Method for homocracking and differential cracking in gas and liquid molecules

Abstract

The present invention relates to a process for the homocleavage and differential cleavage of release bonding energy in gas and liquid molecules, as well as the use thereof to alter the internal geometry of certain molecules, resulting in the formation of new compounds not contained in the initial gas and liquid, secondary release of energy during the synthesis, without the need to implement nuclear reactions on equipment for its implementation, characterized in that the process comprises the steps of: providing a process for the production thereof; increasing the working environment energy and utilizing this energy to generate thermal energy while synthesizing new compounds due to the physical effect of standing pressure waves on gas and liquid molecules at various temperatures, where the temperature is a measure of activation energy and the molecules are subsequently dissociated into atoms or molecular fragments (free radicals), which are then separated from each other. The atomic partial ionization and subsequent conversion of the atomic bonds of the molecule, with the atomic number unchanged but the atomic weight and proton-neutron ratio altered. The method further comprises converting the neutron mass directly to a mass equivalent to the total mass of 1-electrons and 1-protons, which does not exceed the electrokinetic interaction framework of electrons and nuclei, ensuring no radiation, where the method further comprises the conversion of atoms to chemical molecules or the reverse conversion of 1-electrons and 1-protons from volume to 1-neutrons, which does not exceed the electrokinetic interaction framework of electrons and nuclei, ensuring no radiation. The elementary particles may be free with an external exchange of energy and mass equal to the positively charged mass and equal to a reduction in neutron and proton mass. The method further comprises a reverse reaction to the physical effects forming the new compounds not contained in the initial gas and liquid, releasing the energy generated during the recombination of the atoms into the original molecules, where the proposed method is performed by a combination of initial effects, e.g., 12C1H4 = 16Ne = 16O, e.g., 12C1H4 = 16Ne = 16O, e.g., 12C1H4 = 16Ne = 16O, and 12C1H4 = 16Ne = 16O, e.g., 12C1H4 = 16Ne = 16O. The method further includes rearranging the structures of certain molecules as a physical impact reaction without altering atomic number, mass number, atomic weight, during which new compounds, including those not included in the initial gas and liquid, are synthesized, while releasing the energy generated in these synthesis reactions, such as 14N2 = 12C16O; and 12C16O2 is equal to 14N2 16O. The proposed method is achieved by a combination of initial influences, such as: the temperature is raised to 250 DEG C, ideally 140 DEG C to 150 DEG C; reducing the pressure (creating a reduced pressure atmosphere) to-100 kPa, ideally-65 kPa; generating standing pressure waves; a discharge with a breakdown voltage of 1 to 15 kV (tribostatic discharge, barrier discharge, spark discharge); the magnetic field value in the reactor is 70 to 120 nTl depending on the discharge condition in the gas; a micro-explosion; an impact, an impact force, producing a negative acceleration of 50,000 to 150,000 g; or a combination of these effects. The device for converting hydrocarbon and non-hydrocarbon gases and liquids consists of: an acceleration module, which is a piece of device for accelerating a mixture of gases and liquids to a speed of 30 to 400 m / s; a deceleration module, which is a friction electrostatic energy generator, covering 70% to 90% of the cross-section of the reactor; a friction electrostatic generator consisting of two electrodes arranged side by side on which positive charges and negative charges are generated from each other; and a reduced-pressure atmosphere zone behind the deceleration module.

Description

Technical Field

[0001] The present invention relates to a method for homolysis and heterolysis in molecular gases and liquids, and for releasing binding energy, which is used for synthesizing new compounds and generating heat energy and microwave energy. It aims to solve the problem of chemical synthesis and excess heat energy generated by changing the composition due to the release of binding energy in molecules and atoms in non-equilibrium weak ionization cold plasma, in gas and in liquid, and to produce new chemical substances in the framework of molecular electrodynamic interaction and without involving nuclear reactions. The present invention also relates to an apparatus for implementing the method.

[0002] The present invention can be used for:

[0003] Utilize the gases produced during the combustion process;

[0004] Production of organic synthesis products;

[0005] Producing green hydrogen; Background Art

[0006] Method and apparatus for generating energy from matter.

[0007] Ionization (cold plasma chemistry) is a known phenomenon in which electrons are ejected from the outer shells of atoms of oxygen, nitrogen, argon and other gases and form ions and other reactive species. Ionization requires temperatures of about 3000°C and can be produced by electrical pulses (Industrial Herald, 9, 1999, p. 19).

[0008] A method for generating heat energy based on nuclear reactions is known, which occurs when cavitation bubbles in water collapse. Cavitation bubbles are formed in liquids by periodically changing pressures generated in cavitation equipment used as "ultrasonic activators". When the bubbles "collapse", the pressure difference accelerates their surfaces; they gain kinetic energy and collide at the center. The energy generated and concentrated in the microdomain is sufficient to destroy part of the bonds between the atoms in the molecules and the nuclei in the atoms, and partially decompose them into elementary particles contained in the working material. As a result, a nuclear reaction occurs at the moment the cavitation bubbles collapse, releasing a large amount of heat energy (RF Patent 2054604, F 24J 3 / 00.Bull.5, February 20, 1996). However, the released heat energy has a low potential energy, which limits the possibility of practical application. In addition, the substance (working medium) must be in a liquid state.

[0009] There is a method to increase the energy of the working medium, which involves exposing cavitated water to a catalyst (e.g., inert argon), which can increase the sonoluminescence of water by three times (MA Margulis. Sonochemical reactions and sonoluminescence-M.: Chemistry, 1986. p. 288). However, the absolute energy level of this method is negligible.

[0010] There is a method for increasing the energy of a working medium for electrical machines and thermal power plants, which method comprises passing electrical pulses through the working medium, for example by magnetic poles, laser beams or arcs (British Patent Application No. 2241746, F 02G 1 / 02. Edition no. 65, no. 5, 1993, p. 22).

[0011] Known devices for improving the air in internal combustion engines (ICE) are known, which ozonate the air before mixing it with the fuel, increasing the completeness of the fuel combustion and reducing the toxicity of the engine exhaust. The ozonation of the air is achieved by moving the air to a stream of electrons generated by a corona discharge between two electrodes (USSR Author's Certificate No. 1341366, F 02M27 / 00, Bull. No. 3 of 30.9.1987). The disadvantage is that the device is complex and requires a sufficiently powerful current generator.

[0012] It is known that when air is exposed to electric or magnetic pulses, only oxygen molecules dissociate into negative ions. In this case, nitrogen molecules do not dissociate because the dissociation energy of nitrogen molecules is twice that of oxygen molecules (USSR Author's Certificate No. 1825887, F 02M 27 / 04, Bull no. 25 of 7.7.1993).

[0013] There is an apparatus for treating fuel components with a catalyst to provide improved fuel combustion efficiency. The apparatus comprises a sealed cylinder with a particulate catalyst (RF Patent No. 1799429, F 02M 27 / 00, Bull. No. 8 of 28.2.1993).

[0014] A method and apparatus for converting natural gas (methane) into organic matter and hydrocarbon fuels.

[0015] Natural gas can be converted into liquid fuels by a variety of known methods. These methods include, for example, the Fischer-Tropsch process, and a multi-step process developed by Mobil Corporation for converting gas into liquid using plasma. The Fischer-Tropsch process and the process developed by Mobil Corporation comprise multiple synthesis stages, in which light hydrocarbons (i.e., gaseous hydrocarbons) are first converted into synthesis gas at high pressure and temperatures up to 1300K (1026.85°C). Synthesis gas is a mixture of carbon monoxide (CO) and hydrogen (H). Synthesis gas is typically produced by burning gaseous hydrocarbons in the absence of oxygen. The following reaction is used to illustrate an example of the above known methods:

[0016] CO+H 2 →Liquid hydrocarbons (Fischer-Tropsch synthesis)

[0017] CO+H 2 →CH 3 OH and / or other liquid hydrocarbons (Mobil method)

[0018] The extremely high temperatures required in the cracking unit mean that gas synthesis requires large structures and is expensive to operate. GTL facilities must be large and complex to be commercially viable. The energy required to compress and heat the gas is very expensive to operate and accounts for 60% to 80% of the total cost of producing fuel by this method. In addition, expensive catalysts are used in almost all stages of the known conversion processes and usually need to be replaced.

[0019] Another approach to converting light hydrocarbons to liquid fuels is to use non-thermal plasma processes.

[0020] USA Patent No. 7,033,551 describes a reactor system comprising an electrochemical cell and using a dielectric barrier discharge, during which liquid products are formed mainly by oligomerization of gaseous hydrocarbon radicals in a non-thermal plasma during a gas barrier discharge. The non-thermal plasma ensures the initial concentration of free radicals, which is the result of the dissociation of light alkane molecules by high-energy electrons at low temperatures (about 100°C to about 600°C) and low atmospheric pressure of the gas. In conjunction with the barrier discharge, the electrochemical cell allows the oxidation of excess hydrogen in the plasma, as well as incomplete oxidation and oxidative condensation of the main gases. The final composition means a mixture of liquid hydrocarbons with a small amount of their alcohols. The disadvantages of this technical solution are the use of an external discharge source, the fact that the conversion process in the barrier discharge reactor is not a chain reaction, and the high activation energy of the main formation process of free radicals.

[0021] USA Patent No. 6,375,832 describes the synthesis of liquid products by barrier discharge, where the use of a catalyst is optional. The synthesis method described in this patent uses direct synthesis and oxidative condensation to produce hydrocarbon radical oligomers by dissociating the source gas and converting hydrocarbons from the radical fragments. If CO 2 Added as an oxidant to the original mixture, carbon dioxide also undergoes conversion, which contributes to the formation of liquid hydrocarbons. The disadvantage of this technical solution is the use of an oxidant and an external discharge source.

[0022] The following patents:

[0023] US Patent No. 8 203 027 B2 - Continuous process and plant design for converting biogas into liquid fuels

[0024] RU (11) 2012 112 065A - Non-fractionation process for producing low-boiling-point fuels from crude oil or its fractions;

[0025] US 2011 / 0049014A1 - Continuous process and plant design for converting biogas into liquid fuels;

[0026] US2011 / 0000128A1 - Process for converting biogas into liquid fuel;

[0027] US 7 880 044 B2 - conversion of biogas into liquid fuels;

[0028] US 8 226 817 B2 - non-fractionation process for producing low boiling point fuels from crude oil;

[0029] Each describes methods and devices for improving the quality characteristics of automotive fuels and for the conversion of biogas and natural gas, in which the concentration of methane must be at least 50% or 80%. The conversion of methane is achieved by passing a mixture of gaseous and oily liquids through a metal grid, on which a voltage of an undefined (uncontrolled) frequency is spontaneously generated. The disadvantage of this technical solution is the low efficiency of methane conversion, which gradually disappears to zero over time.

[0030] There is a known method for high temperature oxidative conversion of methane to produce C using a heterogeneous catalyst containing alkali metal ions, manganese ions, tungsten ions and silicon oxide ions. 2 -C 3 Hydrocarbons (Patent 2341507, RU-hereinafter referred to as "D3"). This conversion occurs when the catalyst temperature is 734-910℃, C 2 -С 3 The selectivity reached 87.6% and the methane conversion rate was 20% (C 2Hydrocarbons: 81% for ethylene and ethane). The disadvantage of this method is the use of high temperatures and external discharge sources.

[0031] There is a known method for converting methane in a discharge plasma [Shigeru Kado, Yasushi Sekine, Tomohiro Nozaki, Ken Okazaki / Catalysis Today 89, (2004), 47-55]. The following are data on the selectivity of hydrocarbon formation in barrier discharge: 2 ~39% (ethane ~35%; ethylene ~2.5%; acetylene ~1.5%) and С 3 -С 5 Hydrocarbons ~ 32%, others ~ 26% and carbonaceous deposits ~ 3%. After comparing corona, spark and barrier discharges, it was found that the methane conversion rate was higher and the proportion of carbonaceous deposits was lower in the barrier discharge case. The disadvantage of this method is the low selectivity for hydrocarbons ≥ 2+ and carbon deposits detected in the external discharge source reactor.

[0032] Patent 2466977RU describes a method for methane conversion using water, with a methane flow rate of 0.63 to 3.6 l / h -1 And the water flow rate is 1.3 to 6 ml / h -1 , delivered to the reactor at a temperature of 25° C. to 120° C. and the reactor discharge time is 12 to 72 s. The use of an external discharge source is a shortcoming of this technical solution.

[0033] Another important limitation of barrier discharge plasma based methods is the low current values ​​(10-5-10-3 A / cm 3 ) and the energy density of the barrier discharge plasma released (1-10W / cm 3 ), thereby reducing the productivity of the reactor system. In addition, the above-mentioned method based on the use of plasma can only adjust the temperature of the source gas.

[0034] At the current state of the art, methane is converted to produce С by using the barrier discharge plasma effect in a reactor with a dielectric barrier. 2+ The hydrocarbon approach is closest to the proposed approach, but this is limited to the conversion of methane.

[0035] Another known state-of-the-art technology is patent RU 2003132259A, a method for heating a liquid by changing its physical and mechanical parameters by cavitation, which can be further enhanced by introducing a gas containing methane and oxygen into the liquid. This heat energy is used in the liquid in which the cavitation process takes place to stimulate the synthesis of organic compounds (alcohols) and higher hydrocarbons of oxygen, which are contained in the chemical compounds contained in the initial liquid and gas. This will generate additional heat energy, which can be used to heat the physical medium in other processes. In the patent currently applied for, the invention claims the application of various physical methods to the liquid or gas, resulting in a structural rearrangement of certain molecules without changing the mass number or atomic weight, but sometimes changing the atomic number, and as a response to the physical activity, synthesizing new compounds, including compounds not contained in the original gas and liquid, while releasing (consuming) the energy generated in these synthesis reactions.

[0036] Another state-of-the-art technology is WO 9729833A1 (ABB RESEARCH LTD) 21 / 08 / 1997, which relates to a method for converting one of greenhouse gases CO2, N2O into synthesis gas, and then into chemically or technically suitable substances, by accelerating the reaction of N2 and N2O in the presence of hydrogen-containing gases H2, H2S, CH4 under the action of a solid catalyst, and then into a chemically or technically suitable substance. In the invention now filed, there is a claim for the application of various physical agents acting on liquids or gases, causing the rearrangement of certain molecular structures without changing the mass number or atomic weight, sometimes the atomic number will change, as a response to the physical activity, synthesizing new compounds that are not contained in the original gas and liquid, and releasing (consuming) the energy generated in these synthesis reactions, such as, without using hydrogen-containing gases, converting CO2 into air components or converting N2 into CO components, and then into C and CO2, for example, according to the following model:

[0037] ·СΟ 2 =N 2 O 6;

[0038] 2N 2 O=2N 2 +O 2 7;

[0039] ·O 2 =N 2 +2H 2 8;

[0040] or the following model:

[0041] ·N 2 =CO 9;

[0042] 2CO=C+CO2 10;

[0043] Different from Patent No. WO 9729833, in the patent application filed herein, nitrogen directly participates in the greenhouse gas conversion process.

[0044] Another state-of-the-art technique is the paper entitled "TV Bonner and WM Rubaker: Nitrogen decay by neutrons", because in the scheme described, nitrogen atoms decay in nuclear reactions under the influence of external neutrons:

[0045] · 14 N 7+0 n 1 → 11 B 5 + 4 He 2 1

[0046] · 14 N 7+0 n 1 → 14 C 6 + 1 H 1 2

[0047] · 14 N 7+0 n 1 → 4 He 2 + 4 He 2 + 7 Li 3 3

[0048] However, in the presently filed invention, nitrogen molecules are converted into new compounds not contained in the original gas and liquid, and protons and neutrons in the molecules are not gained or lost, i.e., no nuclear reactions occur, e.g.:

[0049] ·

[0050] · Summary of the invention

[0051] The method according to the invention for releasing binding energy by homolysis and heterolysis of gas and liquid molecules, using this energy to synthesize new compounds and generate heat and microwave energy eliminates the above-mentioned disadvantages. Its essence is to increase the energy of the working environment and use this energy to generate heat energy as a result of the physical action of standing pressure waves on gas and liquid molecules at different temperatures, while synthesizing new compounds at the same time, where the temperature is a measure of the activation energy, the molecules then dissociate into atoms or molecular fragments (free radicals), partial ionization of atoms and subsequent transformation of the atomic bonds of the molecules without changing the atomic number, but with a changed atomic weight and a different proton-neutron ratio. The method further includes the direct conversion of neutron matter into a mass equivalent to the total mass of 1 electron and 1 proton, which does not exceed the framework of the electrodynamic interaction of electrons with atomic nuclei, thereby ensuring the absence of radiation. The method further includes the conversion of atoms into chemical molecules or the reverse conversion of 1 electron and 1 proton in the volume into 1 neutron, where these elementary particles may be free, with external energy exchange and a mass equal to the mass of the positive charge, and equal to the mass loss of neutrons and protons. Furthermore, it also includes the reverse reaction to physical actions that consist of the formation of new compounds not contained in the initial gas and liquid, the release of energy generated during the reorganization of atoms into the original molecules, where the proposed method is performed by a combination of initial impacts, such as:

[0052] Raise the temperature to 250°C, preferably 140°C to 150°C;

[0053] Reduce the pressure (create a reduced pressure atmosphere) to -100 kPa, preferably -65 kPa;

[0054] Generate standing pressure waves;

[0055] Discharge with a breakdown voltage of 1 to 15 kV (tribostatic discharge, barrier discharge, spark discharge)

[0056] Based on the discharge in the gas, the magnetic field value in the reactor is 70 to 120 nTl;

[0057] Micro explosion;

[0058] Shock, a force that can produce negative accelerations of 50,000 to 150,000 g;

[0059] or a combination of these effects.

[0060] Apparatus for the conversion of gases and liquids of hydrocarbons and non-hydrocarbons, which utilizes only physical impact methods, in particular standing pressure waves and triboelectrostatic effects, in which case the gaseous components are conveyed to a reactor, and which consists of:

[0061] The acceleration module is a device that accelerates the gas and liquid mixture to a speed of 30 to 400 m / s;

[0062] The deceleration module, which is a triboelectrostatic energy generator, occupies 70% to 90% of the reactor cross section;

[0063] · Tribostatic generator, consisting of two electrodes placed side by side, on which positive and negative charges are generated by each other;

[0064] ·Decompression atmosphere area after the deceleration module.

[0065] The following technical equipment can produce non-equilibrium cold plasma:

[0066] An acceleration module, in which the first impact process occurs and supersonic airflow is formed;

[0067] A deceleration module that slows down the airflow and creates triboelectric electrostatic voltage and discharge on its electrodes;

[0068] A decompression zone after the decompression module; the velocity of the gas flow and therefore the intensity of the process in the decompression module depends on the value of its decompression.

[0069] The device is equipped with an input pipe for feeding gas and an output pipe for extracting:

[0070] Inorganic liquids, organic liquids, hydrocarbon liquids or mixtures thereof with modified compositions;

[0071] Non-hydrocarbon and hydrocarbon gases, or mixtures thereof with modified composition;

[0072] Thermal energy, the value of which is such that the energy efficiency value is greater than 1; in the device, the level of the liquid component in the reactor is kept close to the acceleration module. The specific plasma energy of the device ranges from 0.01 J / cm3 to 16 J / cm3. In the device, the tribostatic electric field strength based on the gas discharge in the reactor is less than 14 kV / cm. In the device, the magnetic field value based on the discharge in the gas in the reactor is 70 to 120 nTl.

[0073] Due to the dissociation and ionization of gas and liquid molecules, i.e. the process of separating electrons from molecules or atoms, plasma components - electrons and positive ions - are formed in the space between the electrodes. The mechanical and thermal energy used is converted into ionization energy. The smaller the ionization energy, the more positive the element is, which means that the lower and to the left it is in the group of the periodic table (alkali metals are the smallest and noble gases are the largest). Ionization causes the matter to fragment.

[0074] As soon as they are released, the bound electrons of the atoms begin to function as generators of further energy. Due to the principle of minimum surface energy, the direct discharge breaks down into fragments and transforms into ball lightning, thus generating a non-equilibrium cold plasma. When the gas / liquid mixture is suddenly decelerated, a reverse sound wave is formed, which moves in the direction of the direct wave source and, under its influence, returns to the deceleration zone, where a sudden release of pressure occurs, the molecules "explode" and break down into atoms, fragments and even nuclei, producing a noticeable dynamic impact on their neighbors. Two identical gas and liquid molecules exchange impulses through a one-time interaction, causing them to expand at a specific speed and thus achieve the same interaction with other molecules. The same happens when molecules of gaseous or liquid working substances come into contact with the solid matter of the catalyst in the deceleration module.

[0075] When the working substance molecules interact with the catalyst molecules, they are first affected by their attractive forces; subsequently, they are also affected by the forces of other catalyst molecules, which is the result of dynamic electromagnetic interactions, which significantly increases the dynamic acceleration of the working substance molecules toward the deceleration module and the catalyst. Unlike gas molecules, solid catalyst molecules only vibrate and do not rotate. Therefore, gas molecules moving toward the catalyst do not encounter the repulsive force of the countercharge field.

[0076] The electrostatic field stabilizes the movement of the gas molecules towards the target catalyst: as in any electrodynamic interaction, the gas molecules stop their rotation and choose the shortest route. All this contributes to their accelerated movement towards the target, increasing the shock load at the time of impact and destroying their molecules themselves. In this case, the neighboring molecules of the working substance do not interfere with the process and do not prevent the acceleration of the molecules, because at that moment they are interacting with other molecules.

[0077] The attractive force increases inversely with the square of the distance and directly proportional to the product of the opposite charges of the interacting bodies. If we consider that the molecules move at speeds ranging from 30 to 400 m / s during the interaction, then when they approach the deceleration module, their speed rapidly increases many times, resulting in a collision and an immediate decay of their speed.

[0078] This very obvious nonlinearity is very similar to the energy curve of cavitation bubbles in liquids. In both cases, the energy is proportional to the square of the speed, gradually accumulated, and then suddenly released in a very short time. It is obvious that the low reaction speed causes a huge reaction intensity, thanks to the high speed that can destroy the effect of the material molecules.

[0079] Of course, the reorganization of atoms, especially nucleons, into reaction products under the action of a catalyst has a lower activation barrier than the reorganization of molecules, which ensures that the reaction does not occur without a catalyst, which also accelerates the reaction, while also excluding the increased energy intensity in the reaction zone. The molecular deceleration mechanism ultimately leads to the decomposition of the molecules of the working substance and the interaction of their smaller parts - atoms, fragments and even nucleons - with the formation of reaction products, without initiating a chain reaction.

[0080] The proposed method and the device for its implementation are based on experimental data and data from alternative atomic and molecular spectroscopy. The fundamental law of AMButlerov's theory of structure states: "The chemical properties of a complex particle are determined by the nature of its elemental components, their quantities and chemical structure... Substances containing the same elemental components in the same quantities differ because the kinematic dependencies between the atoms of these parts are resolved differently in different cases..."

[0081] The advantage of the present invention is that it represents a universal method in which liquid and gas molecules are exposed to external influences in the form of shock waves under cryogenic conditions within a given volume, resulting in molecular dissociation, atomic ionization and reorganization of bonds in these molecules, releasing excess energy for chemical synthesis reactions.

[0082] The physicochemical process of the present invention

[0083] (The process is demonstrated by reactions 1 to 38 in Table 1)

[0084] The method implements the following physicochemical principles:

[0085] 1. External physical factors cause any gaseous or liquid substance, including natural and renewable carbon dioxide, air, water, etc., to be decomposed into atoms that form molecules.

[0086] 2. Under natural conditions, based on the energy-mass and mass-energy exchange process in quantum vacuum, the energy and mass shortages and surpluses of the reaction products disappear and regenerate, thereby reducing the consumption of the initial substance.

[0087] 3. The amount of energy generated by the bond breaking-recombination process by means of plasma electrons changes the geometry (length, angle) of the bonds in the atoms of the original molecule, producing new chemical elements. The original electron donor is any gas.

[0088] 4. While the substances in the catalyst volume are being decomposed and synthesized, excess heat energy is released, which is converted into electrical energy with an efficiency coefficient reaching the level of existing industrial equipment and is fed back into the process, thereby improving the energy efficiency of the process in commercial applications for industrial processes.

[0089] For example:

[0090] Nitrogen molecule N 2 (total atomic number 14, atomic weight 28) is converted to:

[0091] Symmetric decomposition:

[0092] Two nitrogen atoms N, total atomic number 14, atomic weight 28, which may recombine to form a nitrogen molecule, or;

[0093] · For two CH 2 Free radical, total atomic number 16, atomic weight 28, or;

[0094] ·For one CH 2 A free radical and a hydrogen atom H 2 and one carbon atom C, the total atomic number of the fragments and the new element is 16 and the atomic weight is 28; or

[0095] · Two carbon atoms 2C and four hydrogen atoms 4H, the total atomic number of the product is 16, the atomic weight is 28, or;

[0096] · Carbon atom C and methane molecule CH 4 , the total atomic number of the product is 16, and the atomic weight is 28;

[0097] Asymmetric decomposition:

[0098] · Oxygen atom O and carbon atom C, total atomic number 14, atomic weight 28, and;

[0099] · is a carbon monoxide molecule CO in a reaction between a carbon atom C and an oxygen atom O, with an overall atomic number of 14 and an atomic weight of 28, or;

[0100] Parallel processes of symmetric and asymmetric decomposition of nitrogen molecules:

[0101] Possible synthesis:

[0102] Water molecule H 2 O and;

[0103] Oxygen molecule 2 and;

[0104] · In carbon C and molecular oxygen O 2 CO in the combustion reaction between 2 molecules, as well as in methane CH 2 With two molecules of oxygen O 2 The reaction between CO 2 Molecules and water molecules H 2 O, and;

[0105] Organic and hydrocarbon molecules in polycondensation reactions, and the synthesis of:

[0106] o aldehyde;

[0107] o Ketone;

[0108] o alcohol;

[0109] o Simple and complex ethers;

[0110] oFatty acids;

[0111] o Alcohols of fatty acids;

[0112] o Hydrocarbon gases;

[0113] o Hydrocarbon liquids:

[0114] For example:

[0115] Oxygen molecules O 2 (total atomic number 16, atomic weight 32) is converted to:

[0116] Symmetric decomposition:

[0117] · Two oxygen atoms O, total atomic number 16, atomic weight 32, and;

[0118] · Two nitrogen atoms N(N 2 molecule) and four hydrogen atoms (2H 2 ), total atomic number 18, atomic weight 32, and;

[0119] · For two CH 2 A free radical and two hydrogen molecules, total atomic number 20, atomic weight 32, or;

[0120] ·For one CH 2 Free radicals, and three hydrogen molecules H 2 and carbon atom C, total atomic number 20, atomic weight 32, or;

[0121] · Two carbon atoms 2C and eight hydrogen atoms 8H, total atomic number 20, atomic weight 32, or;

[0122] · Two methane molecules CH 4 , total atomic number 20, atomic weight 32;

[0123] Asymmetric decomposition:

[0124] · Nitric oxide molecule NO and two hydrogen atoms, total atomic number 17, atomic weight 32, or;

[0125] · A nitrogen molecule and four hydrogen atoms, with a total atomic number of 18 and an atomic weight of 32, and;

[0126] · For two CH 2 Free radical and 4 hydrogen atoms, total atomic number 20, atomic weight 32, or;

[0127] ·For one CH 2 Free radicals, and three hydrogen molecules H 2 and carbon atom C, total atomic number 20, atomic weight 32, or;

[0128] · Two carbon atoms 2C and eight hydrogen atoms 8H, total atomic number 20, atomic weight 32, or;

[0129] · Two methane molecules CH 4 , total atomic number 20, atomic weight 32;

[0130] The parallel process of symmetric and asymmetric decomposition of oxygen molecules makes possible the following synthesis:

[0131] Water molecule H 2 O, and;

[0132] Oxygen molecule 2 ,and;

[0133] · In carbon C and molecular oxygen O 2 CO in the combustion reaction between 2 molecules, as well as in methane CH 2 With two molecules of oxygen O 2 The reaction between CO 2 Molecules and water molecules H 2 O, and;

[0134] Organic and hydrocarbon molecules in polycondensation reactions, and the synthesis of the following products:

[0135] o aldehyde;

[0136] o Ketone;

[0137] o alcohol;

[0138] o Simple and complex ethers;

[0139] oFatty acids;

[0140] o Alcohols of fatty acids;

[0141] o Hydrocarbon gases;

[0142] o Hydrocarbon liquids:

[0143] In the process of forming carbon and hydrocarbon liquids and gases, there will be a deficiency (lack) in the weight of the products. When hydrocarbon gases and liquids decompose, matter is converted into energy.

[0144] According to the method, molecules of other hydrocarbon gases (including toxic gases) can be exposed to decompose, for example:

[0145] ·N 2 O and other oxides of nitrogen;

[0146] ·H 2 S;

[0147] ·SO 2 ;

[0148] Fluoride;

[0149] For example:

[0150] Methane molecule CH 2 , with an overall atomic number of 10 and an atomic weight of 16, will change the geometry of its bonds and acquire new properties or transform into another chemical element:

[0151] · O is the oxygen atom, with atomic number 8 and atomic weight 16;

[0152] Two methane molecules (total atomic number 20, atomic weight 32) are converted into oxygen molecules, total atomic number 16, atomic weight 32;

[0153] · Nitrogen and hydrogen atoms, total atomic number 9, atomic weight 16;

[0154] Two methane molecules (total atomic number 20, atomic weight 32) are converted into two nitrogen molecules and two hydrogen molecules, total atomic number 18, atomic weight 32;

[0155] When the geometric configuration of the bonds between nucleons and electrons changes, a defect (excess) in the product weight will appear. The excess weight occurs by converting protons + electrons + energy into neutrons. Therefore, the amount of product will be greater than the input material used, as observed in the tests. The mechanism of neutron formation from proton-electron pairs is caused by the change (increase) in the strength of the external magnetic field and the synchronization of the magnetic poles of protons and electrons in the neutron space. The electrons and protons in the methane molecule rotate with opposite magnetic poles, and in the process, the electrons transition to lower energy levels in the newly emerged neutron space and emit photons.

[0156] This method solves the problem of treating industrial greenhouse gas CO 2 , CH 4 , water vapor, N 2 O, O 3 (Ozone) problem.

[0157] For example:

[0158] Depending on the energy of external influences, Carbon dioxide molecule CO2, total atomic number 22, atomic weight 44:

[0159] Dissociate according to formula 24 and 25;

[0160] 2CO 2 =2CO+O 2 (twenty four);

[0161] CO 2 =C+O2 (25);

[0162] In reactions 24 and 25, the sum of the product atomic weights is 88 or 44, respectively. Reaction 16 may be continued to:

[0163] CO=C 2 H 4 (26);

[0164] The atomic weight of CO is 29, 2 H 4 The atomic weight of is 28. Due to the decomposition and transformation of oxygen molecules, the final reaction 16 is:

[0165] CO 2 =C 2 H 4 +CH 4 (27);

[0166] CO 2 The atomic weight of C is 44. 2 H 4 The atomic weight of CH is 28. 4 The atomic weight of is 16, and the total atomic number of the product is 44.

[0167] For example:

[0168] Depending on the energy of external influences, Nitrous oxide sub-N 2 O, total atomic number 22, atomic weight 44:

[0169] Dissociate according to formula 28 and 29;

[0170] 2N 2 O=2N 2 +O 2 (28);

[0171] N 2 O = 2N + O (29);

[0172] In reactions 28 and 29, the total atomic weight of the product is 88 or 44, respectively. Reactions 20 and 21 can be continued to carry out reactions 1 to 23.

[0173] For example:

[0174] Depending on the energy of external influences, Water molecules H 2 O, total atomic number 10, atomic weight 18:

[0175] Dissociation according to formula 30 and 31:

[0176] 2H 2 O=2H 2 +O 2 (30);

[0177] H 2 O=2H+O (31);

[0178] In reactions 30 and 31, the total atomic weight of the product is 36 or 18, respectively. Reactions 30 and 31 can be continued to carry out reactions 1 to 23.

[0179] For example:

[0180] Depending on the energy of external influences, Ozone molecule O 3 , total atomic number 24, atomic weight 48:

[0181] Dissociation according to formula 32 and 33:

[0182]

[0183] O 3 =3CH 4 (33);

[0184] In reactions 32 and 33, the total atomic weight of the product is 48. Reactions 32 and 33 can be continued with reactions 1 to 23.

[0185] For example:

[0186] Depending on the energy of external influences, Chlorine molecule Cl 2 , total atomic number 34, atomic weight 68:

[0187] Dissociation according to formula 34 and 35:

[0188] Сl 2 =Cl+Cl(34);

[0189] Cl 2 =2H 2 S(35);

[0190] In reactions 34 and 35, the total atomic weight of the products is 68. The continuation of reaction 35 is determined by the following equation:

[0191] Cl 2 =2H 2 O 2 (36)

[0192] In reaction 36, the total atomic weight of the product is 68. The continuation of reaction 36 is determined by the following equation:

[0193] Cl 2 =2H 2 O+O 2 (37)

[0194] In reaction 37, the total atomic weight of the product is 68.

[0195] Reaction 37 can be continued through reactions 1 to 23.

[0196] CO、COCl 2 , NO, H 2 The reaction mechanism of S gas has been explained in the previous section.

[0197] The proposed method solves the problem of treating toxic gas Cl 2 、CO、COCl 2 (phosgene), NO (nitric oxide), H 2 S (hydrogen sulfide) problem. BRIEF DESCRIPTION OF THE DRAWINGS

[0198] The present invention will be explained using diagrams, wherein Figure 1 Show the structure of the device; Figure 2 An acceleration module is shown; Figure 3 A deceleration module is shown; Figure 4 A general flow chart of the method according to the present invention is shown; and Table 1 gives an overview of the reactions of the chemical elements. Figure 5 An analysis of the products in the reactor boiler R1 of the three-phase separator F1 is shown.

[0199] Figure 1 The relationship between the density of the generated products and the duration of gas action is shown when the gas moves from the acceleration module to the deceleration module and the friction electrostatic generator. Figure 2 The relationship between the weight of the manufactured product and the duration of the gas action from the acceleration module to the deceleration module and the tribostatic generator is shown. Figure 3 The relationship between the weight of the formed product and the physicochemical properties of the gas from the acceleration module to the deceleration module and the tribostatic generator is shown. Figure 4 The relationship between the density of generated products and the physicochemical properties of the gas from the acceleration module to the deceleration module and the tribostatic generator is shown. Figure 5The standard distillation test is shown in the form of a distillation curve ( EN ISO 3405). Figure 6 The distribution of each hydrocarbon group according to the number of carbon atoms is shown using gas chromatography. Figure 7 The gas chromatography results used in Example 6 are shown. Figure 8 The gas chromatography results used in Example 7 are shown. Figure 9 Analysis of the starting material and product from the separator used in Example 8 is shown. Chart 10 A more detailed chromatographic analysis of sample "N2, 20 / 04 / 2018" is shown. Chart 11 The distribution of hydrocarbons in the sample "N2, 20 / 04 / 2018" is shown. Chart 12 Represents the analytical chromatogram of sample "14.8.18" (nitrogen, no recycle). Chart 13 The chromatogram record of sample 3GTL-(060620181), A, 6 / 6 / 18 / 1 is shown. Chart 14 The chromatogram record of sample 3GTL-(060620182), A, 6 / 6 / 18 / 2 is shown.

[0200] Table 1 is an overview of all physicochemical reactions. DETAILED DESCRIPTION

[0201] The gas mixture from the external source and the circulating device passes through the pipe 1 Transfer to the connection acceleration module 2 The gaseous mixture is fed into the reactor and passes through the tube into the inner space of the reactor. 3 .

[0202] Acceleration module 2 A hypersonic shock tube is a device that accelerates a gas mixture to supersonic speeds exceeding 5 Ma. A hypersonic shock tube consists of tubes connected in series. 2a , receiving cavity 2b , Acceleration module 2 and its output leads to the reactor interior space 3 Hypersonic nozzle. Hypersonic nozzle is made into multiple Laval nozzles 2c in the form of a beam 2d . 2c The number of nozzles and 2d The amount of beam flow ensures the passage of gas or liquid.

[0203] Acceleration module 2 The tube 2a and high pressure chamber 2b Assemble the pressure sensor. The interior space of the reactor 3 A pressure sensor is also installed in the instrument. The sensor is connected to a data logging computer.

[0204] A hypersonic shock tube works as follows:

[0205] Acceleration module 2 The tube 2a and high pressure chamber 2b The input gas mixture is filled in the 2a and high pressure chamber 2b The standing pressure wave is initiated by a simple method such as the pressure in the nozzle. The standing pressure wave reaches the hypersonic Laval nozzle through the conical channel. 2c . Some waves enter the hypersonic nozzle 2c The other part passes through the hypersonic nozzle. 2c , and high-speed flow from the hypersonic nozzle 2c Entering the interior space of the reactor 3 , and then enter the deceleration module 4 .

[0206] The input flow is accelerated to velocities exceeding 5 Ma. The velocity range determines the change in the gas medium composition in the reactor. Acceleration module 2 Immersed in various liquids, the covalent bonds of these liquids break down, releasing electrons. The speed of the mixture is determined by the speed of the 2 The inlet and outlet pressures are determined by

[0207] The gas and liquid mixture is discharged into the interior space of the reactor at an acceleration of 50,000 to 150,000 g 3 and by the deceleration module 4 Slowdown. Gas molecules begin to dissociate when they come into contact with the generated moving standing pressure wave. The through flow is different due to the chemical properties of one particular gas compared to other gases. Slowdown modules act as catalysts in these reactions 4 The material capacity plays a role in the calculation of surface heating, which means that the hypersonic flow depends on the chemical properties of the moving gas. The lower limit of the mode is determined by the first component of the gas that starts to dissociate at a given stagnation temperature of the flow, which is 2000K for nitrogen. The upper limit of the mode is determined by the beginning of ionization of gas atoms in the gas flow. In this case, the number of electrons released from atoms becomes significant. The temperature of the electron gas is considered to be isolated from other gas components. This mode corresponds to gas flow velocities in the range of 10 to 12 km / s (>25 Ma), and the gas state in this case is described using a non-radiative plasma model.

[0208] Acceleration module 2The dissociation of the input gas molecules is ensured, which is confirmed by a significant pressure increase in the reactor and a decrease in the molecular weight of the gas in the reactor. For example, when the air in the reactor is ready and more air is fed in, the molecular weight in the geometric volume of the reactor drops from 28.2 to 19 g / mol, which confirms the dissociation and partial ionization of nitrogen and oxygen molecules.

[0209] Speed ​​reduction module 4 Located away from the acceleration module 2 A position not exceeding 1 m ensures maximum energy of the gas flow (gas and liquid mixture).

[0210] Speed ​​reduction module 4 At the same time, it acts as a triboelectric electrostatic voltage generator because the electrodes 4a and 4b The friction process on the electrode causes an increase in electrostatic voltage. This electrostatic voltage causes the electrode 4a and 4b The space between the electrodes decomposes and discharges. 4a and 4b Located on a metal base, ensuring that the electrodes 4a and 4b Remains motionless when impinging on gas and liquid flows. 4a and 4b Insulated from the metal base. When monitoring electrode 4a and 4b When the voltage is between 1 and 10 V, a constant voltage level of 1 to 10 V and a frequency of 0.3 to 1 Hz is recorded.

[0211] The following elements are used for electrodes 4a and 4b Suitable materials for selection: Fe, Co, Ni, Chr, Gd, W, Al, Ti and their alloys containing C, Cu, Hf, Pd, Os, Pt. Electrode 4a and 4b The distance between them ranges from 1 to 10 mm.

[0212] area 5 The volume ensures that the reduction module 4 The pressure after adjustment is used to control the pressure through the Lava nozzle 2c The flow rate of gas and liquid.

[0213] Electrode 4a and 4b The choice of material is determined by calculating the maximum surface emission of electrons and positive ions from a solid surface close to a gas. Electrons are emitted when the surface is bombarded by electrons with a kinetic energy greater than the work function of the metal. In this case, in addition to the surface rebound of the primary electrons, secondary electrons may also be emitted.

[0214] like Figure 2The acceleration module shown in can be immersed in one of the liquids in the recommended list.

[0215] The gas or mixed gas and liquid flow leaves the acceleration module at a speed of 30 to 400 m / s. The gas and liquid molecules reach the reaction space in a short time.

[0216] The data given in the examples were obtained from various tests of the process of the invention carried out in a test facility, such as Figure 1 The physics of the processes occurring in the embodiments are described in detail in the patent section entitled "Operation of the Apparatus and Physical Principles of its Functioning".

[0217] Depending on how the device is used (as described below), a gaseous mixture containing a gas or a mixture thereof is delivered to the gas inlet of the device and passes through an acceleration block with an acceleration module 2 and a catalyst, while performing the following functions:

[0218] Speed ​​reduction module 4 and tribostatic generators, such as Figure 3 The cross section of the channel is shown in Figure 1. 4a and 4b Blockage 60% to 90%. When the gas or gas and liquid mixture passes through the electrodes, it is decelerated sharply. The result is micro-explosions, shocks and electric barrier discharges in the reaction space.

[0219] When a gas or gas and liquid mixture contacts a non-thermal pulsed gliding discharge, micro-explosion, or shock zone, the atoms restructure and combine into the following types of gases and liquids, depending on the energy released:

[0220] ·Air;

[0221] ·nitrogen;

[0222] Carbon monoxide;

[0223] ·carbon dioxide;

[0224] ·oxygen;

[0225] ·hydrogen;

[0226] Hydrocarbon gases;

[0227] Inert gas;

[0228] Nitrogen oxides;

[0229] or a mixture thereof;

[0230] Vegetable oils;

[0231] Mineral oil;

[0232] ·ester;

[0233] ·diesel fuel;

[0234] ·heavy oil;

[0235] Gas oil;

[0236] ·diesel fuel;

[0237] Methyl esters (FAME);

[0238] ·paraffin;

[0239] ·gasoline;

[0240] ·alcohol;

[0241] ·water;

[0242] or a mixture thereof;

[0243] The conversion rate of gas and liquid in the reaction chamber can reach 90%, and by changing the gas compressor in the reactor inlet connected to the acceleration module 2 C1 The reaction gas, initial gas and liquid flow from the gas outlet to cooling, separation and membrane separation.

[0244] Example 1.

[0245] Methane molecules are formed from oxygen molecules.

[0246] Preparation phase. Expel the air with the target gas.

[0247] Reactor R1 With acceleration and catalysis modules, it realizes the following functions:

[0248] Speed ​​reduction module;

[0249] ·Tribostatic voltage generator.

[0250] Atmospheric air fills the internal volume of the reactor. The mass concentrations of nitrogen and oxygen in atmospheric air are 76.37% and 23.225%, respectively. The relative number ratio of nitrogen molecules to oxygen molecules is 3.288. A pressure cylinder of technical nitrogen is connected to the gas mixture inlet. 1 The nitrogen and oxygen contents in the pressure cylinder were 94.25% and 5.747%, respectively. The analysis was carried out by the laboratory of ALS Czech Republic, sro. S1 , transported from the pressure cylinder to the reactor inlet. The composition of sample 1 in the cylinder is as follows:

[0251]

[0252] The volume of gas in the reactor is 0.279m 3 The initial mass of nitrogen in the reactor is 0.2581 kg. The initial mass of oxygen in the reactor is 0.0785 kg. The overpressure is 0 Pa.

[0253] The gas with the given composition is delivered to the reactor inlet from a gas cylinder via stream S1 at a flow rate of 120 to 130 g / min. The specific energy provided by the gas stream is 25 J / cm 3 The reactor was maintained at a constant overpressure of 3447.5 Pa. The average temperature of the reactor during gas delivery was 13°C.

[0254] 494.27 g of gas were fed into the reactor and at the same time 514 g of gas were discharged through the outlet. The analysis of the gas after feeding into the facility was carried out by the laboratory of ALS Czech Republic, sro. After feeding the gas, the composition of the gas in the reactor was:

[0255]

[0256]

[0257] Theoretical calculations of the amounts of nitrogen and oxygen after the gas was transferred from the gas cylinder to the reactor initially containing air showed that, without any reaction occurring in the reactor, the mass concentrations of nitrogen and oxygen should be 93.225% and 6.775% respectively, with a relative ratio of nitrogen molecules to oxygen molecules of 13.263.

[0258] The concentrations of molecular nitrogen, methane, carbon monoxide, and hydrogen sulfide increase with the decrease of oxygen concentration in the reactor and the participation of nitrogen molecules, as follows:

[0259]

[0260] See Table 1 - Methods described in the patent application Reactions 5, 7, 13, 15 and 16 Overview of the physicochemical reactions.

[0261] Material balance:

[0262] During the process, the mass concentration of oxygen decreased by 4.48%, while the mass concentrations of methane and nitrogen increased by 4.48%.

[0263] Example 2.

[0264] Cyclic formation of nitrogen and oxygen molecules from methane

[0265] Preparation phase. Expel the air with the target gas.

[0266] Reactor R1 With acceleration module2 and catalytic modules to achieve the following functions:

[0267] Speed ​​reduction module;

[0268] ·Tribostatic voltage generator.

[0269] The reactor and separator were kept open during the test preparation phase.

[0270] Atmospheric air fills the internal volume of the reactor. The mass concentrations of nitrogen and oxygen in atmospheric air are 76.37% and 23.225%, respectively. The relative number ratio of nitrogen molecules to oxygen molecules is 3.288. The pressure cylinder (flow) containing methane NG S1 , flow rate of 110 to 130 g / min) was connected to the gas mixture inlet. The gas analysis in the facility was as follows:

[0271] parameter value Units of measurement method Evaluation results Methane 98.78 %volume ISO 6974-3.4 S oxygen 0.17 %volume ISO 6974-3.4 S nitrogen 0.62 %volume ISO 6974-3.4 S Carbon monoxide 0.00 %volume ISO 6974-3.4 S Hydrogen sulfide 0.00 %volume ISO 6974-3.4 S hydrogen 0.34 %volume ISO 6974-3.4 S C2 0.02 %volume ISO 6974-3.4 S C2＝ 0.00 %volume ISO 6974-3.4 S C3 0.03 %volume ISO 6974-3.4 S С3= 0.00 %volume ISO 6974-3.4 S С4 0.02 %volume ISO 6974-3.4 S С4= 0.00 %volume ISO 6974-3.4 S C5 0.00 %volume ISO 6974-3.4 S С5+ 0.01 %volume ISO 6974-3.4 S

[0272] Liquid adsorbent naphtha is fed into the reactor with the surface level above the acceleration module 2 .

[0273] In gas ventilators C2 With the help of the gas cycle from the three-phase separator F1, the gas is returned to the reactor R1 Entrance.

[0274] Reactor R1 The liquid sorbent in the boiler is heated to 146°C. C2 Start. From the separator F1 The gas mixture is delivered to the gas ventilator C2 and through the circulation flow S20 Return to the acceleration module 2. The gas and liquid mixture is discharged from the acceleration module at a speed of 30 to 400 m / s. 2 It is discharged into the reactor space, where it comes into contact with the catalyst, which performs the following functions:

[0275] Speed ​​reduction module;

[0276] Tribostatic voltage generators 4a, 4b;

[0277] The speed of the mixture is regulated by the amount of gas delivered to the acceleration module 2. After leaving the reaction space, the gas and liquid mixture is heated in a heat exchanger. E3 Cooling and entering the three-phase separator F1 .

[0278] In the separator F1 In the process, the gas is separated from the liquid and enters the air pump inlet. The repeated gas mixture is then C2Circulation period between the inlet and outlet. Analysis of circulating gas:

[0279] parameter value Units of measurement method Evaluation results Methane 82.19 %volume ISO 6974-3.4 S oxygen 0.94 %volume ISO 6974-3.4 S nitrogen 13.55 %volume ISO 6974-3.4 S Carbon monoxide 0.01 %volume ISO 6974-3.4 S Hydrogen sulfide 0.00 %volume ISO 6974-3.4 S hydrogen 2.17 %volume ISO 6974-3.4 S C2 0.21 %volume ISO 6974-3.4 S C2＝ 0.03 %volume ISO 6974-3.4 S C3 0.29 %volume ISO 6974-3.4 S С3= 0.01 %volume ISO 6974-3.4 S С4 0.29 %volume ISO 6974-3.4 S С4= 0.00 %volume ISO 6974-3.4 S C5 0.13 %volume ISO 6974-3.4 S С5+ 0.18 %volume ISO 6974-3.4 S

[0280] From the equilibrium analysis of input materials and reaction products, the following conclusions can be drawn:

[0281] The concentrations of molecular nitrogen and oxygen increase as the methane concentration decreases:

[0282] parameter Units of measurement Process Start End of process Difference in process results Relative percentage difference in mass Methane kg 0.707 0.589 -0.118 -16.690 oxygen kg 0.002 0.013 0.011 550.000 nitrogen kg 0.008 0.169 0.161 2012.500 Carbon monoxide kg 0.000 0.000 0.000 - Hydrogen sulfide kg 0.000 0.000 0.000 - hydrogen kg 0.000 0.002 0.002 - C2 kg 0.000 0.003 0.003 - C2＝ kg 0.000 0.000 0.000 - C3 kg 0.001 0.006 0.005 500.000 С3= kg 0.000 0.000 0.000 - С4 kg 0.001 0.008 0.007 700.000 С4= kg 0.000 0.000 0.000 - C5 kg 0.000 0.004 0.004 - С5+ kg 0.000 0.007 0.007 - total kg 0.720 0.801 0.081

[0284] ·Compared with the patented method Reactions 20, 21, 22, and 23 , with a total excess of 11.3%; see Table 1 - Overview of the physicochemical reactions.

[0285] Example 3

[0286] A hydrocarbon liquid is formed from the air during part of the cycle.

[0287] Reactor R1 With acceleration module 2 and catalytic modules to achieve the following functions:

[0288] Speed ​​reduction module 4 ;

[0289] • Frictional electrostatic voltage generators 4a, 4b.

[0290] Reactor R1 The internal volume is 0.136m 3 . Separator F1 is open. There is no condenser in the separator. The initial temperature in the reactor is 10°C. The final temperature is 102°C.

[0291] The device for measuring the flow rate of incoming and outgoing gas has an accuracy class of 0.25. The amount of gas passing through the flow meter is checked by reweighing the gas cylinder on a digital scale. The relative error of the flow measurement is 0.25%.

[0292] Gas ventilator C2 Air is extracted from the upper part of the separator, which is connected to the atmosphere and sent to the inlet of reactor R1 and then to the acceleration module. R1 After that, the product is heated by water heat exchanger E3 Cooling, the liquid phase of the product in the three-phase separator F1 Part of the gas is condensed in the separator in the form of mist. F1 Enter the ventilator C2 , and condenses in the pressure tube.

[0293] Process preparation parameters:

[0294] 1. Input materials: air and air vapor and synthetic organic liquids.

[0295] 2. Reactor internal volume: 0.136m 3 .

[0296] 3. Ventilator C2 Pressure at inlet: 0 kPa.

[0297] 4. Overpressure in the reactor: 55 to 58 kPa.

[0298] 5. C2 Gas flow rate: (38 to 40m3 / h).

[0299] 6. Catalytic space volume: 0.0129m 3 .

[0300] 7. Air flow velocity in front of the catalytic plate: 330m / s.

[0301] 8. Gas ventilator C2 Current power consumption: 3.04kW / h.

[0302] 9. Gas ventilator C2 The motor efficiency is 0.6.

[0303] 10. Gas ventilator C2 The efficiency is 0.85.

[0304] 11. Gas ventilator C2 The current energy on the shaft is 1.55 kW / h.

[0305] 12. During the process, gas ventilator C2 Total power consumed: 17.94kW / h.

[0306] 13. Process gas ventilator C2 Total energy on the shaft: 9.145kW / h.

[0307] 14. In heating mode E3 The temperature of the liquid in the circuit varies between 14 and 17 degrees Celsius.

[0308] 15. Cooling mode E3 The temperature of the liquid in the circuit varies between 17 and 14 degrees Celsius.

[0309] 16. Cooling circuit E3 Heat capacity of coolant: 3.8kJ×C -1 .

[0310] 17. Cooling circuit E3 The mass of the coolant: 115kg.

[0311] 18. Cooler E3 Coolant temperature at inlet: 14 to 18 degrees Celsius.

[0312] 19. Water Cooler E3 Coolant temperature at outlet: 14 to 18 degrees Celsius.

[0313] 20. By the water cooler E3 Coolant flow rate: 3,500kg / h.

[0314] 21. Assign to water cooler E3 The actual value of thermal energy is: 5.76kW / h.

[0315] 22. Assign to water cooler E3 Total heat energy: 33.98kW / h.

[0316] 23. The mass of the product obtained is 100 g.

[0317] 24. The density of the product is 858 kg / m at 25 °C. 3 ; Kinematic viscosity at 40°C is 13.2 mm 2 / s.

[0318] 25. Product freezing point: -11.2℃.

[0319] 26. Physical energy efficiency - the ratio of the heat energy released after the process to the total energy consumed (heat energy, mechanical energy), considering energy efficiency: 3.71. Energy balance of the process:

[0320]

[0321] Analyzing the balance of input materials and reaction products, the following conclusions can be drawn:

[0322] The synthesis of hydrocarbon products is caused by:

[0323] 1. By decomposing nitrogen and oxygen molecules, then synthesizing these molecules and releasing excess energy.

[0324] 2. If there is enough excess energy when the air molecules are decomposed in the catalytic zone, the air->water reaction will begin. Reaction 1 , releasing 12.2MJ / kg of air energy.

[0325] 3. If Reaction 1 During this period, if there is enough excess energy in the catalytic zone, the air->methane reaction in the water and air environment will begin. Reaction 2 , releasing 24.7MJ / kg of air energy.

[0326] 4. If Reaction 2 During this period, if the catalytic zone has enough energy, methane will be directly converted into ordinary alkanes and hydrogen. Reaction 3 .

[0327] 5. If there is enough methane at a specific point in the catalytic space at a specific time, a reaction will occur, releasing 150.7 kJ / mol of energy, and then possible synthesis of ordinary alkanes: n = 1 + E se / 9;E se = kcal / mol; therefore n = 1 + (150,7 / 4,166) / 9; n = 5, so according to the synthesis of ordinary alkanes with a given hydrocarbon chain length, 1 mole of pentane C is formed from 5 moles of methane 5 H 12 and 4 moles of hydrogen.

[0328] 6. At a lower level and with insufficient energy, it is also possible to synthesize alkanes first and then ethers in the presence of oxygen, or to synthesize alcohols from alkanes.

[0329] 7. If the formula С m Η 2m+2 Hydrocarbons in gas ventilators C2 The pressure pipe gradually accumulates. After a certain period of time, part of the circulating gas will enter the acceleration module, making the reaction block Reaction 4 become possible.

[0330] Due to the reduction of nitrogen and oxygen concentrations and Reactions 15, 16, 24 and 25 , the concentration of molecular methane also increases.

[0331] See Table 1 - Overview of the physicochemical reactions for all reaction details.

[0332] Example 4

[0333] Methane is converted to hydrocarbons.

[0334] The reactor is equipped with an acceleration module and a catalytic module to achieve the following functions:

[0335] ·Deceleration module 4;

[0336] Frictional electrostatic voltage generator 4a , 4b .

[0337] No circulation used. Preparation phase. Exhaust air with target gas.

[0338] Atmospheric air fills the internal volume of the reactor. The mass concentrations of nitrogen and oxygen in atmospheric air are 76.37% and 23.225% respectively. The relative number ratio of nitrogen molecules to oxygen molecules is 3.288. A pressure cylinder containing methane NG (stream S1) is connected to the gas mixture inlet.

[0339] Process preparation parameters:

[0340] 1.Atmospheric pressure: 97,990Pa.

[0341] 2. After the device is closed, at the given atmospheric pressure, there are 325 g of air with a molecular weight of 28.98 g / mol, including 248 g of nitrogen (76.3% by mass) and 75 g of oxygen (23.07% by mass).

[0342] 3. The first delivery of methane from the gas cylinder is 22.57 g. The flow rate of the supplied gas is S1 The speed is 0.7m 3 / h; the overpressure in the equipment after gas delivery is 12.41 kPa. The average temperature in the equipment during methane delivery is 15°C. Methane delivery takes 2.53 minutes.

[0343] 4. First output of reaction gas: Open the valve that releases the gas out of the reactor until the overpressure value is 0 kPa. Draw 20.53 grams of gas. When the gas leaves, the average temperature in the facility is 15°C.

[0344] 5. 2.7 grams of liquid phase were discharged from the reactor. They were captured in a test tube and numbered 1. The product density was 794.12 kg / m at 22.8 °C. 3 .

[0345] 6. The second time, 23.23 g of methane was delivered from the gas cylinder. S1 The speed is 0.7m 3 / h; the overpressure in the equipment after gas delivery is 13.79 kPa. The average temperature in the equipment during methane delivery is 15.5°C. The methane delivery time is 2.61 minutes.

[0346] 7. Second output of reaction gas: Open the valve that releases the gas out of the reactor until the overpressure value is 0 kPa. 21.393 grams of gas are extracted. When the gas leaves, the average temperature in the facility is 16°C.

[0347] 8. 2.726 grams of liquid phase were discharged from the reactor. They were captured in a test tube and numbered 2. The product density was 801.76 kg / m at 22.8°C. 3 .

[0348] 9. The third time, 46.15 g of methane was delivered from the gas cylinder. S1 The speed is 0.7m 3 / h; the overpressure in the equipment after gas delivery is 26.2kPa. The average temperature in the equipment during methane delivery is 16.5℃. The methane delivery time is 5.18 minutes.

[0349] 10. 3rd output of reaction gas: Open the valve that releases the gas out of the reactor until the overpressure value is 12.62 kPa. 41.99 grams of gas are extracted. When the gas leaves, the average temperature in the facility is 16.5°C.

[0350] 11. 2.908 g of liquid phase was discharged from the reactor. It was captured in a test tube and numbered 3. The product density was 785.95 kg / m at 22.8 °C. 3 .

[0351] 12. The fourth time, 22.55 g of methane is delivered from the gas cylinder. The flow rate of the supplied gas is S1 The speed is 0.7m 3 / h; the overpressure in the equipment after gas delivery is 26.41 kPa. The average temperature in the equipment during methane delivery is 17°C. The methane delivery time is 2.53 minutes.

[0352] 13. Fourth output of reaction gas: Open the valve that releases the gas out of the reactor until the overpressure value is 11.86 kPa. 20.52 grams of gas are extracted. When the gas leaves, the average temperature in the facility is 17°C.

[0353] 14.2.068 grams of liquid phase were discharged from the reactor. They were captured in a test tube and numbered 4. The product density was 795.38 kg / m at 22.8 °C. 3 .

[0354] 15. The fifth time methane is delivered from the gas cylinder, the amount is 48.13 g. The flow rate of the supplied gas is S1 The speed is 0.7m 3 / h; the overpressure in the equipment after gas delivery is 39.99 kPa. The average temperature in the equipment during methane delivery is 17.5°C. Methane delivery takes 5.4 minutes.

[0355] 16. Fifth output of reaction gas: Open the valve that releases the gas out of the reactor until the overpressure value is 25.09 kPa. 43.80 grams of gas are extracted. When the gas leaves, the average temperature in the facility is 17.5°C.

[0356] 17.1.358 grams of liquid phase was discharged from the reactor. It was captured in a test tube and numbered 5. The product density was 754.44 kg / m at 22.8 °C. 3 .

[0357] 18. The sixth delivery of methane from the gas cylinder is 17.5 g. The flow rate of the supplied gas is S1 The speed is 0.7m 3 / h; after the gas is input, the overpressure in the equipment is 40.68 kPa. The average temperature in the equipment during methane transportation is 18°C. Methane transportation takes 1.97 minutes.

[0358] 19. 6th output of reaction gas: Open the valve that releases the gas out of the reactor until the overpressure value is 21.37 kPa. 15.93 grams of gas are extracted. When the gas leaves, the average temperature in the facility is 18°C.

[0359] 20.0.855 g of liquid phase was discharged from the reactor. It was captured in a test tube and numbered 6. The product density was 777.27 kg / m at 22.8 °C. 3 .

[0360] 21. The seventh delivery of methane from the gas cylinder is 60.12 g. The flow rate of the supplied gas is S1 The speed is 0.7m 3 / h; the overpressure in the equipment after gas input is 55.44 kPa. The average temperature in the equipment during methane delivery is 18.7°C. Methane delivery takes 6.75 minutes.

[0361] 22. 7th output of reaction gas: Open the valve that releases the gas out of the reactor until the overpressure value is 24.82 kPa. 54.71 grams of gas are extracted. When the gas leaves, the average temperature in the facility is 18.7°C.

[0362] 23.0.985 grams of liquid phase were discharged from the reactor. They were captured in a test tube and numbered 7. The product density was 757.69 kg / m at 22.8 °C. 3 .

[0363] 24. The 8th delivery of methane from the gas cylinder is 79.7 g. The flow rate of the supplied gas is S1 The speed is 0.7m 3 / h; the overpressure in the equipment after gas input is 68.95 kPa. The average temperature in the equipment during methane transportation is 19°C. Methane transportation takes 8.96 minutes.

[0364] 25. 8th output of reaction gas: Open the valve that releases the gas out of the reactor until the overpressure value is 0 kPa. 72.53 grams of gas are discharged. When the gas leaves, the average temperature in the facility is 19°C.

[0365] 26.0.893 grams of liquid phase were discharged from the reactor. They were captured in a test tube and numbered 8. The product density was 744.17 kg / m at 22.8 °C. 3 .

[0366] 27. The 9th delivery of methane from the gas cylinder is 21.55 g. The flow rate of the supplied gas is S1 The speed is 0.7m 3 / h; after the gas is input, the overpressure in the equipment is 12.41 kPa. The average temperature in the equipment during methane transportation is 19.2°C. Methane transportation takes 2.42 minutes.

[0367] 28. 9th output of reaction gas: Open the valve that releases the gas out of the reactor until the overpressure value is 0 kPa. 19.61 grams of gas are extracted. When the gas leaves, the average temperature in the facility is 19.2°C.

[0368] 29. 0.196 g of liquid phase was discharged from the reactor. It was captured in a test tube and numbered 9. The product density was 753.85 kg / m at 22.8 °C. 3 .

[0369] Figure 1 The density of the resulting product is shown in relation to the movement time of the gas from the acceleration module to the deceleration module and the tribostatic generator.

[0370] The following table gives the results of sample number, gas delivery time, density of obtained products and number of obtained products:

[0371] Sample No. 1 2 3 4 5 6 7 8 9 Gas delivery time, minutes 2.53 2.61 5.18 2.53 5.4 1.97 6.75 8.96 2.42 <![CDATA[Product density, kg / m 3 > 794.12 801.76 785.95 795.38 754.44 777.27 757.69 744.17 753.85 The mass of the product obtained, g 2.7 2.726 2.908 2.068 1.358 0.855 0.985 0.893 0.196

[0372] Figure 2 The relationship between the mass of the obtained product and the movement time of the gas from the acceleration module to the deceleration module and the tribostatic generator is shown:

[0373] Figure 3 The relationship between the quality of the obtained product and the physicochemical properties of the gas from the acceleration module to the deceleration module and the tribostatic generator is shown:

[0374] Figure 4 The relationship between the density of the obtained product and the physical and chemical properties of the gas from the acceleration module to the deceleration module and the tribostatic generator is shown:

[0375] The following conclusions can be drawn from the analysis of Example 4 and the liquid product:

[0376] The chronological synthesis of hydrocarbon products is caused by:

[0377] 1. By breaking down nitrogen and oxygen molecules, and then synthesizing them and releasing excess energy.

[0378] 2. If there is enough excess energy in the catalytic zone during the decomposition of air molecules, the air->methane reaction 16 will begin, releasing 24.7 MJ per kg of air.

[0379] 3. The higher the concentration of nitrogen and oxygen in the reactor, the more energy is generated and the higher the density of the liquid generated. reaction 24 .

[0380] Due to the reduced concentration of nitrogen and oxygen after the equipment is depressurized, and the processes described in reactions 5, 7, 13, 14, 15, 16 and 17 and Reaction 24After the process of forming normal alkanes from methane, the concentration of molecular nitrogen and the energy obtained increase. These processes are covered by this pending patent.

[0381] See Table 1 - Overview of the physicochemical reactions for all reaction details.

[0382] Example 5

[0383] In the cycle, methane is converted into hydrocarbons

[0384] The reactor is equipped with an acceleration module and a catalytic module to achieve the following functions:

[0385] Speed ​​reduction module;

[0386] ·Tribostatic voltage generator.

[0387] Preparation phase. Expel the air with the target gas.

[0388] Atmospheric air fills the internal volume of the reactor. The mass concentrations of nitrogen and oxygen in the atmospheric air are 76.37% and 23.225%, respectively. The relative number ratio of nitrogen molecules to oxygen molecules is 3.288. A pressure cylinder containing methane NG is connected to the gas mixture inlet.

[0389] 1.Atmospheric pressure: 97,990Pa.

[0390] 2. After the device is closed, at the given atmospheric pressure, there are 325 g of air with a molecular weight of 28.98 g / mol, including 248 g of nitrogen (76.3% by mass) and 75 g of oxygen (23.07% by mass).

[0391] 3. The first delivery of methane from the gas cylinder is 134.3 g. The flow rate of the supplied gas is S1 The speed is 0.7m 3 / h; the overpressure in the equipment after gas delivery is 68.95kPa. The average temperature in the equipment when transporting methane is -2℃.

[0392] 4. First output of reaction gas: Open the valve that releases the gas out of the reactor until the overpressure value is 0 kPa. 90.69 grams of gas are extracted. When the gas leaves, the average temperature in the equipment is -2°C.

[0393] 5. The second time, 124.5 g of methane is delivered from the gas cylinder. S1 The speed is 0.7m 3 / h; the overpressure in the equipment after gas delivery is 68.95kPa. The average temperature in the equipment when transporting methane is -1.5℃.

[0394] 6. Second output of reaction gas: Open the valve that releases the gas out of the reactor until the overpressure value is 6.895 kPa. 132.42 grams of gas are extracted. When the gas leaves, the average temperature in the equipment is -1.6°C.

[0395] 7. The third time, 35.7 g of methane was delivered from the gas cylinder. S1 The speed is 0.7m 3 / h; the overpressure in the equipment after gas delivery is 26.20kPa. The average temperature in the equipment when transporting methane is -1℃.

[0396] 8. The fourth delivery of methane from the gas cylinder is 34.1 grams. The flow rate of the supplied gas is S1 The speed is 0.7m 3 / h; the overpressure in the equipment after gas delivery is 48.06kPa. The average temperature in the equipment when delivering methane is -1℃. The gas concentration in the equipment: nitrogen by mass 36.41%; oxygen by mass 11.07%; methane by mass 52.52%.

[0397] 9. Start heating of the reactor gas space.

[0398] In gas ventilators C2 With the help of F1 The gas is circulated to transport the gas back to the reactor.

[0399] 10. Turn on the gas ventilator C2 The temperature in the reactor was 87.5°C, and 27 g of methane was delivered from the gas cylinder; the flow rate of the gas was S1 The speed is 0.7m 3 / h; after the gas is delivered, the overpressure in the reactor is 68.95 kPa.

[0400] 11. The reactor was operated for 1 hour and 25 minutes. Gas ventilator C2 The initial power consumption was 2.02 kW / h; the final power consumption was 1.87 kW / h. The temperature in the reactor: initial 87.5°C, final 79.19°C. Overpressure 65.019 kPa. Gas fan performance: initial 130.07 m 3 / h, final 115.68m 3 / h.

[0401] 12. At a temperature of 15°C, the density of 160 g is 836.7 kg / m 3 product of.

[0402] Product analysis.

[0403] Gas chromatography analysis was performed and selected parameters were assigned to the diesel supply sample marked “13.12.2017”; Example 5.

[0404] Gas chromatography analysis showed that the sample was diesel with a typical distribution of hydrocarbons, containing 2.5% FAME (biocomponents). The complete results of the standard distillation test (CSN EN ISO 3405) are shown in the form of a distillation curve. Figure 5 middle.

[0405] Gas chromatography is used to determine the distribution of various hydrocarbon groups by carbon atom number, e.g. Figure 6 As shown in:

[0406] The cumulative values ​​for the same determinations are given in the following table:

[0407]

[0408]

[0409] The table below shows the results of the determination of other physicochemical characteristics of the analyzed samples, as well as the requirements for diesel fuel in accordance with the EU standard EN 590. The results show that the sample "13.12.2017" does not comply with the EN 590 standard only in terms of sulfur content. If we ignore this deficiency, the analyzed fuel can be used in the Czech Republic only as diesel fuel of class B (from 15.4. to 30.9. in the summer period) and diesel fuel of class D (from 1.10. to 15.11. and from 1.3. to 14.4. in the transition period), but not as winter diesel fuel of class F (from 16.11. to 29.2.).

[0410] parameter Sample GGGTL 13.12.2017 EN 590 Requirements Density at 15℃ 836,7 820-845 Kinematic viscosity at 40℃ 3,15 2,00-4,5o Distillate recovered at 250°C (volume %) 25,0 Max 65 Distillate recovered at 350°C (volume %) 95,0 Minimum 85 95% volume recovery at (℃) temperature 250 Max 360 Cetane Index 55,7 Minimum 46 Flash point-PM(℃) 69,5 Minimum 55 Monoaromatic content (% by mass) 13,5 - Polyaromatic hydrocarbon content (% by mass) 1,8 Max 8 Total aromatics content (% by mass) 15,3 - FAME content (volume %) 2,4 Max 7 <![CDATA[Sulfur content, mg·kg -1 > 14 Max 10 Filterability-CFPP(℃) -12 Max. 0 / -10 / -20

[0411] The following conclusions can be drawn from the analysis of Example 5 and the reaction product:

[0412] The synthesis of the hydrocarbon product diesel is caused by:

[0413] 1. By decomposing nitrogen and oxygen molecules, then synthesizing these molecules and releasing excess energy.

[0414] 2. If there is enough excess energy in the catalytic zone during the decomposition of air molecules, the air->methane reaction 16 will begin, releasing 24.7 MJ per kg of air.

[0415] 3. The higher the concentration of nitrogen and oxygen in the reactor, the more energy is produced and the greater the density of the liquid produced by reaction 24.

[0416] 4. The presence of methyl esters (FAME) in the products is explained by the recombination of free radicals generated in the plasma with oxygen-containing chemicals.

[0417] Due to the decrease in the concentration of nitrogen and oxygen present after the decompression of the equipment, and the processes described in reactions 5, 7, 13, 14, 15 and 16, the concentration of methane molecules and the energy produced increase. The main synthesis of hydrocarbons is based on React 24 from methane. These processes are within the scope of this patent pending application.

[0418] See Table 1 - Overview of the physicochemical reactions for all reaction details.

[0419] Example 6

[0420] In the circulation process the methyl esters are converted into hydrocarbons.

[0421] Reactor R1 With acceleration module and catalysis module, it can realize the following functions:

[0422] ·Deceleration module 4;

[0423] · Tribostatic voltage generator 4.

[0424] During the test preparation stage, the reactor R1 and separator F1 It is open.

[0425] Preparation phase. Exhaust the air with the target gas.

[0426] Atmospheric air fills the internal volume of the reactor. The mass concentrations of nitrogen and oxygen in atmospheric air are 76.37% and 23.225% respectively. The relative number ratio of nitrogen molecules to oxygen molecules is 3.288. S1 ) is connected to the gas mixture inlet. The gas is delivered from the gas cylinder to the inlet at a flow rate of 110 to 130 g / m until the maximum methane concentration is reached. Analysis of the gas in the reactor:

[0427] gas value Units of measurement method Evaluation results Methane 92,40 %volume ISO 6947-3.4 S oxygen 1,772 %volume ISO 6947-3.4 S nitrogen 5,827 %volume ISO 6947-3.4 S

[0428] Liquid adsorbent methyl esters (FAME) are delivered to the reactor R1 In the case of the accelerator module R1, the surface level is higher than in the accelerator module R1. The incoming FAME liquid does not contain hydrocarbon fuel fractions.

[0429] In gas ventilators C2 With the help of F1 The gas is circulated and sent back to the reactor.

[0430] The liquid adsorbent in the boiler of reactor R1 is heated to 200°C. Gas ventilator C2Start. The gas mixture is sent back to the reactor inlet and the acceleration module. The gas and liquid mixture enters the reactor space from the acceleration module at a speed of 200 to 400 m / s, where it comes into contact with the catalytic space, which performs the following functions:

[0431] ·Deceleration module 4;

[0432] Frictional electrostatic voltage generator 4a , 4b .

[0433] After leaving the reaction space, the gas and liquid mixture is cooled in a water cooler. E3 Cooling and then entering the separator F1 In the separator, the gas is separated from the liquid and enters the gas pump C2 Repeat the gas mixture in the gas ventilator C2 The cycle is a cycle between the inlet and outlet of the unit. The condensation of the resulting liquid reduces the volume of gas in the internal volume of the unit, which causes a pressure drop in the unit, but the formation of molecular hydrogen compensates for the pressure drop and the cycle causes a constant change in the gas composition. The removal of molecular hydrogen from the circulating gas causes a pressure drop in the device and allows the input of "fresh" gas.

[0434] Analytical Reactor R1 Boilers and separators F1 The product of .

[0435] Gas chromatography analysis and density and viscosity measurements were performed on two samples of fatty acid methyl esters.

[0436] The results of gas chromatography showed that both samples were fatty acid methyl esters (FAME). In addition to FAME, the samples contained a small amount of intermediate fractions. The chromatogram was a typical diesel chromatogram (e.g. Chart 7 ).

[0437] The main difference between the samples analyzed is the diesel content, the chromatographic curves are completely comparable. The calculated contents of the two samples are listed in the table below.

[0438]

[0439] The compositions shown in the table above correspond to the density and viscosity of the samples:

[0440]

[0441] Sample 1441 (FAME) has a higher diesel content (diesel has a lower density than FAME) and lower average density and viscosity values ​​than sample 1440 (FAME), which has a lower diesel content. The higher diesel content in sample 1441 (FAME) is reflected in the calculation of the hydrocarbon content:

[0442]

[0443] By analyzing Example 6 and the liquid product, the following conclusions can be drawn:

[0444] The synthesis of hydrocarbon products -> diesel is caused by:

[0445] 1. By decomposing nitrogen and oxygen molecules, then synthesizing these molecules and releasing excess energy.

[0446] 2. If there is enough excess energy in the catalytic zone during the decomposition of air molecules, the air will start -> The reaction of methane 5, 7, 13, 14, 15 and 16 , 24.7MJ is released per kg of air.

[0447] 3. The higher the concentration of nitrogen and oxygen in the reactor, the more energy is generated and the higher the density of the liquid produced. opposite Should 24 .

[0448] 4. Synthesis of oxygenated chemicals by decomposition of methyl ester (FAME) molecules and subsequent recombination of free radicals generated in the plasma. The low concentrations of nitrogen and oxygen in the input gas determine the low product yields.

[0449] The increase in molecular methane concentration and energy production is due to the decrease in nitrogen and oxygen concentrations and Reactions 5, 7, 13, 14, 15, and 16 As a result of the process, methyl esters are converted into hydrocarbons due to the energy generated. These processes fall within the scope of the present patent application.

[0450] See Table 1 - Overview of the physicochemical reactions for all reaction details.

[0451] Example 7

[0452] In the course of the cycle, normal alkanes are formed from the vegetable oils.

[0453] Reactor R1 With acceleration module and catalysis module, it can realize the following functions:

[0454] Speed ​​reduction module 4 ;

[0455] Frictional electrostatic voltage generator 4a , 4b ;

[0456] Preparation phase. Expel the air with the target gas.

[0457] Atmospheric air fills the internal volume of the reactor. The mass concentrations of nitrogen and oxygen in atmospheric air are 76.37% and 23.225% respectively. The relative number ratio of nitrogen molecules to oxygen molecules is 3.288.S1 ) is connected to the inlet of the input gas mixture. The gas is delivered from the gas cylinder to the inlet at a flow rate of 110 to 130 g / m until the maximum methane concentration is reached. After the gas is delivered, the gas in the reactor is analyzed:

[0458] gas value Units of measurement method Evaluation results Methane 93,40 %volume ISO 6947-3.4 S oxygen 2,170 %volume ISO 6947-3.4 S nitrogen 4,427 %volume ISO 6947-3.4 S

[0459] In gas ventilators C2 With the help of F1 Gas circulation, transporting gas back to the reactor R1 middle.

[0460] Liquid adsorbent rapeseed oil is delivered to the reactor with the surface level above the acceleration module R1 The rapeseed oil contains no hydrocarbon fuel fractions and no methyl esters. The liquid adsorbent in the reactor boiler is heated to 146°C. The gas ventilator is started. The gas mixture is discharged from the ventilator. C2 Enter the reactor inlet and the acceleration module. The gas and liquid mixture enters the reactor space from the acceleration module at a speed of 200 to 400 m / s, where it contacts the catalytic space, which realizes the following functions:

[0461] Speed ​​reduction module 4 ;

[0462] Frictional electrostatic voltage generator 4a , 4b ;

[0463] After leaving the reaction space, the gas and liquid mixture is cooled in a water cooler. E3 Cooling and then entering the separator F1 In the separator, the gas is separated from the liquid and enters the gas pump C2 Repeat the cycle.

[0464]

[0465] Analytical Reactor R1 Product and three-phase separator in boiler F1 Two product samples in.

[0466] The density and viscosity of three fuel samples were determined. The composition of these samples was analyzed by gas chromatography.

[0467] The results of gas chromatography analysis showed that sample 26920163 was pure vegetable oil.

[0468] Samples 26920162 and 29920161 contain trace amounts of vegetable oil (up to 2% by mass). The main components of these two samples are FAME and middle distillates:

[0469] The main difference between samples 26920162 and 29920161 is their FAME, diesel and vegetable oil content ratios. The diesel chromatogram readings for both samples are comparable. Density and viscosity results are Figure 8 Shown in.

[0470] Composition of analyzed samples:

[0471]

[0472] Hydrocarbon chain content calculated by carbon chain number (cumulative)

[0473]

[0474] The analysis of Example 7 and the liquid product leads to the following conclusions:

[0475] The synthesis of hydrocarbon products -> diesel is caused by:

[0476] 1. By decomposing nitrogen and oxygen molecules, then synthesizing these molecules and releasing excess energy.

[0477] 2. If there is enough excess energy in the catalyst zone during the decomposition of air molecules, air->methane will occur opposite 5, 7, 13, 14, 15 and 16 , 24.7MJ is released per kg of air.

[0478] 3. The higher the concentration of nitrogen and oxygen in the reactor, the more energy is generated, and Reaction 24 The greater the density of the liquid produced from methane.

[0479] 4. The triglyceride molecules in the vegetable oil molecules are decomposed, and then the free radicals generated in the plasma are recombined through the synthesis of oxygen-containing chemicals and diesel fractions. The low concentration of nitrogen and oxygen in the input gas determines the low product yield.

[0480] 5. In this example, it can be assumed that methane is converted into nitrogen and oxygen molecules as an additional source for the synthesis of oxygen-containing components.

[0481] 6. The absence of glycerol in the analysis results indicates that glycerol as a compound has been destroyed and other elements can be synthesized from the glycerol fragments.

[0482] Due to the reduction of nitrogen and oxygen concentrations and Reactions 5, 7, 13, 14, 15, 16 and 17 By the process described in the invention, the molecular methane concentration and the energy produced increase. As a result of the energy produced, the bonds in the triglyceride molecules are broken and hydrocarbons are subsequently synthesized. These processes fall within the scope of the present patent being applied for.

[0483] See Table 1 - Overview of the physicochemical reactions for all reaction details.

[0484] Example 8

[0485] In the course of the cycle, normal alkanes are formed from the vegetable oils.

[0486] Reactor R1 With acceleration module and catalysis module, it can realize the following functions:

[0487] Speed ​​reduction module 4 ;

[0488] Frictional electrostatic voltage generator 4a , 4b .

[0489] Preparation phase. Expel the air with the target gas.

[0490] gas value Units of measurement method Evaluation results Methane 0.00 %volume ISO 6974-3.4 S oxygen 9.22 %volume ISO 6974-3.4 S nitrogen 90.78 %volume ISO 6974-3.4 S

[0491] Atmospheric air fills the internal volume of the reactor. The mass concentrations of nitrogen and oxygen in the atmospheric air are 76.37% and 23.225%, respectively. The relative number ratio of nitrogen molecules to oxygen molecules is 3.288. A pressure cylinder of nitrogen gas NG (stream S1) is connected to the gas mixture inlet. The gas is delivered from the gas cylinder to the inlet at a flow rate of 110 to 130 g / m until the maximum nitrogen concentration is reached. After the gas is delivered, the gas in the reactor is analyzed:

[0492] Liquid adsorbent rapeseed oil is fed into the reactor at a surface level above the acceleration module. The rapeseed oil does not contain hydrocarbon fuel fractions and methyl esters.

[0493] At the pump C2 With the help of F1 Gas circulation, transporting gas back to the reactor R1 middle.

[0494] The liquid sorbent in the reactor boiler is heated to 250°C. Gas ventilator C2 Start. The gas mixture is pumped from the pump C2 Return to the reactor inlet and the acceleration module. The gas and liquid mixture enters the reactor space from the acceleration module at a speed of 200 to 400 m / s, where it comes into contact with the catalytic space, which performs the following functions:

[0495] Speed ​​reduction module;

[0496] ·Tribostatic voltage generator.

[0497] After leaving the reaction space, the gas and liquid mixture is cooled in a water cooler. E3 Cooled and enters the separator F1 In the separator, the gas is separated from the liquid and enters the gas pump C2 Repeat the cycle.

[0498] Analyze the input material and the F1 product of.

[0499] Gas chromatography was performed on two organic liquid samples. Both liquids were first analyzed using high temperature gas chromatography (HTGC). After determining the nature of the components present, the sample labeled "N1, 20.4.2018" was determined to be pure rapeseed oil, while the sample labeled "N2, 20.4.2018" was analyzed using a further chromatography method with better separation.

[0500] The analysis showed that sample "N1, 20.4.2018" was pure rapeseed oil formed by a mixture of triglycerides of fatty acids. In contrast, the sample labeled "N2, 20.4.2018" was an almost pure hydrocarbon mixture, containing only 2.1% vegetable oil by mass (such as Figure 9 ).

[0501] A more detailed chromatographic analysis of sample "N2, 20.4.2018" revealed that the distribution of hydrocarbons in this sample is typical of middle distillates. In terms of the representativeness of n-alkanes and the overall distribution of hydrocarbons, sample "N2, 20.4.2018" can be fully compared with diesel or possibly gasoline. Chart 10 as shown in .

[0502] The distribution of hydrocarbons in sample "N2, 20.4.2018" is Chart 11 It shows:

[0503] The table shows the distribution of hydrocarbons, expressing the cumulative content of hydrocarbon groups by the number of carbon atoms in the molecule.

[0504]

[0505]

[0506] The following conclusions can be drawn from the analysis of Example 8 and the liquid reaction product:

[0507] The synthesis of hydrocarbon products -> diesel is caused by:

[0508] 1. By decomposing nitrogen and oxygen molecules, then synthesizing these molecules and releasing excess energy.

[0509] 2. If there is enough excess energy in the catalyst zone during the decomposition of air molecules, air->methane will begin opposite 5, 7, 13, 14, 15, 16 and 17 , 24.7MJ is released per kg of air.

[0510] 3. The higher the concentration of nitrogen and oxygen in the reactor, the more energy is generated. Reaction 3The liquid produced from methane is denser.

[0511] 4. In this example, there is no methane in the input gas. Methane and ordinary alkanes can be synthesized:

[0512] ·according to Reactions 5, 7, 13, 14, 15, 16 and 17 , synthesizing methane from nitrogen and oxygen, and then according to Reaction 24 Synthesis of common alkanes; or

[0513] ·Synthesize common alkanes by decomposing triglycerides in vegetable oil molecules and recombining free radicals generated in plasma.

[0514] 5. The absence of glycerol in the analysis results indicates that it has been destroyed as a compound and other elements have been synthesized from its fragments.

[0515] The increase in methane molecular concentration and energy production is due to the decrease in nitrogen and oxygen concentrations and Reactions 5, 7, 13, 14, 15, 16 and 17 The results of the process described in . Due to the energy generated, the breaking of the bonds in the triglyceride molecules and the subsequent synthesis of hydrocarbons occur. These processes fall within the scope of the present patent being applied for.

[0516] See Table 1 - Overview of the physicochemical reactions for all reaction details.

[0517] Example 9

[0518] Formation of organic synthesis products from vegetable oils in a nitrogen-containing environment.

[0519] Reactor R1 With acceleration module and catalysis module, it can realize the following functions:

[0520] Speed ​​reduction module 4 ;

[0521] Frictional electrostatic voltage generator 4a , 4b ;

[0522] Preparation phase. Exhaust the air with the target gas.

[0523] Atmospheric air fills the internal volume of the reactor. The mass concentrations of nitrogen and oxygen in atmospheric air are 76.37% and 23.225%, respectively. The relative number ratio of nitrogen molecules to oxygen molecules is 3.288. The pressure cylinder (flow S1 )Connect the gas mixture inlet.

[0524] No gas circulation is used, which conveys the gas from the separator F1 back into the reactor with the aid of the gas ventilator C2.

[0525] 1.Atmospheric pressure: 97,990Pa.

[0526] 2. After the device is closed, at the given atmospheric pressure, there are 325 grams of air with a molecular mass of 28.98 g / mol, including 248 grams of nitrogen (76.3% by mass) and 75 grams of oxygen (23.07% by mass).

[0527] 3. The first nitrogen is delivered from the gas cylinder, the amount is 11.33g. The flow rate of the supplied gas is S1 The rate is 0.7m3 / h; the overpressure in the equipment after gas delivery is 3.48kPa. The average temperature in the equipment during gas delivery is 22℃.

[0528] 4. First output of reaction gas: Open the valve that releases the gas out of the reactor until the overpressure value is 0 kPa. Draw 12.00 grams of gas. When the gas is discharged, the average temperature in the facility is 22°C.

[0529] 5. The second nitrogen is delivered from the gas cylinder, with a quantity of 22.67 g. The flow rate of the supplied gas is S1 The speed is 0.7m 3 / h; the overpressure in the equipment after gas delivery is 6.89kPa. The average temperature in the equipment during gas delivery is 22.5℃.

[0530] 6. Second output of reaction gas: Open the valve that releases the gas out of the reactor until the overpressure value reaches 3.48 kPa. 12.03 grams of gas are extracted. When the gas is discharged, the average temperature in the facility is 22.5°C.

[0531] 7. The third nitrogen delivery from the gas cylinder is 11.33 g. The flow rate of the supplied gas is S1 The speed is 0.7m 3 / h; the overpressure in the equipment after gas delivery is 6.48kPa. The average temperature in the equipment during gas delivery is 23℃.

[0532] 8. The third time of outputting the reaction gas: the valve for releasing the gas from the reactor was opened until the overpressure value reached 3.48 kPa. 11.62 g of gas was extracted. When the gas was discharged, the average temperature in the facility was 23°C.

[0533] Calculated gas composition in the pre-process equipment:

[0534] gas value Units of measurement method Evaluation results Methane 0,00 %volume ISO 6947-3.4 S oxygen 20,21 %volume ISO 6947-3.4 S nitrogen 79,79 %volume ISO 6947-3.4 S

[0535] Liquid adsorbent rapeseed oil is delivered to the reactor R1 In the case of the accelerator module, the surface level is higher than that of the accelerator module. Rapeseed oil does not contain hydrocarbon fuel fractions and methyl esters.

[0536] Reactor R1 The liquid adsorbent in the boiler is heated to 250°C. At this temperature, nitrogen delivery to the plant begins according to the following algorithm:

[0537] The control system issues a command to maintain the pressure in the separator at 34.475 kPa;

[0538] If the pressure in the separator is lower than the set value, the valve for transferring nitrogen from the gas cylinder to the reactor and then to the acceleration module is opened;

[0539] The gas and liquid mixture enters the reactor space and catalyst space from the acceleration module at a speed of 30 to 40 m / s to achieve the following functions:

[0540] Speed ​​reduction module;

[0541] ·Tribostatic voltage generator.

[0542] When the set pressure value is reached, the inlet valve for the gas from the gas cylinder is closed and the outlet valve for releasing the reaction gas out of the device is opened;

[0543] If the pressure in the separator is lower than the set value, the output valve for discharging the reaction gas out of the device is closed, and the valve for delivering nitrogen from the gas cylinder to the reactor is opened.

[0544] After the test, the product is removed from the separator.

[0545] Analysis from separator F1 Product:

[0546] A sample of the organic liquid labeled "14.8.18" (nitrogen, not recycled) was analyzed. The liquid was analyzed by gas chromatography-mass spectrometry (GC-MS) to determine the substances present. In addition, the sample was screened by high temperature gas chromatography.

[0547] Sample "14.8.18" (nitrogen, not recycled) is a two-component mixture of about 75% of the upper organic layer and 25% of the lower aqueous portion. The analysis results show that about more than 50% of the organic portion is a mixture of higher fatty acids, mainly acids containing 18 carbon atoms in the molecule (oleic acid and stearic acid). About 4% of the organic portion is vegetable oil. The remaining organic portion is a mixture of organic substances, mainly fatty acid methyl esters (FAME), hydrocarbons (mainly C14 and C18), alcohols and aldehydes. The chromatographic readings of the GC-MS analysis and the substances identified are listed in the Appendix (the maximum value of vegetable oil is not included in the Appendix because its boiling point is extremely high and cannot be detected by standard GC-MS).

[0548] The chromatogram of sample "14.8.18" (nitrogen, not recycled) is Chart 12 Shown in.

[0549] Explanation of Chromatography:

[0550]

[0551]

[0552]

[0553]

[0554]

[0555]

[0556]

[0557]

[0558]

[0559]

[0560] Total content of product components:

[0561] Substance name Units of measurement value Hydrocarbons - Alkanes %quality 6.45 Hydrocarbons - Olefins %quality 3.73 Hydrocarbons - i-Alkanes %quality 2.07 Hydrocarbons - Aromatics %quality 0.89 Hydrocarbons - Naphthenes %quality 0.14 aldehyde %quality 1.81 acid %quality 65.88 Oleyl alcohol %quality 7.92 ester %quality 9.04 total 97.93

[0562] Analysis of Example 9 and the liquid reaction product led to the following conclusions:

[0563] The synthesis of hydrocarbon products is caused by:

[0564] 1. By decomposing nitrogen and oxygen molecules, then synthesizing these molecules and releasing excess energy.

[0565] 2. If there is enough excess energy in the catalyst zone during the decomposition of air molecules, the air->water conversion begins. Reaction 5. 7, 13, 14, 15, 16 and 17 , releasing 12.2MJ per kg of air.

[0566] 3. If there is enough excess energy in the catalyst zone during the air->water reaction, the air->methane reaction begins. reaction 5, 7, 13, 14, 15, 16 and 17 , 24.7MJ is released per kg of air.

[0567] 4. If there is enough energy in each catalyst zone during the reaction of methane in air, methane will Reaction 24 Direct conversion to common alkanes and hydrogen. To a lesser extent, alkanes can be synthesized if energy is insufficient, and then esters can be synthesized in the presence of oxygen, as well as alcohols from alkanes.

[0568] 5. The production of free fatty acids is related to the hydrolysis of triglycerides, based on the reaction between triglycerides and water produced by the air->water reaction.

[0569] Due to the reduction of nitrogen and oxygen concentrations and Reactions 5, 7, 13, 14, 15, 16 and 17 By the process described in the above, the concentration of methane molecules and the energy generated increase. Due to the energy generated, the bonds in the triglyceride molecules are broken and organic synthesis products are subsequently synthesized. These processes fall within the scope of the present patent application.

[0570] See Table 1 - Overview of the physicochemical reactions for all reaction details.

[0571] Example 10

[0572] Formation of organic synthesis products from vegetable oils in an air environment.

[0573] Reactor R1 With acceleration module and catalysis module, it can realize the following functions:

[0574] Speed ​​reduction module 4 ;

[0575] Frictional electrostatic voltage generator 4a , 4b ;

[0576] Atmospheric air fills the internal volume of the reactor. The mass concentrations of nitrogen and oxygen in the atmospheric air are 76.37% and 23.225% respectively. The relative number ratio of nitrogen molecules to oxygen molecules is 3.288. An air compressor is connected to the gas mixture inlet.

[0577] Gas composition calculated in the pre-process equipment:

[0578] gas value Units of measurement method Evaluation results Methane 0,00 %volume ISO 6947-3.4 S oxygen 23,23 %volume ISO 6947-3.4 S nitrogen 76,37 %volume ISO 6947-3.4 S

[0579] Liquid adsorbent rapeseed oil is fed into the reactor with a surface level above the acceleration module. The rapeseed oil does not contain hydrocarbon fuel fractions and methyl esters.

[0580] No gas circulation is used, which conveys the gas from the separator back into the reactor with the aid of a gas ventilator.

[0581] Reactor R1 The liquid adsorbent in the boiler is heated to 250°C. At this temperature, air delivery to the plant begins according to the following algorithm:

[0582] The control system issues a command to maintain the pressure in the separator at 34.475 kPa;

[0583] If the pressure in the separator is lower than the set value, valve V1 is opened to send air from the compressor into the reactor and then into the acceleration module;

[0584] The gas and liquid mixture enters the reactor space and catalyst space from the acceleration module at a speed of 20 to 40 m / s to achieve the following functions:

[0585] Speed ​​reduction module 4 ;

[0586] Frictional electrostatic voltage generator 4a , 4b ;

[0587] When the set pressure value is reached, the valve for delivering air from the compressor is closed and the valve for releasing the reaction gas from the device is opened;

[0588] If the pressure in the separator is lower than the set value, the valve for releasing the reaction gas out of the device is closed and the valve for sending air from the compressor to the reactor is opened.

[0589] After the test, the product is removed from the separator.

[0590] 3GTL-(060620181),A,6.6.18 / 1 3. Processing of heavy products of rapeseed oil in GTL process 3GTL-(060620182),B,6.6.18 / 2 3GTL process for light products of rapeseed oil

[0591] Analyzing three-phase separators F1 The product:

[0592] Two organic liquid samples were analyzed:

[0593] Both liquids were analyzed by gas chromatography-mass spectrometry (GC-MS) to determine the substances present. In addition, the samples were screened by high temperature gas chromatography (HTGC).

[0594] The analysis results show that more than 90% of sample "060620181), A, 6.6.18 / 1" is vegetable oil, and the rest is mostly fatty acid methyl esters (FAME) and a small amount of diacetone alcohol (<3%). The chromatographic readings of the GC-MS analysis and the substances identified are shown in the Appendix (the maximum value of vegetable oil is not included in the Appendix because its boiling point is extremely high and cannot be detected by standard GC-MS).

[0595] The sample labeled "(060620182), B, 6.6.18 / 2" is a mixture of FAME, saturated hydrocarbons and other oxygen-containing components. FAME (fatty acid methyl esters C16 to C24) accounted for about 40% of the sample.

[0596] The GC-MS data analysis of sample "060620182), B, 6.6.18 / 2" found that the sample contained saturated hydrocarbons from approximately C12 to C19. In addition, the sample also contained light oxygen-containing substances with carbon atom numbers ranging from approximately C6 to C10. These components formed a characteristic series in the order of retention: aldehydes with saturated hydrocarbon chains, methyl olefins, methyl alkanoates, and aldehydes with unsaturated hydrocarbon chains. The chromatographic reading of sample 3GTL-(060620181), A, 6.6.18 / 1 was Chart 13 Shown in.

[0597] The chromatogram reading of sample 3GTL-(060620182), A, 6.6.18 / 2 is Chart 14 Shown in.

[0598] The following table lists the interpretation of the two product chromatograms:

[0599]

[0600]

[0601]

[0602]

[0603]

[0604]

[0605] The following conclusions can be drawn from the analysis of liquid products:

[0606] The synthesis of hydrocarbon products -> diesel is caused by:

[0607] 1. By decomposing nitrogen and oxygen molecules, then synthesizing these molecules and releasing excess energy.

[0608] 2. If there is enough excess energy in the catalyst zone during the decomposition of air molecules, the air->water conversion begins. Reaction 1 , releasing 12.2MJ per kg of air.

[0609] 3. If there is enough excess energy in the catalyst zone during the air->water reaction, the air->methane reaction begins. Reactions 5, 7, 13, 14, 15, 16 and 17 , 24.7MJ is released per kg of air.

[0610] 4. If there is sufficient energy in the catalyst zones during the reaction of methane in air, methane is converted directly into ordinary alkanes and hydrogen according to reaction 24. To a lesser extent, if there is insufficient energy, alkanes can be synthesized and then esters in the presence of oxygen, as well as alcohols from alkanes.

[0611] 5. The production of free fatty acids is related to the hydrolysis of triglycerides, based on the reaction between triglycerides and water produced by the reaction of air->water.

[0612] The increase in methane molecular concentration and energy produced is due to the decrease in nitrogen concentration and Reactions 5, 7, 13, 14, 15, 16 and 17 The results of the described process. Due to the energy generated, the bonds in the triglyceride molecules are broken and the organic synthesis products are subsequently synthesized. These processes fall within the scope of the present patent application.

[0613]

[0614]

[0615] See Table 1 - Overview of the physicochemical reactions for all reaction details.

[0616] Embodiment 11

[0617] Organic synthesis products are formed from water and carbon dioxide in a cyclic process.

[0618] Reactor R1 With acceleration module and catalysis module, it can realize the following functions:

[0619] Speed ​​reduction module 4 ;

[0620] Frictional electrostatic voltage generator 4a , 4b ;

[0621] Preparation phase. Expel the air with the target gas.

[0622] Atmospheric air fills the internal volume of the reactor. The mass concentrations of nitrogen and oxygen in atmospheric air are 76.37% and 23.225%, respectively. The relative number ratio of nitrogen molecules to oxygen molecules is 3.288. The pressure cylinder (flow) containing carbon dioxide S1 ) is connected to the input gas mixture inlet.

[0623] 1.The atmospheric pressure is 99,425Pa.

[0624] 2. After the device is closed, at the given atmospheric pressure, there are 337 grams of air with a molecular mass of 28.98 g / mol, including 258 grams of nitrogen (76.3% by mass) and 78.5 grams of oxygen (23.07% by mass).

[0625] 3. The first delivery of carbon dioxide from the gas cylinder is 17.79 g. The flow rate of the supplied gas is S1 The speed is 0.7m 3 / h; the overpressure in the equipment after gas delivery is 3.48kPa. The average temperature in the equipment when delivering carbon dioxide is 18℃.

[0626] 4. First output of reaction gas: Open the valve that releases the gas out of the reactor until the overpressure value is 0 kPa. Draw 12.00 grams of gas. When the gas is discharged, the average temperature in the facility is 18°C.

[0627] 5. The second time, 355.87 g of carbon dioxide is delivered from the gas cylinder. The flow rate of the supplied gas S1 is 0.7 m 3 / h; the overpressure in the equipment after gas delivery is 68.95kPa. The average temperature in the equipment when delivering carbon dioxide is 18.8℃.

[0628] 6. Second output of reaction gas: Open the valve that releases the gas out of the reactor until the overpressure value reaches 4.65 kPa. Draw 270 grams of gas. When the gas is discharged, the average temperature in the facility is 18.8°C.

[0629] 7. The third time, 355.7 g of carbon dioxide is delivered from the gas cylinder. S1 The speed is 0.7m 3 / h; the overpressure in the equipment after gas delivery is 68.95kPa. The average temperature in the equipment when delivering carbon dioxide is 19.1℃.

[0630] 8. The third time of outputting the reaction gas: the valve for releasing the gas from the reactor was opened until the overpressure value reached 42.06 kPa. 156.95 g of gas was extracted. The average temperature in the facility during the discharge was 19.1°C.

[0631] Gas composition in pre-process equipment:

[0632] gas value Units of measurement carbon dioxide 74.47 %volume oxygen 5.920 %volume nitrogen 19.49 %volume

[0633] Liquid adsorbent water is delivered to the reactor R1 The water is free of hydrocarbon fuel fractions and methyl esters.

[0634] In gas compressor C2 With the help of F1 The gas is circulated to transport the gas back to the reactor.

[0635] Reactor R1 The liquid adsorbent in the boiler is heated to 60°C. Compressor C2 Start. From the separator F1 The gas mixture is directed to the compressor C2 The gas and liquid mixture enters the reactor space from the acceleration module at a speed of 200 to 400 m / s, where it comes into contact with the catalytic space to achieve the following functions:

[0636] Speed ​​reduction module 4 ;

[0637] Frictional electrostatic voltage generator 4a , 4b ;

[0638] After leaving the reaction space, the gas and liquid mixture is cooled in a water cooler. E3 Cooled and enters the separator F1In the separator, the gas is separated from the liquid and enters the gas compressor C2 The repeated gas mixture in the gas compressor C2 circulation between the inlet and outlet.

[0639] Product analysis.

[0640] At the end of the test, the product was discharged from the separator. A product consisting of the separated two components (aqueous component and organic component) was removed from the reactor boiler.

[0641] The product in the reactor boiler was separated into two components: an organic component on the surface and sides of the laboratory beaker, and water. After determining the volume composition ratio of the two components, the item was homogenized by mixing and preheating to 60°C. Then 3.5 ml of the homogenized product was transferred into a 4 ml test tube with a pipette. The product was separated into two components in a centrifuge at 4,400 rpm for 2 minutes. It was found that the volume of the organic component accounted for about 2.7% of the total volume.

[0642] The energy generated destroys CO 2 and H 2 O molecules, and products containing organic components and hydrocarbons appear in the reactor boiler and separator. The synthesis of organic synthesis products is based on Reactions 5, 7, 13, 14, 15, 16 and 17 These processes fall within the scope of this patent application.

[0643] See Table 1 - Overview of the physicochemical reactions for all reaction details.

[0644] Example 12

[0645] Generate heat in 3GTL process with efficiency >1

[0646] Process types: both cyclic and single run.

[0647] The data in Examples 9 and 10 are used to demonstrate the effect of thermal energy generation with an energy efficiency coefficient greater than 1. The examples show energy efficiency with minimal input energy. Process Type: One-shot nitrogen generation; see Example 9.

[0648] Process energy.

[0649] The power consumption of the process to heat the rapeseed oil was recorded. Taking into account the efficiency of the heater, the reactor was calculated R1 Energy transferred to the rapeseed oil and the transport gas (nitrogen) in space. The kinetic energy of the gas and nitrogen flow is also taken into account. No other forms of energy are involved in the process. The instantaneous input energy and the total input energy of the process are calculated.

[0650] Reactor R1The flow energy at the outlet is measured by a calorimeter in water cooler E3.

[0651] Temperature scanners installed at the inlet and outlet of the water cooler send data to a computer for calculating the cooler E3 The mass flow meter on the coolant delivery pipe sends data on the current coolant mass flow rate to the computer. The instantaneous energy and total output energy of the process are calculated.

[0652]

[0653]

[0654] Operation of equipment as part of a technical plant

[0655] Figure 4 A general flow chart for carrying out the method claimed in the present invention is shown. The flow chart includes a reactor R1 A device in which the process of gas and liquid molecular decomposition occurs and is maintained to produce a flow of electrons that affects the atoms of the gas and liquid. In the process of molecular decomposition, electrons bound to atoms are released. These electrons begin to interact with atoms and other fragments, and in the process they produce thermal energy that accumulates in the original gas and liquid molecules. In such a device, the mechanisms for the creation of plasma as an ionized state of the fragmented matter include temperature increase, molecular impact and electrical discharges. As a result of these processes, thermal and electromagnetic energy is generated in the reaction. This energy can be used to synthesize new compounds.

[0656] The device can be used to break down the molecules of all gaseous and liquid compounds and subsequently synthesize organic synthesis products, fuel hydrocarbons and obtain thermal energy.

[0657] Suitable input gases for the process forming the subject of the present patent application are:

[0658] ·Air;

[0659] ·nitrogen;

[0660] Carbon monoxide;

[0661] ·carbon dioxide;

[0662] ·oxygen;

[0663] ·hydrogen;

[0664] · Hydrocarbon gases, related petroleum gases;

[0665] Inert gas;

[0666] Nitric oxide and nitrogen dioxide;

[0667] or a mixture thereof.

[0668] Suitable input liquids for the method forming the subject of the present patent application are:

[0669] Liquids containing C, H, O, and N elements;

[0670] Vegetable oils;

[0671] Mineral oil;

[0672] Esters;

[0673] ·crude;

[0674] ·heavy oil;

[0675] Gas oil;

[0676] ·diesel fuel;

[0677] Pyrolysis products;

[0678] Methyl esters (FAME);

[0679] ·paraffin;

[0680] ·gasoline;

[0681] ·alcohol;

[0682] ·water;

[0683] or a mixture thereof.

[0684] Equipment operation using mixtures (methane and air), (associated petroleum gas and air) - Figure 4

[0685] Gaseous mixture of methane and air (associated petroleum gas and air) - gas flow S1 ——Enter the compressor C1 The suction pipe has a methane concentration of at least 18% by volume and other methane homologues in a concentration that is not explosive with air. The reaction gas purged of molecular hydrogen is simultaneously fed to the compressor C1 In the suction pipe of S20 . Mixed Flow S2 Entrance to the heater E1 The gas mixture is heated to 150°C to 160°C and used as a stream. S3 Enter the tube 1 , and then enter the acceleration module 2 ; It passes through the deceleration module 4 Leaving the interior space of the reactor 3 , to the decompression zone 5 . Decompression Zone 5 By compressor C2 In the deceleration module 4In the process, the gas flow and the electrode 4a and 4b The collision generates standing pressure waves and friction static electricity, the nitrogen and oxygen molecules dissociate and partially ionize, and the bonds of some oxygen atoms and nitrogen atoms are geometrically reorganized. These processes are exothermic. Due to the released energy, the CH and CC bonds are decomposed, and the subsequent synthesis of hydrocarbons proceeds according to the following reaction:

[0686] n / mC m H 2m+2 =C n H 2n +(n / m)H 2 (18)

[0687] n / mC m H 2m+2 =C n H 2n+2 +(n / m-1)H 2 ,(19)

[0688] Synthesis of gasoline component C from methane and its gaseous homologues 5 To C 10 Energy required:

[0689] Synthetic C 5 The minimum value of synthetic C is 42.696 kJ / mol; 10 The maximum value is 339 kJ / mol.

[0690] Synthesis of fuel component C from methane and its gaseous homologues 8 To C 18 Energy required:

[0691] Synthetic C 8 The minimum value of synthetic C 18 The maximum value is 640.458 kJ / mol.

[0692] Synthesis of Diesel Component C from Methane and Its Gaseous Homologs 11 To C 20 Energy required:

[0693] Synthetic C 11 The minimum value of synthetic C is 376.74 kJ / mol; 20 The maximum value is 715.806 kJ / mol.

[0694] Reaction products (gas, liquid, solid in the form of carbon), flow S4 (which mainly contain liquid hydrocarbons), are oxygen-containing organic components; they are E3 Heat energy is released in the S22- Low boiling point liquids (Freon, etc.) - in heat exchangers E3 is heated, the flow S23 ——and enter the organic Rankine cycle module to generate electricity by self-heating. S5 Enter the three-phase separator Mem1 - F1 In the separator, the flow S5 Separated into:

[0695] ·flow S7 - solid carbonaceous substances (fullerenes);

[0696] ·flow S10 - liquid, reaction water;

[0697] ·flow S9 - mixtures of hydrocarbons and organic liquids;

[0698] ·flow S8- Reactive gas.

[0699] From three-phase separator F1 Gas flow S8 Enter the compressor C2 In this configuration, the compressor C2 There are two functions:

[0700] 1. In the reactor R1 The space forms a decompression zone.

[0701] 2. The reaction gas, flow S17 , delivered to the membrane separation module.

[0702] flow S17 Guide to membrane Mem3 The gas separation is carried out on the membrane. Its main function is to S19 The concentration of molecular hydrogen in the gas is reduced to a level that reduces the pressure in the device and allows more gas to be fed in. S18 It is the obtained molecular hydrogen and other gases whose main components are molecular hydrogen. S20 The circulating flow from the valve block SP2 is directed into the compressor C1 The inlet then enters the reactor R1 Excess gas, flow S21 It is led out of the unit for external use.

[0703] When processing liquid hydrocarbon products, it is expected that these products will be supplied to the storage tank from an external source F2 (flow S15 ). Hydrocarbons from the storage tank F2 Enter the pump P1 The entrance, flow S16. A mixture of hydrocarbons and organic liquids (fluid S9 ) and reaction water (flow S10 ) is also directed to the pump P1 Entrance.

[0704] As a stream S11 , a mixture of these components enters the valve block SP1 , here it is split into two streams:

[0705] ·flow S12 , enter the heater E2 The hydrocarbon mixture heated to 150°C to 160°C enters the reactor R1 The interior space;

[0706] ·flow S14 - Hydrocarbon mixture discharge unit.

[0707] Use CO 2 and air mixture equipment operation - Figure 4

[0708] A gaseous mixture of carbon dioxide and air (flue gas from industrial power plants and thermal power plants can be used) 1 Enter the compressor C1 The gas mixture is sucked into the compressor C1 Compressed to a pressure of 11 to 15 bar and enters heater E1. CO 2 The mixture of air and gas is heated to a temperature of 150-160°C and is used as a flow S3 Enter the tube 1 , and then enters the acceleration module 2; it passes through the deceleration module 4 Leaving the interior space of the reactor 3 , to decompression zone 5. In the deceleration module 4 In the process, the gas flow and the electrode 4a and 4b The collisions lead to standing pressure waves and frictional static electricity, dissociation and partial ionization of nitrogen and oxygen molecules, and geometric reorganization of some bonds between oxygen and nitrogen atoms. These processes are exothermic; due to the released energy, CO 2 The molecular dissociation process proceeds according to reaction (24).

[0709] 1 mol CO 2 Complete dissociation requires 730 kJ. External physical effects are equivalent to 8 to 9 kJ / mol of incoming gas, resulting in the generation of a standing pressure wave and the gas flowing out at supersonic speeds, generating energy equivalent to 800 to 900 kJ / mol. This energy acts on the bonds in the carbon dioxide molecules, breaking them apart and leading to reactions 1 to 27 in Table 1.

[0710] By controlling the energy generated when bonds are broken and input gas molecules are dissociated, a generator gas consisting primarily of carbon monoxide, oxygen and small amounts of hydrocarbon gases can be produced.

[0711] A stream of reaction products (gas, liquid, solid in the form of carbon) containing primarily nitrogen and oxygen S4 In heat exchanger E3 Heat energy is released in the heat carrier flow S22 , low boiling point liquid (Freon), in the heat exchanger E3 Heat up and flow 23 Enters the organic Rankine cycle module to generate electricity and heat. S5 Directed to the centrifuge Mem1 and three-phase separator F1 Here, the reaction gases are separated, mainly to separate the mixture of nitrogen and oxygen from the residual CO in the reaction gases. 2 Separation.

[0712] From three-phase separator F1 Airflow S8 Enter the compressor C2 In this configuration, the compressor C2 There are two functions:

[0713] In the reactor R1 A decompression zone is formed in the space;

[0714] · The reaction gas flow S17 Delivery to membrane Mem3 .

[0715] flow S17 is directed to the membrane Mem3 The gas separation is carried out on the membrane. Its main function is to S19 The concentration of molecular nitrogen and oxygen in the gas is reduced to a level that reduces the pressure in the equipment and allows more gas to be introduced. S18 A mixture is obtained, the main components of which are molecular nitrogen and oxygen.

[0716] flow S20 (circulation flow), from the valve block SP2 is directed to the compressor C1 The inlet and then the reactor R1 For further processing. The remaining gas flow S21 It is led out of the unit for external use.

[0717] This configuration does not use the following devices:

[0718] Pump P1 ;

[0719] Storage tank F2 ;

[0720] Heater E2 ;

[0721] Valve block SP1 ;

[0722] ·Heliu S9 , S10 , S11 , S12 , S 13 , S14 ;

[0723] Equivalent

[0724] The embodiments of the method described are limited only to the specific implementation possibilities described in this application. Various changes and modifications may be made without departing from the scope of the invention.

[0725] It is apparent from the foregoing description that functionally equivalent methods and compounds, as well as the methods listed below, are within the scope of the patent being filed. These variations and modifications fall within the scope of the formulae contained in this document. The invention being filed is limited only to the key points of the formulae in this document and to all equivalent ranges mentioned in these formulae. It should be kept in mind that the present invention is not limited to specific methods, reagents, and compound compositions, which can of course be changed. It should also be noted that the terms used in this application are only used to describe specific implementation methods and are by no means restrictive terms. If we use Markush structures to describe features and aspects of the present invention, then the present invention is also described from the perspective of any single element or sub-element group of the Markush structure.

[0726] For all purposes (particularly the written description provided in the present invention), all intervals disclosed in the present invention description also include all possible parts of these intervals and combinations of interval parts. Each of these intervals is easily identifiable as sufficiently descriptive and unique even if it is divided into half, three parts, four parts, five parts, ten parts, etc. For example, the interval of 30 to 400 m / s disclosed in this application can be divided into three parts, further divided and combined in any way.

[0727] All expressions such as "up to", "less than", "greater than", "at least", etc., refer to the stated quantity, which can then be divided into parts similar to the above intervals.

[0728] The scope includes each individual element. Although certain versions of implementations have been described in the present description, it should be borne in mind that changes and modifications can be made without departing from the claimed method in accordance with the formula and text of the claimed invention.

[0729] Industrial applications of the invention

[0730] The invention can be used in many industrial sectors. It is mainly used for treating existing gases and producing new gases. It can be used to develop gases produced in combustion processes, produce organic synthesis products or, for example, produce "green" hydrogen.

[0731] legend

[0732] 1 Feed pipe

[0733] 2 Acceleration module

[0734] 2.1 Equivalent membrane

[0735] 2a Hypersonic tube

[0736] 2b High-voltage receiving cavity

[0737] 2c Laval nozzle (hypersonic jet)

[0738] 2D nozzle beam arrangement

[0739] 3. The internal space of the reactor

[0740] 4 speed reduction module

[0741] 4a, 4b electrodes (friction electrostatic generator)

[0742] 5Decompression zone with reduced pressure atmosphere

[0743] 6 output tube

[0744] C1 Compressor

[0745] C2 Gas Ventilator (Blower)

[0746] S1 Gas Flow

[0747] S2 Hybrid Stream

[0748] S3 Heating Mixed Flow

[0749] S4 reaction product stream

[0750] S5 Cooling Flow

[0751] S7 Solid Carbonaceous Material Flow

[0752] S8 Reaction Gas Flow

[0753] S9 mixture of hydrocarbons and organic liquids

[0754] S10 Reaction Water Flow

[0755] S11 Synthetic Liquid Product Stream

[0756] S12 is used to recycle part of the synthesis product stream to the reactor

[0757] S13 is used for heating the part of the synthesis product circulated to the reactor

[0758] S14 Synthetic liquid product stream leaving the device

[0759] S15 External input liquid product flow to equalization tank F2

[0760] S16 External input liquid product stream to the inlet of pump P1

[0761] S17 Reaction gas flow in the continuing stage

[0762] S18 Nitrogen stream separated from the reaction gas; for external use

[0763] S19 Reaction gas flow to purge nitrogen

[0764] S20 circulation flow

[0765] Hydrogen stream synthesized in the S21 process and methane residue after membrane separation

[0766] S22 Low boiling point liquid flow

[0767] S23 Flow for power generation

[0768] The SP1 valve block separates the mixture of synthetic product and external input material into two streams:

[0769] For external use

[0770] For recycling

[0771] The SP2 valve block splits the reaction gas mixture into two flows:

[0772] For external use

[0773] For recycling

[0774] P1 pump, used to pump away synthetic liquid products:

[0775] For external use

[0776] For further processing in the loop

[0777] E1 Input Gas Heater

[0778] Liquid product heater in E2 cycle

[0779] E3 Heat Exchanger

[0780] F1 three-phase separator

[0781] F2 is used to receive the equalization tank of external input liquid

[0782] Mem1 Centrifuge for separating solids from reactions

[0783] Mem3 membranes for gas separation

[0784] R1 Reactor

Claims

1. The method is for homolytic and heterolytic cleavage in gaseous and liquid molecules with release of bonding energy, and its application to change the internal geometric structure of certain molecules, leading to the synthesis of new compounds not contained in the initial gas and liquid, with secondary release of energy during the synthesis, without the need for nuclear reactions on equipment for its realization, characterized in that Increase of the energy of the working environment and use of this energy to generate heat and simultaneously synthesize new compounds, due to the physical effect of standing pressure waves on gas and liquid molecules at various temperatures, where the temperature is a measure of the activation energy, and the subsequent dissociation of molecules into atoms or molecular fragments (free radicals), partial ionization of atoms and subsequent transformation of the atomic bonds of the molecules, where the atomic number remains unchanged, but the atomic weight and the proton-neutron ratio change. The method also includes the direct conversion of the mass of the neutron into a mass equivalent to the total mass of 1 electron and 1 proton, which does not exceed the framework of the electrodynamic interaction of electrons and atomic nuclei, ensuring the absence of radiation, where the method also includes the conversion of atoms into chemical molecules or the reverse conversion of 1 electron and 1 proton from the volume into 1 neutron, these elementary particles can be free, and the external exchange of energy and mass is equal to the mass of the positive charge and equal to the reduction of the mass of the neutron and proton. The method further includes the reverse reaction of the physical effects to form new compounds not contained in the initial gas and liquid, releasing the energy generated in the process of reorganizing the atoms into the original molecules, wherein the proposed method is performed by a combination of initial impacts, for example, 12 C 1H 4=16Ne=16O, and the method further includes rearranging the structure of certain molecules as a reaction to the physical impact without changing the atomic number, mass number, atomic weight, synthesizing new compounds in the process, including those not contained in the initial gas and liquid, while releasing the energy generated in these synthesis reactions, for example, 14 N 2=12C 16 O; 12 C 16 O 2=14 N 2 16 O. The proposed method is achieved by a combination of initial impacts, such as: The temperature is increased to 250°C, ideally 140°C to 150°C; Reduce the pressure (create a reduced pressure atmosphere) to -100 kPa, ideally -65 kPa; Generate standing pressure waves; Discharges with breakdown voltages of 1 to 15 kV (tribostatic discharge, barrier discharge, spark discharge); ·Depending on the discharge in the gas, the magnetic field value in the reactor is 70 to 120 nTl; Micro explosion; Shock, impact force, producing negative acceleration of 50,000 to 150,000 g; or a combination of these effects.

2. The method according to claim 1, characterized in that The energy of the breaking and recombination of bonds in the original molecules is used to transform gases and liquids, for the ionization of atoms of subsequent molecules, and to organize the cold plasma flow, changing the geometric length and angular structure of the atoms of the original input material molecules within the framework of electrodynamic interactions with adjacent molecules, while forming new chemical elements / compounds, including chemical elements / compounds not contained in the initial gases and liquids, and a two-way reaction exchange of energy-mass, mass-energy, without nuclear reactions.

3. The method according to claim 1, characterized in that The physical impact of this process on nitrogen N2 molecules depends on the pressure and velocity of the gaseous mixture, inducing the following physical and chemical changes in the nitrogen molecules: Symmetrical decomposition of nitrogen molecules: · are two nitrogen atoms N, and; · Two CH2 radicals, or; A CH2 radical and a hydrogen atom H2 and a carbon atom C, or; · two carbon atoms 2C and four hydrogen atoms 4H, or; ·It is carbon atom C and methane molecule CH4; Asymmetric decomposition of nitrogen molecules: · is an oxygen atom O and a carbon atom C, and; Carbon monoxide molecules CO in a reaction between carbon atoms C and oxygen atoms O, or; In the parallel process of symmetric and asymmetric decomposition: In the reaction between molecular nitrogen N2 and molecular oxygen O2, it is converted into water molecules H2O and carbon atoms C, and; In the reaction between molecular nitrogen N2 and molecular oxygen O2, it is converted into water molecules CH4 and carbon atoms C, and; · In the reaction between two oxygen atoms O, they are converted into oxygen molecules O2, and; into CO2 molecules in the combustion reaction between carbon C and molecular oxygen O2, and into CO2 molecules and water molecules H2O in the reaction between methane CH4 and two molecules of molecular oxygen O2, and; In the polycondensation reaction, it is converted into organic molecules and hydrocarbon molecules and synthesizes the following products: ο aldehydes; ο ketone; ο alcohol; ο simple and complex ethers; ο fatty acids; o alcohols of fatty acids; ο hydrocarbon gases; ο Hydrocarbon liquids: o cycloalkanes; o aromatic hydrocarbons; o isoalkanes; o normal alkanes.

4. The method according to claim 1, characterized in that The physical impact of this process on nitrogen O2 molecules will induce the following physical and chemical changes in nitrogen molecules: Symmetric decomposition only: · are two oxygen atoms O, and; · two nitrogen N atoms and four hydrogen atoms, and; · two CH2 radicals and two hydrogen molecules, or; A CH2 radical and three hydrogen molecules H2 and a carbon atom C, or; · two carbon atoms 2C and eight hydrogen atoms 8H, or; Two methane molecules CH4; Asymmetric decomposition only: · Nitric oxide molecule NO and two hydrogen atoms, or; · is a nitrogen molecule and 4 hydrogen atoms, and; · Two CH2 radicals and 4 hydrogen atoms, or; A CH2 radical and three hydrogen molecules H2 and a carbon atom C, or; · two carbon atoms 2C and eight hydrogen atoms 8H, or; Two methane molecules CH4; In the parallel process of symmetric and asymmetric decomposition: In the reaction between molecular nitrogen N2 and molecular oxygen O2, it is converted into water molecules H2O and carbon atoms C, and; In the reaction between molecular nitrogen N2 and molecular oxygen O2, it is converted into methane molecules CH4 and carbon atoms C, and; · In the reaction between two nitrogen atoms N, it is converted into nitrogen molecules N2, and; into CO2 molecules in the combustion reaction between carbon C and molecular oxygen O2, and into CO2 molecules and water molecules H2O in the reaction between methane CH4 and two molecules of molecular oxygen O2, and; In the polycondensation reaction, it is converted into organic molecules and hydrocarbon molecules and synthesizes the following products: ο aldehydes; ο ketone; ο alcohol; ο simple and complex ethers; ο fatty acids; o alcohols of fatty acids; ο hydrocarbon gases; ο Hydrocarbon liquids: o cycloalkanes; o aromatic hydrocarbons; o isoalkanes; o normal alkanes.

5. The method according to claim 1, characterized in that The physical impact of this process on the methane CH4 molecule triggers the following physical and chemical changes in the methane molecule: CH4=0,5O2 3,77N2+O2=7H2O+0,15C+0,3O2 3,77N2+O2=7CH4+1,305C+0,3O2 nCH4=C n H 2n+2 +(n-1)H2 (n / m)C m H 2m+2 =C n H 2n+2 +(n / m-1)H2 6. The method according to claim 1, characterized in that The physical impact of this process on the carbon dioxide CO2 molecule triggers the following physical and chemical changes in the carbon dioxide CO2 molecule: Possible decomposition: 2СΟ2=2СΟ+O2; Possible decomposition СO2=С+O2; Possible decomposition СΟ2=N2O; Possible decomposition 2N2O = 2N2 + O2; The reverse reaction may be: N2 = N + N; O2=O+O; 2N2O=2N2+O2; N2O=CO2 7. The method according to claim 1, characterized in that The plasma specific energy is 0.01J / cm 3 Up to 16J / cm 3 .

8. The method according to claim 1, characterized in that The electric field strength in the gas discharge reactor is less than 14 kV / cm.

9. The method according to claim 1, characterized in that The gas component consists of methane, ethane, propane, butane or a mixture of at least two of these gases with an admixture of CO2, air or oxygen.

10. The method according to claim 1, characterized in that The gas component consists of ethylene, propylene, butylene, isobutylene or a mixture of at least two of these gases with an admixture of CO2, air or oxygen.

11. The method according to claim 1, characterized in that The gas component is composed of methane, ethane, propane, isopropane, butane, isobutylene et FC-butane or a mixture of at least two of these gases with an admixture of CO2, air or oxygen.

12. The method according to claim 1, characterized in that The gas component consists of CO2.

13. The method according to claim 1, characterized in that The gas component consists of N2.

14. The method according to claim 1, characterized in that The gas composition consists of a mixture of nitrogen oxides.

15. The method according to claim 1, characterized in that The gas component consists of an inert gas component or a mixture of at least two of them.

16. The method according to claim 1, characterized in that The gas component consists of a mixture of N2, CO2, and O2.

17. The method according to claim 1, characterized in that The gas component consists of air.

18. The method according to claim 1, characterized in that The liquid component comprises a gasoline fraction, a paraffin fraction, a diesel fraction, an oil fraction, a heavy oil, a diesel or a mixture of at least two of these substances.

19. The method according to claim 1, characterized in that The liquid component comprises vegetable oil, mineral oil or a mixture of at least two of these substances.

20. The method according to claim 1, characterized in that The liquid component comprises a heat-treated vegetable oil, a mineral oil or a mixture of at least two of these substances.

21. The method according to claim 1, characterized in that The liquid component comprises water.

22. The method according to claim 1, characterized in that The liquid component comprises free fatty acids, alcohols, aldehydes, ketones, ethers and ethers, unsaturated hydrocarbons or a mixture of at least two of these substances.

23. The method according to claim 1, characterized in that With the help of the feed liquid the following is obtained: Inorganic, organic, hydrocarbon liquids or mixtures thereof with varying composition; Non-hydrocarbons, hydrocarbon gases or mixtures thereof with varying compositions; Provide thermal energy with an energy efficiency coefficient greater than 1.

24. Apparatus for carrying out the method according to claim 1, wherein a physical effect is used: A shock wave and a set of means for inducing the shock wave in the reactor and heating the gas to the desired temperature. Discharge due to frictional electrostatic phenomena; The reactor consists of:

1. The acceleration module (2), consisting of a high-pressure chamber (2b) and an equivalent membrane (2.1), is a set of Laval micro-nozzles (2c) to ensure the delay of the pressure rise in the low-pressure chamber (3), the maximum velocity of the critical section nozzle and the maximum velocity of each nozzle outlet.

2. A low pressure chamber (3) which contains the process gas which was initially in the chamber (3) and whose concentration must be maintained by converting the raw gas into working gas. Liquid products can be synthesized in the low pressure chamber.

3. The deceleration module (4), which is a large device composed of metal plates (4.1), blocks the flow path of the raw gas as much as possible and ensures that the raw gas collides with them. The deceleration module (4) contains a tribostatic voltage generator (4.2) as an internal device. The tribostatic generator (4.2) is a system consisting of an insulator and alternating metal electrodes (4a), (4b) attached to the metal plate of the deceleration module (4), with a gap of 0.5 to 10 mm, preferably 1 mm, between them. The metal electrode conductors are selected according to the following criteria: Electrodes having the largest difference in the electron emission work of the metals must be placed adjacent to each other. The movement of the raw gas through the gap between the electrodes causes a tribostatic effect and generates a voltage across the adjacent electrodes, and once the breakdown voltage of the gas gap is reached, discharge occurs in the moving gas, leading to further dissociation of molecules and ionization of atoms in a given gas. During the increase in density, the initially cold gas in the reactor is almost instantly heated to high temperatures (up to 30,000 K), which can be controlled by varying the temperature to change the intensity of the shock wave: The pressure in the high pressure chamber of the acceleration module; The pressure in the low-pressure chamber of the module; Import and working gas parameters; Various processes then take place in the heated gas particles: Stimulate molecular vibrations; Dissociation, ionization, etc., the effect and speed of which depend on temperature (and density).

25. The device according to claim 24, characterized in that It is equipped with a feed pipe (1) for conveying the gas and an output pipe (6) for its discharge: Inorganic, organic, hydrocarbon liquids or mixtures thereof with modified composition; Non-hydrocarbon, hydrocarbon gas or their mixture with modified composition; Thermal energy, the value of which provides an energy efficiency coefficient greater than 1.

26. The method according to claim 1, characterized in that The level of the liquid component in the reactor is maintained close to the level of the acceleration module (2).

27. The method according to claim 1, characterized in that The specific energy range of plasma is 0.01J / cm 3 Up to 16J / cm 3 .

28. The method according to claim 1, characterized in that The tribostatic electric field strength based on gas discharge in the reactor is less than 14 kV / com, and the tribostatic generator contains metals Fe, Co, Ni, Cr, Gd, W, Al or their alloys containing C, Cu, Hf, Pd, Os, and Pt.

29. The method according to claim 1, characterized in that The magnetic field value based on the gas discharge in the reactor is 70 to 120 nTl.

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