vapeur d'une chaine d'hydrocarbure
US7285189B2 (en) 2000-05-24 2007-10-23 Yasushi Sekine Method for steam reforming of chain hydrocarbon
WO2002089536A1 (fr) * 2001-04-27 2002-11-07 David Systems & Technology, S.L. Procede permettant de convertir en gaz synthetique par voie plasma catalytique des combustibles susceptibles d'etre utilises dans un moteur a combustion interne ou dans une turbine a gaz et convertisseur plasma catalytique correspondant
US7384619B2 (en) 2003-06-30 2008-06-10 Bar-Gadda, Llc Method for generating hydrogen from water or steam in a plasma
US8574422B2 (en) 2006-04-07 2013-11-05 Qinetiq Limited Hydrogen production
EP2196258A1 (fr) * 2008-12-03 2010-06-16 NGK Insulators, Ltd. Réacteur
CN102536460A (zh) * 2010-12-20 2012-07-04 西安航科等离子体科技有限公司 等离子体废热电能循环利用方法及系统
US10332726B2 (en) 2016-11-15 2019-06-25 Lyten, Inc. Microwave chemical processing
US9812295B1 (en) 2016-11-15 2017-11-07 Lyten, Inc. Microwave chemical processing
US10937632B2 (en) 2017-02-09 2021-03-02 Lyten, Inc. Microwave chemical processing reactor
US9767992B1 (en) 2017-02-09 2017-09-19 Lyten, Inc. Microwave chemical processing reactor
US10373808B2 (en) 2017-02-09 2019-08-06 Lyten, Inc. Seedless particles with carbon allotropes
US9997334B1 (en) 2017-02-09 2018-06-12 Lyten, Inc. Seedless particles with carbon allotropes
US11380521B2 (en) 2017-02-09 2022-07-05 Lyten, Inc. Spherical carbon allotropes for lubricants
US10428197B2 (en) 2017-03-16 2019-10-01 Lyten, Inc. Carbon and elastomer integration
US10920035B2 (en) 2017-03-16 2021-02-16 Lyten, Inc. Tuning deformation hysteresis in tires using graphene
US11008436B2 (en) 2017-03-16 2021-05-18 Lyten, Inc. Carbon and elastomer integration
US10756334B2 (en) 2017-12-22 2020-08-25 Lyten, Inc. Structured composite materials
US10502705B2 (en) 2018-01-04 2019-12-10 Lyten, Inc. Resonant gas sensor
US10644368B2 (en) 2018-01-16 2020-05-05 Lyten, Inc. Pressure barrier comprising a transparent microwave window providing a pressure difference on opposite sides of the window
RU2779848C1 (ru) * 2021-09-14 2022-09-14 Общество с ограниченной ответственностью "ДЕЙЗИНСК" Установка первичной переработки нефти с очисткой ее от серы и пластовой воды

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