HYBRID FUEL AND METHOD OF ITS PRODUCTION

[0001] the present invention relates generally to development and production of hybrid types of fuel and methods in particular of producing liquid kinds of fuel, including hydrocarbons mineral, vegetable and animal origin.

[0002] suitable liquid STI are important raw product for fuel and chemical application. In the present time, liquid hydrocarbons, mainly frequently is obtained from raw material based on crude oil by different methods. However as world reserves of crude oil reduced, there is growing demand for search for alternative sources of liquid energy carriers. Possible alternative sources include biomass, coal and natural gas. Methane, which is the main component of natural gas, biogas and gasification of coal is the source of, along with emulsions, including vegetable and animal fats. World reserves of natural gas constantly increased, and natural gas in the present time detected more than, than oil.

[0003] from - the problems, associated with transportation large volumes of natural gas, larger part of natural gas, produced together with oil, in particular, in places difficult, is burnt and lost. Consequently, conversion of natural gas directly in higher hydrocarbons, is especially attractive method to increase the quality of ny natural gas, at which can be overcome accompanying technical difficulties. Significant majority of methods conversion of methane in liquid hydrocarbons includes the first converting methane into synthetic gas ("singaz", in a context of this description), mixture of hydrogen and carbon oxide. Preparation of synthetic gas is intensive and energy intensive; therefore track, which do not require formation of synthetic gas, are preferable. For example, usual at hydro cleaning is used two stages, first production of syngas, and then creation of free radicals under action of high temperatures and pressure, for reaction with oil, subject to hydro cleaning. Such processes are very energy intensive. Was a row of alternative methods for conversion of methane directly in higher hydrocarbons.

[0004] existing proposals by transformation light gases, such as methane and carbon dioxide, and also biofuel, into liquid fuel are subjected to multiple problems, which limit their provisional market potential. Methods of oxidative interaction usually include high exothermal and potentially hazardous combustion reaction of methane, often require expensive systems of oxygen generation and production of large amounts of ecologically dangerous carbon oxides. The other side, existing methods of reducing interaction, frequently have low selectivity in relation to aromatic hydrocarbons, and can require expensive together used initial raw material for improving conversion and/or selectivity of aromatic hydrocarbons. In addition, at any method of reducing interaction is formed large amount of hydrogen and, for economic expediency is required method of effective employment of hydrogen, as by-product. Since deposit natural gas often are in remote places, effective application of hydrogen may be serious problem.

[0005] one more switching factor in hydrocarbon liquid styakh, is presence of polycyclic aromatic compounds, and also the total number of aromatic compounds. In some cases these compounds are known carcinogens. Regulating members began to pay attention on the scope of these compounds in environment, and require WiFi client continuously ny of polycyclic aromatic hydrocarbons in industrial processes, including in treatment of fuel. To the same, polycyclic aromatic compounds during combustion of have tendency to formation of small particles, which leads to additional ecological issues. Nevertheless, WiFi client continuously tracks the polycyclic aromatic compounds is difficult at existing methods of processing oil, from - the variety, technical difficulties and cost of various methods reaction, necessary for reduction of polycyclic aromatic compounds. For example, in some situations, reduced polycyclic aromatic compounds requires addition of considerable amount of gaseous hydrogen and results to formation of carbon dioxide, which is alone requires removal and/or restoration.

[0006] vodka difficulty when using natural gas as liquid hydrocarbon source relates to the the fact, that many deposit natural gas along the whole peace contain large amount of, sometimes more than 50%, of carbon dioxide. Carbon dioxide is target to increase the control of national nnogo from - behind its potential contribution global change of climate. In addition, any method, which requires separating and removing large amounts of carbon dioxide from natural gas, is possibly, will be economically intolerable. Itself on art, some deposit natural gas have such high levels of carbon dioxide, that in the present time are considered to be economically non-return.

[0007] in addition, in the existing methods of producing different types of biofuel from fats and oils usually esterification for production of biodiesel fuel, in particular, in its form without impurities (T. E. v100). This expensive method, and exist known technical problem, connected with application of biodiesel fuel, in particular, v100, in existing plants. The described below versions of the invention are directed on said problem.

[0008] exist also large reserves of heavy oil/bitumen, that may not be easily used. Economically, WiFi client continuously tracks the viscosity (T. E. density of oil in degrees of API) heavy oil, increases its value for oil refining company, and also reduces costs of transportation.

[0009] there is also necessity of improving properties of kinds of fuel for transportation and heating. These include improving was to increase the efficiency of energy conversion in useful work and reduced emissions of greenhouse gases (pg), including GES, hydrocarbons, of SOx, of NOx, and solid particles. By still - there is necessity in reduction of aromatic fractions, including polycyclic aromatic hydrocarbons, in hydrocarbon types of fuel and biofuels.

[0010] there is demand creation of improved conversion method of light gas (for example, methane) in liquid hydrocarbons, in particular, where light gas is present in the stream of natural gas, containing large amount of carbon dioxide. There is also necessity of creating hybrid fuel, for, to use unique characteristics of products, produced from natural gas, bio fats and oils, crude and heavy oil/bitumen, in mixed fuel, which can be obtained at costs, comparable with existing expenses on types of hydrocarbon fuel. There is necessity of integration methods, systems and devices, which is reduced total volume of emissions greenhouse gases (pg) and solid particles based on analysis of operational resource. Such methods also require possibility of using carbon dioxide, to minimize its emission.

[0011] the invention relates to hybrid types of fuel and methods of their production.

[0012] in one aspect, hybrid fuel is produced by method, which includes: introduction of the first reagent in reactor, where the first reagent comprises one or more light gas; action non-thermal plasma on the first reagent in conditions of sufficient, to reform the first reagent with formation of syngas and generation of free radicals and electrons of high energy;

introduction of the first liquid initial fuel reactor; and close interaction of reaction of action products non-thermal plasma on the first reagent with the first liquid initial fuel in reactor, to produce modified liquid fuel. As is disclosed in this description, hybrid fuel, produced in accordance with the open methods, can be used as an alternative "the drop-In of" fuel. In some versions of implementation, blend or mixture is obtained with hybrid fuel, obtained according to the present invention. Such mixture include, without limiting, vehicles fuel, biofuel emulsion, fuel for jet engines, diesel fuel and other standard fuel products, as other components in the mixture. In one version the first reagent additionally contains the second initial liquid fuel.

[0013] in one aspect of hybrid fuel is provided hybrid fuel, containing the first fuel product and second fuel product. The first fuel product includes, without limiting, biofuel emulsion, fuel for jet engines, diesel fuel, diesel fuel with ultra-low content of sulfur or other types of fuel on oil base (for example, result 102 on Figure 1 or 222 on Figure 2). The second fuel product includes fuel, resulting from one or more light gases in combination with initial liquid fuel (for example, 328 on fig. Of members or result 104 on fig. 11). In some versions of implementation hybrid fuel contains at least approximately 20 wt.% of the first fuel product. In some versions of implementation hybrid fuel contains to approximately 20 wt.% of the first fuel product. In additional versions hybrid fuel contains from approximately 5 wt.% to approximately 10 wt.% of the first fuel product. In other versions the hybrid fuel contains water. In some versions of implementation hybrid fuel contains approximately 20 wt.% of the first fuel product and approximately 80 wt.% of the second fuel product. In some versions of implementation hybrid fuel additionally contains to approximately 20%, or from approximately 10% to approximately 20%, or approximately 20% water, residue composition includes the second fuel product. In some versions of implementation temperature solidification of hybrid fuel is approximately -30 theoretically. In other versions the temperature solidification of hybrid fuel is less than approximately -15 theoretically. In other versions the temperature solidification of hybrid fuel is approximately from -10 theoretically to approximately -50 theoretically, or approximately from -25 theoretically to approximately -35 theoretically. In other versions the temperature cloud of hybrid fuel is approximately -44 theoretically. In other versions of the invention temperature cloud of hybrid fuel is not more than approximately -10 theoretically, or approximately -15 theoretically. In some versions of implementation temperature solidification of hybrid fuel is approximately from -10 theoretically to approximately -15 theoretically, or approximately 15 theoretically below, than temperature of solidification of the second fuel product in insulation (that is, in absence of the first fuel product, or before joining of production of hybrid fuel). In some versions of implementation hybrid fuel contains not more than approximately 1% of polycyclic aromatic hydrocarbons. In other versions the hybrid fuel contains not more than approximately 20% aromatic hydrocarbons. In some versions of implementation the second fuel product is a hybrid fuel, produced methods, described in the present invention. In some versions of implementation the first fuel product also contains ether of glycerol.

[0014] in another aspect a method of preparing hybrid fuel. Method includes: introduction of the first reagent in reactor, where the first reagent comprises one or more light gas; action non-thermal plasma on the first reagent in conditions sufficient for formation of syngas (that is with + ng) and free radicals; introduction of the first liquid initial fuel reactor; and close interaction of synthetic gas and free radicals, formed by from the first reagent, with the first liquid initial fuel in reactor, to produce modified liquid fuel. In some versions of implementation hybrid fuel is a biofuels. In some versions of implementation, the method is a method of processing oil. In some versions of implementation process free radicals formation not precedes process dissociation of one or more light gases (T. E. reaction products are the first reagent directly is mixed with the first liquid initial fuel). In some versions of implementation, the reactor is a reactor non-thermal plasma. In some versions of implementation, non-thermal plasma reactor is a reactor with sliding by arc discharge, microplasma generator, or homogenizer. In some versions of implementation, free radicals are formed by means of device with high force shift, ultrasonic, cavitation action, mixing device high-energy or their combination.

[0015] in some versions of implementation, methods of preparing hybrid fuel, discovered in this description, additionally include addition of catalyst in reactor. In some versions of implementation, catalyst is a metallic catalyst, organometallic catalyst, nanosfericheskii catalyst, catalyst on carrier, soluble catalyst or mixture of two or more. In some versions of implementation, catalyst is molibdenorganicheskoe compound.

[0016] in some versions of implementation, in methods of producing hybrid fuel, disclosed in this description, are formed ethyl esters of fatty acids (FAEE) and glycerol as by-products. In some versions of implementation by-product glycerol is additionally subjected to reaction with formation of one or more of essential products glycerol, which are added in hybrid fuel.

[0017] in additional aspect, a method is proposed for reforming of light gas. Thermal reforming method includes one or more light gases in the presence of non-thermal plasma in conditions, sufficient for generation of free radicals formation. In some versions of implementation, stage reforming represents one or more of dry reforming (T. E. interaction of methane with carbon dioxide in reactor, such as plasma reactor), steam reforming, partial oxidation and formation of methyl radicals. In some versions of implementation, stage of reforming one or more light gases, prepared at pressure of approximately less than 5 atm. In other versions, method is carried out at temperature from approximately 200 theoretically to approximately 500 theoretically. In some versions of implementation stage reforming represents one or more of dry reforming, steam reforming, partial oxidation and formation of methyl radicals.

[0018] in some versions of implementation, in methods of producing hybrid fuel, disclosed in this description, light gas is methane, natural gas or their mixture.

[0019] in one aspect is disclosed for preparing hybrid fuel. Device includes first inlet hole for insertion of the first reagent, where the first reagent comprises one or more light gas; electrodes are in liquid stnom connection with inlet hole, the electrodes are able to create arc with supply of voltage, and the electrodes is determined path passage of first reagent; the second inlet opening for introduction of the first liquid initial fuel in device; output zone, where product of reaction of the first reagent and electrodes and first liquid initial fuel come in contact; and outlet hole, which is in liquid stnom connection with zone output. In some versions of implementation, zone outlet is located between, and is in liquid stnom connection with by, determined with the use of electrodes, and second inlet hole. In some versions of implementation device also includes Helmholtz coils. In some versions of implementation Helmholtz coils are located within or near with reactor. In some versions of implementation Helmholtz coils are located within or near zone output.

[0020] in some versions of implementation, device additionally includes catalyst. In some versions of implementation catalyst is disposed within or near zone output.

[0021] in some versions of implementation, device additionally includes heating coils. In some versions of implementation heating coils are able heated content device to preset temperature.

[0022] in some versions of implementation, device additionally includes cathode slightly accurate force. In some versions of implementation cathode slightly accurate force performs functions of acceleration of electrons flow and/or density of electrons. In some versions of implementation cathode slightly accurate force includes thorium.

[0023] in one of the aspects the method of conversion of light gases in liquid STI. Typical methods are those, in which is used generation of free radicals for the process of conversion. In some limited versions of implementation methods include use of non-thermal plasma. Neteplovuyu plasma is used for reform light gases, T. E. for production of syngas (ng and with), radicals, electrons of high energy or mixture of two or more of these components. In some versions of implementation, reactive intermediate products, formed in plasma, are converted directly to produce molecules of hydrocarbon fuel. Such versions providing quick transmission of withdrawn gases in initial liquid fuel, such as diesel fuel or other suitable hydrocarbon liquid st. Advantage of specific embodiment is presence of free radicals, which are korotkozhivushchimi, and their interaction with initial liquid fuel (for example, in some versions of implementation, with oil or biozhidkostyu) for hydrogenation of compounds, present in initial liquid fuel, so, is formation of molecules with more short chain. In some versions of implementation application reactor non-thermal plasma has the advantage, depicting in maximization of electrons density in reaction space.

[0024] in some versions of implementation methods, discovered in this description, lead to WiFi client continuously agreed to content of polycyclic aromatic compounds and total amount of aromatic compounds in hybrid fuel. For example, in some versions of implementation concentration of polyaromatic compounds, in methods, disclosed in this description, is less than approximately 5 wt.%, less than approximately 3 wt.%, less than approximately 2 wt.% or less approximately 1 wt.%, less than approximately 0.1 wt. %. In some versions of implementation concentration of aromatic compounds, in methods, disclosed in this description, is less than approximately 35 wt.%, less than approximately 30 wt.%, less than approximately 25 wt.% or less approximately 20 wt. %. In some versions of implementation methods, discovered in this description, is brought to at least fold, trekhkratnomu, five times or desyatikratnomu WiFi client continuously agreed to polyaromatic compounds as compared with by common methods. In addition, methods, discovered in this description, lead to increases the volume of fuel product, as compared with by common methods treatment of fuel. Respectively, methods, discovered in this description, is modified molecular components, that leads to hybrid fuel, which is relatively completely sgorayushchim and has low level of emissions greenhouse gases and small particles smoke. In addition, methods, discovered in this description, lead to production of fuel with low level of viscosity and pour point.

[0025] in the versions, disclosed in this description, light gas includes, without limiting, methane, ethane, butane, GES, Ngo and h2s.

[0026] in some versions of implementation biogas, used in methods, disclosed in this description, contains up to approximately 40% GES. In some versions of implementation, methods can be used for treatment of heavy oil (for example, oil with high content of sulfur) for WiFi client continuously ny viscosity. Final products methods, disclosed in this description, include furnace fuel oil, diesel fuel, fuel (gasoline), marine fuel and fuel for jet engines.

[0027] in another aspect, there are disclosed methods of reforming of methane and other lower hydrocarbons using free radicals. In some versions of implementation, thermal reforming has the advantage of producing reaction products, which contain relatively low levels of aromatic compounds and polycyclic aromatic compounds. In specific versions of, methods, discovered in this description, lead to promote reduced formation of aromatic compounds and polycyclic aromatic compounds as compared with by common methods. In some limited versions, generation of free radicals due to using non-thermal plasma.

[0028] in one aspect of the present invention a method of preparing hybrid fuel. Method includes stages of combination of biofuel mixture emulsion and liquid fuel product with formation of hybrid fuel. Optionally, hybrid fuel can be combined with water by water - in - oil. Additionally, and optionally, hybrid fuel can be combined with oxygen additives and complexes additives.

[0029] in another aspect of the present invention method of producing biofuel emulsion involves combining oil and alcohol, and optionally emulsifier. Mixture is subjected high-pressure, and then is passed through expansion chamber, which homogenise mixture. Then mixture, at least, partially is oxidized, to produce the biofuel emulsion.

[0030] in one more aspect of the present invention method of producing liquid fuel product involves combining of light gas and initial liquid fuel and, optionally, water, catalyst and emulsifier in mixture. Mixture is subjected to interaction in body reactor for production of, at least, one modified fuel product in the form of steam. Method can optionally include interaction of modified fuel product in the form of steam in gas-phase catalytic reactor, and condensation of vaporous product in form of liquid fuel product.

[0031] in another aspect of the present invention invention proposes hybrid fuel. Versions of hybrid fuel include mixtures of biofuel emulsions and liquid fuel products. Hybrid fuel can also be merged with water, oxygen and other additives complexes additives.

[0032] in one of the aspects, in the method, described in this document, there are formed free radicals as a result supercritical reaction homogenizer, so, are formed ethyl esters of fatty acids (FAEE) and similar products glycerol, formed by common methods treatment of biodiesel fuel. Glycerol can be removed and processed in ethers of glycerol, glycerol ethers then may be added to emulsion for the, to lower chilling temperature and to reduce viscosity product.

[0033] not wishing to be connected a certain theory, the authors of rate, that the described here methods for preparing of hybrid types of fuel, including biofuels, energy are rational. In addition, test results are demonstrated total WiFi client continuously tracks the density of hybrid fuel mixture, which is the proof of proof of advantages of hydrogenation of aromatic compounds to hydrocarbons (T. E. in method undesirable aromatic compounds then successfully converted into applicable fuel margin).

[0034] in one of the aspects disclosed is a method of producing raw material. Method includes: supply of carbon-containing raw material in reactor hydro metanizatsii; and the interaction of carbon-containing raw material in the presence of catalyst and steam to produce multiple gases. In some versions of implementation carbon-containing raw material is a coal, biomass, petroleum coke or their mixture. In some versions of implementation catalyst is alkali metal. In some versions of implementation stage interaction is at nnoi to increase the temperature, pressure, or both these conditions.

[0035] for more full understanding of various embodiment of the present invention, move assortment of the following description together with accompanying graphic materials, where:

[0036] on figure 1 is presented integrated method of preparing hybrid fuel according to one of versions of the present invention.

[0037] on figure 2 the inventive method for producing biofuel emulsion according to one of versions of the present invention.

[0038] on figure behind is presented method of producing liquid fuel product according to one of versions of the present invention.

[0039] on figure of members is presented method of producing liquid fuel product according to one of versions of the present invention.

[0040] on figure 4 is presented additional method of preparing hybrid fuel according to one of versions of the present invention.

[0041] on figure 5 the inventive method for producing product of mixture of water and oil according to one of versions of the present invention.

[0042] on figure 6 is presented method of mixing complex additives.

[0043] on figure 7 the inventive method for producing initial types of raw materials of hybrid fuel from heavy types of oil according to one of versions of the present invention.

[0044] on figure 8 is presented additional method of producing initial types of raw materials of hybrid fuel from carbon-containing materials according to one of versions of the present invention.

[0045] on figure 9a is presented configuration reactor for production of liquid fuel product according to one of versions of the present invention.

[0046] on figure 0.9B is presented configuration reactor for production of liquid fuel product according to one of versions of the present invention.

[0047] on figure 9C is presented configuration reactor for production of liquid fuel product according to one of versions of the present invention.

[0048] on figure 9d is presented configuration reactor for production of liquid fuel product according to one of versions of the present invention.

[0049] term "biogas", used in this description, includes any neinertnyi gas, which can be is obtained by biological decomposition of organic substance. Limiting examples biogas are hydrogen, methane and carbon oxide. Biogases, in a context of this description, also include other gaseous products on base of oil, such as ethane and ethylene, as well as products of decomposition of agricultural wastes, such as wood chips, grain, grass, leaves and the like. Term "biogas", also in a context of this description, includes the same gases, obtained from other sources. One of examples is methane, connected with coal, widely known as "methane coal seams", "methane coal mines" and "methane abandoned mines". In some versions of implementation such methane is produced by bacterial activity or at heating.

[0050] term "natural gas", used in this description, is intended for designations of accumulation of substances, which are formed mainly methane, but also can include ethane, propane, butane and pentane. Composition of natural gas may be changed (for example, changes from approximately 70% to 100% or from approximately 70% to approximately 90% methane, approximately from 5% to 15% ethane, and up to approximately 5% or up to approximately to 20% propane or butane, separately or together), and may include carbon dioxide, oxygen, water, nitrogen, hydrogen sulfide, inert gases (for example, argon, helium, neon and xenon).

[0051] term "light gas", used in this description, is intended for designations gases, including carbon dioxide and hydrocarbons, containing at least two carbon atoms, such as methane, ethane, propane, ethanol, methanol, and mixture of two or more of them. In some versions of implementation, also is connected water.

[0052] term "biofuels", used in this description, as a rule, relates to liquid fuel, which is produced from animals, plants and/or biological materials.

[0053] according to one the present invention, invention proposes hybrid fuel and methods of its synthesis. Term "hybrid fuel", used in this description, as a rule, relates to any of multiple possible compositions fuel or mixtures, including alternative "the drop-In of" fuel formations, in which used is one or more easily available light gas (below described is more specifically), hydrocarbon fractions, biofuels, water and different complexes additives. In some versions of implementation hybrid types of fuel include fuel product, obtained at combining of light gas and initial liquid fuel (for example, natural gas and diesel fuel). Alternative "the drop-In of" fuel is interchangeable and compatible with traditional fuel and replaces its. Alternative "the drop-In of" fuel does not require adaptation system heating, burner system, engine or system of jet fuel or modification of network distribution of fuel, in which it is used.

Alternative "the drop-In of" fuel can be used "as there is" or can be combined with usual fuel, changing alternative "the drop-In of" fuel.

[0054] "electrons of high energy", used in this description, field elektronam, having to increase the nnuyu electron energy, so that, they can receive participate in decomposition of gaseous molecules (for example, decomposition of methane or natural gas by dissociation or ionization). High-energy electrons are part of methods, disclosed in this description (including without limiting application of non-thermal plasma), which allow take place otherwise thermodynamically unfavorable reactions. In some limited versions electrons of high energy electron energy have approximately 1 - 10 eV, or more than approximately 5 eV, or more than approximately 6.5 eV or even more than approximately 10 eV. In some versions of implementation sufficient amount of electrons high energy or high energetic electrons, bound with phenomenon, called electronic flooded, in which are generated secondary electrons. In certain situations, character of fragmentation on radicals, formed from methane, partially depends on function of distribution of electrons according to their energy (EEDF).

[0055] versions methods of producing hybrid kinds of fuel, are flexible, fully integrated and can be easily adapted to existing under hand starting raw material, and also adapted to a desired type of hybrid fuel. For example, versions of realising the method can be adapted for producing the drop-In of substitutions of any of one or more fuel, diesel fuel, fuel, marine fuel and fuel for the jet engines (for example, Jet to a of, Jp of-and-8, Jp of-and-5 and T. d.). Similar manner, versions of realising the method can be adapted with the possibility of use of different types of initial raw material, such as, vegetable oils, animal fats, alcohols, natural gas, GES, heavy oil, diesel fuel, fuel vehicles and products gasification of biomass, coal, coke and other materials. Integrated methods, discovered in this description, provide flexible operation, which maximize storage economic indices of fuel store and meet the requirements of multiple applications of fuel, including heating, transportation (for example, vehicles, ship, jet engines and T. d.). Methods, discovered in this description, can be used to greater number of places, including to remote places with limited amount of natural gas reserves of gas, and also are useful at movement of equipment on truck or barge. Moreover, methods, have relative to low energy consumption (for example, water) and include relatively low capital costs on realization of.

[0056] as mentioned above and more specifically described below, versions of the present invention provide high integrated methods of preparing hybrid fuel. High integrated plant is less sensitive to cost and availability of the raw material, since many types of initial raw material for separate methods are "internal supply". That is, primary or by-products of one subprocess are used in other podprotsessakh. So, lesser amount of initial raw material it is necessary to supply from outside, that reduces total idea about unstable supply raw material.

[0057] in addition, method efficiency as a whole is amplified by high-integration method. High flexibility of integrated method allows to change order of treatment of subprocesses, so as to adapt available initial raw material and desired hybrid fuel products. Similar manner, method can be adapt to changes demand and correspondence of tapped of economically profitable product by production of alternative of hybrid fuel products. Ecological characteristics also improved, so as by-products some subprocesses, requiring utilization of, can be used as raw material for other subprocesses. It also decreases operation, since costs of recycling excluded, as well as themselves cost initial materials. Additionally, in many cases, capital costs on the whole integrated installation below, than if separate subprocesses have been postro enes independently from each other. Similar manner, transport consumption, which would have the place from - the delivery of materials from one subprocess to other, in integrated process of deleted.

[0058] in one of the aspects, methods, discovered in this description, include formation of free radicals from light gases and field free radicals in subsequent methods of producing hybrid kinds of fuel. Methods, discovered in this description, show advantages as compared with by common methods, which require two separate stages the first stage separation of light gas, and the second, subsequent stage, repeated creation of free radicals at high temperatures and pressure, for, to initiate further step of the method. Methods, discovered in this description, is limited demand in these two separate stages, thus providing considerable advantages (for example, lower power consumption) for oil refining company and consumer. In examples of realisation, disclosed in this description, free radicals, generated on the initial stage, is used directly in methods of processing oil and other fuel liquid posts. In addition, free radicals are accessible for use in other methods. Methods, discovered in this description, include being brought (T. E. short-) contact with free radicals vapor phase and subsequently initial liquid fuel (for example, liquid st or liquid phase oil) for the time of existence of free radicals.

[0059] in another aspect, free radicals, containing carbon, hydrogen, oxygen or mixture of two or more of carbon, hydrogen and oxygen, are created in methods of reforming light gases. In some versions of implementation thermal reforming is dry thermal reforming (CO2 + CH4), steam thermal reforming, partial oxidation or formation of methyl radicals. In some versions of implementation method of reforming light gases is carried out in presence of non-heat (nonequilibrium) plasma. In some versions of implementation, method of reforming light gases, using neteplovuyu plasma, is carried out at atmospheric pressure. In other versions, method of reforming light gases, using neteplovuyu plasma, is carried out at pressure above atmospheric. For example, in some versions of implementation method is carried out at pressure in the range from approximately 0.1 atm to approximately 5 atm. In some versions of implementation method is carried out at pressure to approximately 5 atm. In some versions of implementation method is carried out at pressure of about 100 mm Hg. CT. In other versions the method of reforming is carried out at conditions of high shear force, caused by ultrasonic excitation, rotating disks, homogenization, sources of UV - radiation, radiation or combination of two or more of these methods. In some versions of implementation, radiation is a electronic radiation or radiation particles (gamma) or their combination. In one version radiation source is thorium.

[0060] at normal methods with application of high temperatures and high-pressure, there are formed free radicals in the process of reforming. In the formula of invention is disclosed, that free radicals may be formed by with application of non-thermal (nonequilibrium) plasma. Power consumption spider nnoe. Similar manner, subsequent hydro cleaning liquid posts, the prevailing at high temperatures, results in the formation of free radicals, leading to chain reaction. In the formula of invention is disclosed, that this returns singaz with free radicals back to neutral, and then recreates energetically ineffective state free radicals. In method is used free radicals, formed by with plasma, to cause long-chain reaction. In addition, methods using neteplovogo reactor similar manner is returned singaz or metilnyi radical back to normal state.

[0061] in some versions of implementation, methods, discovered in this description, include use of catalysts. Such catalysts promote reaction conversion of gas, as well as redistribution hydrocarbons. Examples catalysts include, without limiting, metals, nanosfery, wire, catalysts on carrier and soluble catalysts. For example, as used in this description, "nanosfera" or "nanokatalizator" invention relates to catalyst, where average diameter of catalyst is from 1 nm to 1 mcm. In some versions of implementation catalyst is soluble in oil catalyst (also known as nanokatalizatory). Such catalysts well diverge and not precipitate in the process of treatment of oil. In some versions of implementation the catalysts are bifunctional catalyst, for example the, which includes inorganic base and catalyst, which contains transition metal, such as iron, chromium, molybdenum or cobalt. In some versions of implementation level of catalysts in the method makes from approximately 0.03 wt.% to approximately 15 wt. %. In some versions of implementation level of catalyst is approximately 1 wt. %. In one not limits example alternatives of, concentration of soluble catalyst, introduced in reaction mixture, is approximately 50 million '¹ , or approximately 100 million '¹ , or makes from approximately 50 million '¹ to approximately 100 million '¹ liquid oil. In some versions of implementation level of catalyst is at least approximately 50 million '¹ . In some versions of implementation level of catalyst is from approximately 50 million '¹ to approximately 100 million '¹ . In some versions of implementation level of catalyst is in the range of.

[0062] in some versions of implementation catalyst is metallorganicheskoe compound. Examples of metal-organic compounds include transition metal, compound, containing transition metal, or their mixture. Typical transition metals, inserted in catalytic compounds, include catalysts, selected from the group V, VI and VIII elements of periodic table of elements. In some versions of implementation, transition metal catalyst is one or more of vanadium, molybdenum, iron, cobalt, nickel, aluminum, chromium, tungsten, manganese. In some versions of implementation catalyst is metal naftanat, etilsulfat or polymetallic anions ammonium salt. In one version catalyst is organomolibdenovyi complex (for example, MOLYVAWM 855 (R.T.Vanderbilt the COMPANY, Inc.Norwalk, conn-., the CAS Reg. No 64742 - 52 - 5), organomolibdenovyi complex organic amide, containing from approximately 7% to approximately 15% molybdenum. In another embodiment catalysts are nekhsem (MooneyChemicals, Inc., The Cleveland, Debug, containing approximately 15% 2 - mentioned above molybdenum) or bimetallic wire, chips or powder catalyst, representing h25/l605 (AltempAlloys, the Orange Calif.), which includes from approximately 50% to 51% cobalt, 20% chromium, approximately 15% tungsten, approximately 10% nickel, to approximately 3% iron and 1.5% manganese.

[0063] in additional versions other suitable catalysts include compounds, which soluble in butter, have relatively high loading of molybdenum. In some versions of implementation, catalyst gives ability of fuel, which is required for diesel fuel with above - low content of sulfur (ULSD). In some versions of implementation organometallic compound gives ability of liquid fuel product, and also serves as catalyst, which allows to avoid necessity added additional lubricating additive to final hybrid fuel product. Other organometallic compounds, which are useful for methods, disclosed in this description, are disclosed in the Patent the U.S. 7.790, 018 Khan, is Et and!. and 4.248, 720 Couplandetal.

[0064] in some versions of implementation catalyst based on transition metal is a single transition metal or combination of transition metals, or is in the form of metal salts, pure metals, or metal alloys, and in some versions of implementation its is used in combination with other metals, except transition metals. Preferred catalysts for use in this invention, are metals and metal alloys. In some versions of implementation atomic number of used transition metals is from 23 to 79; in other versions the atomic number of more used transition metals is from 24 to 74. In some versions of implementation cobalt, nickel, tungsten, iron and their combination is used as metals for catalytic compounds. Limiting example of additional metal, which can be connected, is aluminum. In some versions of implementation base transition metal (s), together with other metals, such as aluminum, iron supports frame. In some versions of implementation iron frame is a basket or bed. In some versions of implementation catalyst is applied on the surface of the electrode. Different shapes iron can be used as material frame. Limiting examples are pig iron, grey cast iron and malleable cast iron. In some versions of implementation metal coils is maintained at iron frame in the form of open grid network. For example, in some versions of implementation, casting gray cast iron include, for example, common carbon from 2.75 to 4.00%; silicon from 0.75 to 3.00%; manganese from 0.25 to 1.50%;

sulfur from 0.02 to 0.20%; and phosphorus from 0.02 to 0.75%. In addition, in some versions of implementation one or more of the following alloying elements are present in different amounts: molybdenum, copper, nickel, vanadium, titanium, tin, antimony and chromium. In some versions of implementation nitrogen, as a rule, is present in the range from approximately 20 to approximately 92 million '¹ .

[0065] rate and degree of chemical reactions are limited by laws kinetics and thermodynamics. Reaction rate depends on many factors, including time, temperature and pressure. In case of catalyzed reactions that additional limiting factor in the form of speed contact time reagents with catalyst, and also time for removing proreagirovavshikh products with catalyst surface, to use catalyst for of catalytic of subsequent reagents.

[0066] in some versions of implementation, method of merging of light gas with initial liquid fuel is carried out at temperature from approximately 100 theoretically to approximately 850 theoretically. In some versions of implementation method is carried out at room temperature. In some versions of implementation method is carried out at temperature from approximately 200 theoretically to approximately 500 theoretically, or approximately from 500 theoretically to approximately 700 theoretically, or from approximately 700 theoretically to 850 theoretically. In other versions, method is carried out at temperature from approximately 300 theoretically to approximately 500 theoretically. In some versions of implementation gases and initial liquid fuel is heated. Temperature is regulated so, to help reaktsionnomu process.

[0067] in some versions of implementation method is carried out at pressure higher than 1 atm. In some versions of implementation method is carried out at atmospheric pressure. In some versions of implementation method is carried out at excessive pressure, components of from approximately 0.1 atm to approximately 5 atm. In some versions of implementation method is performed at pressure of not more than approximately 5 atm. In some versions of implementation (for example, mikroplazmennye reactors) method is performed at pressure of approximately to 100 mm Hg. CT. In some versions of implementation value of pressure makes from approximately 1200 pounds per square inch (8274 kPa) to approximately 3000 pounds per square inch (20680 kPa).

[0068] in some versions of implementation method of producing biofuel from combination of light gas and initial liquid fuel is a method, passing in phase of liquid st/of gas or vapor/gas.

[0069] in some versions of implementation device for reforming of natural gas or for production of biofuel is a reactor non-thermal plasma. Limiting examples reactors non-thermal plasma include sliding arc, vortex arc, distributed discharge, micro-channel discharge and dielectric barrier. In some versions of implementation device or the reactor includes radiation source. Typical radiation sources include, without limiting, thorium. In some versions of implementation device or the reactor includes slightly accurate materials for acceleration of electrons flow. In some versions of implementation of the present invention device or the reactor includes magnetic field.

[0070] device for production of free radicals includes, without limiting, non-thermal plasma reactors, reactors with high force shift, electronic or reactors beam of particles and hybrid system. Reactors non-thermal plasma include those, in which electrons provide effective activation and free radicals are formed at relatively low temperatures. In some versions of implementation is used reactors non-thermal plasma, and external electric source for creating electric fields. Applied voltage, in some versions of implementation, is a direct current, while in other versions it is high frequency. Typical reactors non-thermal plasma include, without limiting, reactor with sliding by arc discharge, mikroplazmennye generators, homogenizers, reactors with high force shift. In additional limited versions reactors non-thermal plasma include vortex generators, mikroplazmennye generators, rotating disk by centrifugation with high frequency, microwave furnace and sound activation. Limiting examples reactors with high force shift are reactors homogenizers, ultrasonic reactors, cavitation reactors, smeshivayushchie device high-energy, as well as catalytic reactors centrifugation. Typical electronic or generators beam of particles free radicals include, without limiting, electronic oscillators of high energy and radioactive sources. For example, in one version, radioactive source is a material, which generates alpha - particles, such as thorium.

[0071] in some versions of implementation reactors are mikroplazmennye reactors. Microplasma are plasma reactors in submillimetrovoi geometry. They have high electron density and relative to high part of electrons of high energy (more than 20 eV), which theoretically are capable of effectively start chemical reaction. Mikroplazmennye reactors, used in this description, operate with non-thermal plasma and energizing with application of or direct source of energy, or pulse current (less than 80 kHz). In one specific version of realisation of device is a discharge tube with hollow cathode (MHCD) with elongated recess.

[0072] application microplasma technology for creating radicals by reforming natural gas increased density of electrons and free radicals, that theoretically should to increase of total efficiency. Plasma, limited by at least one size of 1 mm or less, is determined as microplasma. Microplasma have much higher power density (more than 1 kW/cm³ ), higher density of electrons (more than 10¹⁵ cm '³ ) and enlarged ratio of surface to volume as compared to ordinary, large extensive plazmokhimicheskimi systems. High ratio of surface to volume gives excellent control of temperature conditions of and smeshivayushchie characteristics, which help maintain homogeneity, isothermal volumes, engage in reaction. These characteristics microplasma are technological advantages for use of reforming of hydrocarbons. For realization of the method at pressure, close to atmospheric, reduces to minimum requirements to equipment and simplifies common working circuit.

[0073] in ordinary reactors, time of contact reagent and catalyst frequently is controlled by mixing, that provides contact between components, participating in chemical reaction. Exist different innovation, directed on maximum field mixing and mixing devices for acceleration of chemical reactions. High shift and high energy mixing device have been proposed for ny to increase the rate of chemical reactions. Exist and other device, proposed for acceleration of reaction of chemical reagents. For example, hydro dynamic cavitation has been proposed as method acceleration of chemical reactions. Hydro dynamic cavitation entails behind a change of phase of and fast increase of temperature and pressure; pressure change, caused by the change of speed coming liquid STI, leads to accelerated chemical reaction.

[0074] as a whole, reactor with high force shift also called emulsifying mixer, dispersion mixer or sound unit. A specific realization of the reactor and method includes consideration, among other things, value, cost, quality and quantity of raw material. Reactors homogenizers are one of types of configurations, suitable for methods, disclosed in this description.

[0075] not wishing to be limited to specific theory, accepted, that level or degree of high-shear force is sufficient to increase rate of mass transfer and can to create localized, neidealnye conditions, which allow reaction flow, which should not be expect in other case, based on calculations free energy phenomenon. Localized, neidealnye conditions, as accepted, are within device with high force shift, which leads to to increase the nnym temperatures and pressure, with the most considerable increase, as accepted, localized pressure. Ny to increase the values of pressure and temperature inside the device with high force shift are instantaneous and localised, and they quickly returned to normal or averaging conditions system, after extraction from device with high force shift. In some cases mixer with high force shift causes cavitation sufficient intensity for dissociation of one or more reagents on free radicals, which can capable chemical reaction or allow reaction flow at less rigid conditions, than can require in another case. Cavitation may also increase pace transfer processes, creating local turbulence and microcirculation liquid STI (acoustic for). View application cavitation phenomena in chemical/physical methods of treatment of is presented in Gogate is Et a of!., "Cavitation: a of the Technology of an of The Horizon Solo," The Current The Science 91 (No 1): 35 - 46 (2006). Device with high force shift some embodiment presented system and methods, are operated at cavitation conditions, which, as accepted, are effective dissociation reagents for optimization of reactions. In some cases these conditions are effective for mechanical grinding and/or extracting hydrocarbons. In addition, conditions can be efficient for mechanical homogenization hydrocarbon chains for production of liquid hydrocarbon products.

[0076] in some versions of implementation, speed tip and, therefore, speed of shift, are an important factor in achieving thin microemulsion. In one specific version of realisation of the Super DISPAX Lucinda combines a extremely high speeds of force shift with a thin geometry generator for generation of high-energy scattering. From - the high speeds of tip, sufficiently the whole two stages for achieving desired results. In some versions of implementation achieved speed tip considerably exceeds 10000 FT/min (50.8 m/with).

[0077] device with high force shift (HSD), such, as mixers with high force shift and mill with high force shift, as a rule, are grouped classes, based on their ability mixed liquid STI. Mixing this method of reducing size in homogeneous types or particles in liquid STI. One criterion or degree of meticulousness mixing is power density per unit volume, which mixing device generates for splitting liquid STI. Differentiate classes, based on the supplied energy density. Exist three class industrial mixers, having sufficient power density for successive of producing mixture or emulsion, where size of particles or bubbles is from 0 to 50 mcm.

[0078] gomogenizatsionnye valve system, as a rule, classified as energy intensive device. Liquid st for treatment of is pumped under very high pressure through narrow gap valve in lower medium under pressure. Gradients of pressure on valve and the obtained turbulence and cavitation act so, that any particles in liquid STI degrade. In some versions of implementation data valve system are particles with average size from approximately 0.01 mcm to approximately 1 mcm. On the other end of spectrum are system mixers with high force shift, classified as a device with low energy consumption. These system, as a rule, have blades or rotors for liquid STI, which rotate at high speed in tank for treatment of liquid STI, which in many from the most applications is a food product. Data system, as a rule, is used, when size of particles, globule, or bladder is more than 20 micron, permissible in treated liquid STI.

[0079] in some versions of implementation reactors non-thermal plasma, heterogeneous medium heavy hydrocarbon with the hydrogen gas (for example, singazom) in chamber is exposed to, as electron beam, so field and field of electric discharge, so, to create thermal nonequilibrium, and also spatially heterogeneous state of given medium. Such double action allows to carry out cracking without high temperature and high-pressure, that, as a rule, is required, consequently, so, reduced power consumption and impurities, generated together with desired product output.

[0080] in other versions, not podderzhivayushchiisya electric discharge arises due to external ionizer very high intensity, such as electron beam (preservation of the). Electric field of high intensity, superimposed on gas, which, in its turn, is exposed to the preservation of the, multiplies the number of electrons, generated as a result of preservation of the, and creates electric discharge, which generates chemically active particles. Much numeric application of these discharges in homogeneous media, well are known (for example, for actuation of the gas lasers). For example, chemical activity of electric discharge, supported preservation of the in homogeneous gas, there is disclosed Y n-Novoselov, of V of V Ryzhov, and of I Suslov // Letters of in vitro The Journal care TheoreticalPhysics, 1998. ν. 24. No 19; p. 41.

[0081] in addition, introduction of gamma - rays in zone non-thermal plasma, containing gases, is cause, as accepted, improvement of stability of plasma and promotes initiation formation of free radicals. 4 meV gamma - beams can be obtained as a result of ejection from the materials, containing thorium.

[0082] on Figure 1 is presented total circuit integrated method 100 of preparing hybrid fuel 120 according to one embodiment of the present invention. Method 100 includes various subprocesses, each of which is described more specifically below. Figure 1 is a outlinear order, in which may occur subprocesses (shown solid single lines). Nevertheless, method 100 is flexible and order of subprocesses may be changed in accordance with used initial materials and desired hybrid fuel 120. Itself on art, in some variants, one or more subprocesses can be submerged. This aspect of is dotted double lines. On Figure 1 also is presented circuit realization of the method 100 of producing alternative "the drop-In of" replacement for fuel 118, described more specifically below (it is shown solid double lines).

[0083] method 100 includes process of the biofuel emulsion 102 for producing biofuel product emulsion (as described more specifically below), and process liquid fuel 104 for producing liquid fuel product (as described more specifically below). Method 100 also includes the process of mixing 106, where liquid fuel product mixed with the biofuel emulsion. Method 100 additionally includes the process of mixing water/fuel 108 for creation of emulsion of water and oil, based on use of biofuel emulsion, liquid fuel and/or mixture of two products. Method 100 additionally includes the process of mixing oxygen-containing additives 110 for additional oxygen enrichment of of any of intermediate products, obtained in the method 100. Method 100 also includes the process of mixing additives complex 112 for addition of various complexes additives in accordance with used raw material and/or desired hybrid fuel 120. Complexes additives are described more specifically below.

[0084] as mentioned above, circuit realization of the method 100 includes method 114 of preparing product fuel 118. In one version product process biofuel emulsion 102 directly is used as product fuel 118. In another embodiment (not shown), from approximately 5% to 20%, or in some versions of implementation approximately 10% biofuel emulsion mixed with diesel fuel on oil base, to produce fuel for vehicles. In one more version livestock emulsion is introduced at complex mixing additives 116 for production of fuel 118. The process of mixing complex additives 116 can be identical to process 112; it shown separately for clarity circuit. Additionally, intermediate product biofuel emulsion process 102 and intermediate liquid fuel product process 104 can be combined in mixing 106, then additionally are combined with water at performing process 108, before combining with complex additives during process 116, for production of product fuel 118. As mentioned above, method 114 is only illustration flexibility of integrated method 100 and other combination subprocesses are within volume of the present invention.

[0085] on Figure 2 is presented total circuit method biofuel emulsion 200. In some versions of the integrated method 100, method 200 may be used as biofuel process emulsion 102. In the method 200 is fed oil 202, emulsifier 204 and alcohol 206 in centrifugal compressor 208, which performs some mixing of raw material and increases pressure mixture for supply to reactor 210. In some variants, reactor 210 is a reactor in supercritical state, in which mixture is subjected to high pressure (for example, up to approximately 8000 pounds per square inch (55160 kPa)). Intermediate product from reactor 210 then is fed into the expansion chamber 212. In expansion chamber pressure mixture reduced, so as mixture is loaded on plate, to provide high degree of mixing and homogenization, and as a result of components of the mixture will be are divided into small particles (in some versions of implementation approximately hundreds nanometers), which facilitates formation of stable emulsion.

[0086] in some alternative versions, ethyl esters of fatty acids (FAEE) and glycerol 224 are formed as by-products of the method 200. In some versions of implementation glycerol is additionally treated glikolefirami, which can be returned to back to method 200 as additive (for example, 218). Glikolefiry is used as additive for WiFi client continuously ny viscosity and chilling temperature biofuel obtained emulsion 222. Theoretically, action of supercritical pressure from reactor 210 and fast expansion creates high force shift, which results to formation of free radicals, which are then take part in forming FAEE and glycerin. Respectively, types of fuel, containing FAEE and glycerol, is increased calorific capacity. In addition, switching aqueous ethanol in fuel, described herein, allows existence of stable water in product and additional content of water.

[0087] thermopolymer of intermediate product is passed through oxidation reactor 214. In some variants, oxygen-containing gas is passed through thermopolymer of intermediate product, which can, optionally, appear at to increase the nnykh temperatures. The accepted, components emulsified intermediate products oxidized (for example, ethanol). By oxidation of, at least, part of emulsified intermediate product, reactor 214 raises temperature of ignition final biofuel emulsion 222. Oxidized intermediate product may be unpaid in storage chamber 216 for treatment of complex additives 218 by means of total mixer 220 with production of the product emulsion biofuel 222. Complex addition of additives is optional and can be lowered in some variants. In some versions of implementation complex additives includes stabilizers oxidation for reducing speed decomposition of biofuel, produced from nemineralnoi crude oil. As was indicated above, in some versions of implementation complex additives also includes glikolefiry.

[0088] in some versions of implementation oil 202, used as raw material for method of 200, includes vegetable oils, animal fats and/or oil, obtained by pyrolysis of hydro silicate (for example, thermal depolymerization). So, represented examples sources include ryzhiki, palm, soya are fried, corn, rape, yatrofu and animal fats and wastes from various livestock farming activity. In some versions of implementation alcohol 206 represents any of mono -, di -, three, much nuclear alcohols, and/or alcohol from C1 to C4. At the same time, examples emulsifiers 204 include, without limitation, any from one or more different types of surface - active substances, such as nonionic, ionic or partially ionic, anionic, amphoteric, cationic and zwitterion surface - active substances. For example, any of surface - active substances, given in the U.S. patent 2010/0037513, entitled BiofuelComposition and sort the Method care Producing a of Biofuel, filed before the 18 September 2009 (is connected as references in this description), can be used as emulsifier 204.

[0089] in one exemplary version of method 100, methods, discovered patent in the U.S. 2009/0185963, entitled The Method for Laptops MakingDieselFuelAdditive, filed before the 22 January 2009 (is connected as references in this description), is used for method 200.

[0090] in other exemplary version of method 100, methods, discovered patent in the U.S. 2010/0186288, entitled The Method for Laptops in production care EmulsionFuel and sort Apparatus for Laptops in production care of The Fuel, filed before the 31 August 2007 (is connected as references in this description), is used for method 200.

[0091] in one more exemplary version of method 100, methods, discovered patent in the U.S. 4.526, 586, filed before the Microemulsions The From Vegetable ECO And Sort AqueousAlcohol Hotel With 1-And-ButanolSurfactant As Of AlternativeFuel For Laptops Diesel Engines Signifies, filed before the 24 September 1982, (is connected as references in this description), is used for method 200.

[0092] on fig. Is presented the total circuit method 300 of producing liquid fuel product 328. In some versions of the integrated method 100, method 300 may be used as process liquid fuel 104. Light gas 302 and initial liquid fuel 304 is fed by means of pump and/or compressor 306 through ejector 308 in reactor body 310 (shown solid lines). Optionally, light gas 302 and initial liquid fuel 304 can be delivered together with water 308 (which can be treated, to have negative oxidation/potential (oxidation) in the interval from approximately -100 eV to approximately -500 eV), catalyst 311, and/or emulsifier 312 pump/compressor 306 (shown double lines) through homogenizer 313. In some versions of realization of air also is added by means of pump/compressor 306. Pump/compressor 306 and/or homogenizer 313 increases homogeneity of mixture before its transmission through ejector 308. Pump/compressor 306 can include centrifugal pump with high rate of shift, which helps to reduce drop size of separate mixture components. In addition, ejector 308 helps in production of small bubbles and/or liquid droplets (depending on phase component), that increases reaction capacity of mixture components due to increase of total contact between components.

[0093] although this and is not indicated, all components are, which can be raw material in homogenizer 313 can be fluoric directly to pump 306, while supply of initial liquid fuel 304 is through homogenizer 313 before feeding pump 306. In such version, homogenizer breaks initial liquid fuel 304 (which may include, for example, heavy oil, bitumen, and/or other high viscous components are) on small drops, that of reaction capacity of initial liquid fuel 304 (by, for example, increase in surface area to mass). In alternative version initial liquid fuel 304 can be preliminarily processed by method (not shown), which breaks initial liquid fuel, as soon as that described above. Suitable methods for breaking of drops on high viscous raw material include methods of, discovered in the U.S. Patent 2010/0101978, entitled Flow that-Through Module Cavitation-and-Assisted the Rapid Modification care Crude ECO, filed before the 26 October, 2009 year, Kentucky 2400188, entitled The Method And Sort The Device For Laptops ResonanceExcitation Care Fluids And Sort The Method And Sort The Device For Laptops FractionatingHydrocarbonLiquids, filed before the 22 March 2000 Da, and in patent the U.S. 2010/0260649, entitled Deep To The Conversion Combining Of The Demetallization And Sort Of The The Conversion Care Crudes, Residues Or-Of Heavy Oils Finished Into Emitting Liquids Hotel With The Pure Or-ImpureOxygenatedCompounds, filed before the 28 June 2010 Da (all are connected in this description as references). For relatively more of low viscosity materials of initial liquid fuel 304, industrial homogenizer can be used for breaking initial of droplets of liquid fuel 304.

[0094] reactor body 310 can be catalytic reactor with stationary layer, fluidized bed, movable layer, and also bubbling or suspension polymerisation catalytic reactor. Catalyst can be applied on zeolite, and include one transition metal or combination of transition metals in the form of metal salts, pure metals and/or metal alloy. Preferable transition metals with atomic number from 23 to 79, and more preferable transition metals with atomic number from 24 to 74. In addition, other neperekhodnye metals can be used instead of or in combination with catalysts based on transition metal (for example, aluminum). Catalysts can be in the form of balls, granules, wire, mesh, perforated plates, sticks or strips. In one exemplary version of catalytic mixture includes aluminium wire, kobaltovuyu wire (alloy, containing approximately 50% cobalt, 10% nickel, 20% chromium, 15% tungsten, 1.5% manganese and 2.5% iron), nikelevuyu wire, volframovuyu wire and pig iron granules. In another version catalyst is a wire from metal alloy. Such wire from metal alloy include, without limiting, transition metals, the described, including, without limiting, molibdenorganicheskie catalysts. Catalysts can be arranged in fixed or fluidized bed, in combination with distributing manifoldami gas and liquid STI, inside the body 310. Moreover, screens from wire mesh (made from catalytic or other materials) can be used in limits of housing reactor 310 for starting interaction between gaseous reagents and catalysts.

[0095] during method, reactor body 310 and its content is maintained at temperature above ambient temperature and, as a rule, lower than boiling point or decomposition temperature of liquid phase of reaction mixture. Body 310 is heated by any of known methods heating reaction bodies, for example, internal or external inductive heater, steam jacket and T. d. Reaction usually is carried out at or within two atmospheres above pressure.

[0096] in some variants, reactor body 310 includes or allows creation of activating energy source for rupture with - and/or with - H bonds in Ventilation and/or other components of natural gas. Activating energy source may include radiation from microwave oven, infrared port or other sources. In one embodiment nonthermal plasma is activating energy source in accordance with methods, set forth in the U.S. patent 7.494, 574, entitled For Laptops Methods From The Natural Gas To And Sort Of Heavy Hydrocarbon Of Co-The Conversion, filed before the 3 February 2005 Da (is connected in this description as references).

[0097] in other versions of, wire or other point sources of media is placed inside reactor body 310 (which can include catalytic materials), so that bubbles and/or liquid STI take place through electric field, creating medium, and potentials voltage in liquid and gas phases in reactor. So, distance between wires, particles and/or plates leads to the production of energy for activation of methane and other reagents in bubbles of junctions in proximity of catalyst. Field electrostatic voltage, generated by passing bubbles and/or liquid styami in much phase turbulent flow, so, provides activating energy, applicable for conducting reactions. In one embodiment, methods, discovered in the Two Phase Of Streaming Potentials (S.S.Marsen, PET With. Eng. The dept ., hotel Stanford University of; μ is. w Wheatall, ARCO the International) (is connected in the present description as references), can be widened and are used in reactor body 310 for achievement of required electrostatic voltage for activation of reagents.

[0098] in other versions of, sound energy can be used as source of activating energy. Such energy can include subsonic, ultrasonic and/or sound energy in the audio range.

[0099] in some versions of implementation, oxygen and/or air include light gas 302 or separately is fed into body reactor 310 (separate raw material is not indicated). In these versions reactor body 310 is adjusted, and reaction conditions is adjusted for production of organic oxygen-containing compounds and/or synthetic gas from oxygen and natural gas components in accordance with methods, set forth in Of Oxygen Pathways and sort of carbon Dioxide tcam utilization of in vitro Methane the PARTIAL Oxidization of in vitro the Ambient temperature going of Electric Discharges (Prosthetic w Larkin, τ. a. The Caldwell, l l Laban, and R. g Mallinson; the Energy & Fuels 1998, 12, 740 - 744) and/or The PARTIAL Oxidation care Methane Hotel With the AIR for Laptops Gas to Synthesis in production in vitro of a MultistageGliding the Arc Discharge the System (Τ. Sreethawong, P. Thakonpatthanakun, S Chavadej; Chulalongkorn University Of;

accessible online 12 September 2006 Da) (are connected in this description as references).

[0100] gaseous product of reaction is extracted from free space reactor vessel 310 and is fed through gas-phase catalytic reactor 314. In some versions of implementation reactor 314 has the same type of catalyst, used in reactor body 310. In reactor 314 is completed reaction (and) between any neproreagirovavshimi components, which can be transferred from free space body 314. Reactor outlet 314 passes through heat exchanger 316, including cooling circuit 318, for condensation of at least, part of reaction product formation. Heat exchanger 316 and cooling circuit 318 have such sizes, to condense of cooling vaporous product, produced in time reactions, and some of formed compounds can to return and/or quickly biodegrade in gas phase and/or at to increase the nnykh temperatures. Fast cooling is preferable for cooling of products.

[0101] condensed product and other pairs of pass in accumulating body 320. Pair in free space 322 storage body 320 recycled back to reactor body 310 by means of pump/compressor 324 and ejector 326, which may be the same, or just, as described above. At the same time, condensate in accumulating body 320 contains liquid fuel product 328. Reaction by-products 330 can be removed from the system and additionally separated by means of separator 332. Such by-products can include heavy fractions, alkanes and sulfur compounds. Separator 332 may include filter, membrane, centrifuge, installation for distillation, column, and/or other known device for separation of liquid posts and solid substances, and also separation of various liquid fractions from each other.

[0102] in one version separator 332 is a centrifuge, which separates solid sulfur compounds from liquid components (which may include alkanes). Solid sulfur compounds is removed in the form of waste 334, and at least part of liquid components 336 is transferred to mixer 338 together with part of liquid STI from storage body 320. Mixer 338 can be any mixer, known in the given engineering, such as mixer with wetting. Mixture, produced by means of mixer 338, also can be used as liquid fuel 328.

[0103] as was indicated above, light gas 302 includes, without limiting, methane, ethane, propane, butane, pentane, hydrogen, carbon dioxide, carbon oxide, ethylene, ethanol, methanol or their combination. In some versions of implementation, to light gas water is added. In some variants, light gas 302 is activated by action on light gas 302 source of infrared radiation. In some variants radiation is a long-wave infrared region of spectrum (that is, light in the range of 3 - 8 mcm) and/or srednevolnovuyu infrared region of spectrum (that is, light in the range of 8 - 15 mcm). Nevertheless, field any wavelengths in infrared range are within volume of the present invention (for example, 0.75 - 1000 mcm). Activation of light gas, as accepted, increases energy of gas, thereby reaction characteristics of light gas 302. So, light gas 302, as accepted, more completely and/or more quickly enters in reaction with initial fed liquid fuel 304 and/or reaches reaction with more high molecular weight and/or aromatic compounds in initial liquid fuel 304. In some variants, methods, set out in the U.S. patent 7.721, 719, entitled Fuel the activation Apparatus for Laptops Methane Gas to, filed before the 16 February 2006 Da and/or the U.S. 2009/0120416, entitled FuelActivator The Using The Multiple InfraredWavelengths, filed before the 13 November 2007 Da, are used for providing activated of light gas 302 (both are connected in this description as references).

[0104] initial liquid fuel 304 may include types of fuel, obtained from fossil fuel or renewable resources. Examples include one kind or mixture of mineral oil, fuel, diesel fuel, fuel for the jet engines, rocket fuel, fuel based on residues petroleum fuel (for example, flotskoe fuel and residual types of fuel), straight-run diesel fuel, diesel fuel rack feeding mechanism, light of reprocessed oil. Initial liquid fuel 304 may also include one or mixture crude oil fractions, including products processes hydro cracking, catalytic cracking, thermal cracking, coking and/or desulfurization. Initial liquid fuel 304 may also contain light straight-run ligroin, heavy straight-run ligroin, light ligroin steam cracking, light ligroin thermal cracking, light ligroin catalytic cracking, heavy ligroin thermal cracking, a reformed ligroin, bottom ligroin, kerosene, hydro purified kerosene, atmospheric gas oil, light vacuum gas oil, heavy vacuum gas oil, residue, vacuum residue, light fuel coking, distillate coking, rich (fluid - catalytic cracking) gas oil and FCC suspension in oil product. In some versions of implementation initial liquid fuel 304 is activated by action on initial liquid fuel 304 of the infrared radiation source, as described above, for light gas 304. Field of infrared radiation for activation of material does not prevent using short-wave area for achievement of activation, for example, length waves in nanometre range.

[0105] in the versions, where light gas 302 and/or initial liquid fuel 304 is activated source of infrared radiation, infrared radiation source, may be connected in reactor body 310. In other versions, source of infrared radiation is external in relation to body of reactor 310, but above from body reactor. N1aprimer, radiation source may be is located directly below from ejector 308 and directly above from body reactor 310. In additional versions infrared radiation source is located above pump 306 and can be in any from initial materials, supplied to pump 306 (for example, initial light gas 302, initial liquid fuel 304, and/or starting material from homogenizer 313), or in any from initial materials, supplied to gomogenizatoru 313.

[0106] in another embodiment, activated light gas 302 and/or initial liquid fuel 304 is not treated in reactor body 310. Peer the whole, they are mixed after or in the activation time, and from them is obtained liquid fuel product. On fig. Of members is presented total circuit alternative method 350 of producing liquid fuel product 328. Members of the method 350, which is used jointly one and the same ssylochnye position, as members of the method 300, are the same, as described above. Possible alternative methods for arrangement of external sources of infrared radiation, shown as radiation source 352 (they correspond to arrangement of on fig. Behind, but shown on fig. Of members for ease of illustration). In one version, light gas 302 and/or liquid fuel 304 is activated, as indicated earlier (for example, above from pump 306, or below from ejector 308), mixed in pump 306 and ejected in settler 354. Liquid st from bottom of settler 352 is a product of an alternative liquid fuel 328. In the other version of source of infrared radiation is located in settler 354. In additional versions light gas 302 and liquid fuel 304, either one, or both of which may be intensified, can be simply mixed and are presented as an alternative liquid fuel product.

[0107] as mentioned above, accepted, that activation of light gas 302 and/or initial liquid fuel 304 results in the fact, materials, become more reactive, in increased reaction rate components. Supposed, that activation of materials changes stereochemistry reagents, which allows flow reactions, which would otherwise not could place. In addition, accepted, that activation reagents increases efficiency of catalysts. Also affirms, that activated reagents can be emulgirovany without emulsifier or surface - active substance. Methods and devices set out in PhotoassistedActivated care Methane by Over SupportedCatalysts Hotel With a of XenonExcimer a LAMP (Loviat, means F., ε-τη Zurich Hotel, 2009), Bonded-and-and sort the Mode Specific Reactivity care Methane of an Of λ //(100) (Maroni, p ., Ecole culinary PolytechniqueFederale the de the Lausanne, 2005), Infrared-and-Excitation for Laptops ImprovedHydrocarbonFuel's the Combustion Efficiency tool (Wey, a. The, Flandy, R g, Zheng, υ ., and sort the KIM, s., the International of SAE, 2007) (all are connected in this description as references) can be used for preparing activated reagents.

[0108] in some variants of the method 300, methods, discovered in the U.S. Patent 2009/0249682, entitled The Conversion care Biogas t the Liquid Fuels, filed before the 7 April 2008 Da, the U.S. 7.806, 947, entitled The Liquid HydrocarbonFuel the From MethaneAssisted By the Spontaneously generated is Voltage, filed before the 5 October 2010 Da, and/or the U.S. 7.897, 124, entitled 'S Continuous the Process and sort Plant specialise the Design for Laptops the Conversion care Biogas t the Liquid Fuel, filed before the 18 September 2008 Da (all are connected in this description as references), can be used to provide for liquid fuel product 328.

[0109] predict, that at certain operating conditions, method 300 provides the direct conversion of light gas 302 into liquid fuel, where some light gases, for example methane, is carried out as a source of hydrogen for ny to increase the quality of various oils and initial types of raw materials of liquid fuel. The same way, some researchers predict, that relatively more longer chain alkane (and) may be subjected to interaction with methane to form two relatively more short chains alkanes (in, with) in accordance with equation 1.

Equation 1

CH4 + S_UN2p + 2

CP - Abrasive Tools

u - and " 2 (U - and) + 2

Ca +1 Nga + 4

(AND)

(IN)

(WITH)

[0110] this catalytic reaction "methanolysis" (equation 1), as its sometimes, result actuation of methane in contact with, at least, one more initial alkane (and), U having carbon atoms with U, equal to at least 2, preferably at least 3, so, that catalytic reaction, as a rule, results in the formation of at least one of the end alkane (in) or at least two end alkanes (in, with), having carbon atoms from 2 to (U - 1) or even to value, larger, than (U - 1). This is therefore, that alkane or alkanes, appearing directly at reaction methanolysis, can receive proper participation in at least one metathesis reaction of other alkanes. Field words alkane, not excludes the applicability to other fractions, for example, aromatic hydrocarbons, alkenam and T. d.

[0111] known, that methane can be one of original species of raw material for production of synthetic liquid fuel. For example, methane and steam can be reform, for, to create hydrogen and carbon oxide. Hydrogen and carbon oxide is subjected to interaction by Fischer - Tropsch for creating liquid kinds of fuel. Nevertheless, capital costs, necessary for production of by Fischer - Tropsch, at least, on order of, than required to open the present invention method. In addition, this method on 30% is more effective, than method of Fischer - Tropsch.

[0112] in addition, by direct connection of methane (and/or other components of natural gas) to hydrocarbon and/or bio - derivatives of fractions, and/or destruction of methane in reaction of alkane - alkane, natural gas, available for use (and which otherwise can chomp at) converted into liquid fuel. In addition, method 300 decreases content of aromatic hydrocarbons, and, in particular, of polycyclic aromatic hydrocarbons (PAC) in final fuel product. PAC in diesel and in fuel for jet engines have some undesirable properties, such as very poor characteristics of ignition and cetane number of, adverse properties of cold fluidity, for tendency to formation of carbon black and very low content of hydrogen. It results in high specific outbursts of carbon dioxide from engine.

[0113] maximum level PAC, allowed in diesel fuel is adjusted in many countries, and some country offered to to reduce these limits. So, some flows of oil processing plants, which contain relative to high levels of polycyclic aromatic hydrocarbons, such, as light reprocessed gas oil from flyuidkataliticheskogo cracking or middle distillate fractions from installation coking of delayed action or from installation for coking in fluidized bed, can only be mixed in diesel fuel in limited amounts. Question content PAC in fuel intensify, when considerably larger portion of non-conventional, lean with hydrogen types of heavy oil will be treatment is in future, such as bitumen from oil-bearing sands or ultra - heavy types of oil type Orinoco. Selective hydro detsiklizatsiya PAC, the prevailing in middle distillates in hydrogen-rich fuel components with high cost fuel compounds, like a monocyclic naftenam or, preferably, alkanam, without reducing the amount of carbon, continues remain of one of main problems of heterogeneous catalysis. So, methods, in the given document, provide track application other undesirable types of initial raw material for production of fuel with low content of PAC.

[0114] additionally, versions of realising the method 300 provide fuel product, which has improved viscosity and spider nnuyu cloud point relative to beet initial liquid fuel. In the method 300 also is removed sulfur from crude initial liquid fuel.

[0115] on Figure 4 is presented method of mixing the biofuel emulsion and liquid fuel 400. In some versions of the integrated method 100, method 400 may be used as mixing process 106 biofuel emulsion and liquid fuel. Method 400 includes mixing reactor 402, in which is fed biofuel product emulsion 404 and liquid fuel product 406 for preparing hybrid fuel product 408. Biofuel product emulsion 404 and liquid fuel product 406 can be obtained by any of described above embodiment. Mixing reactor 402 can be any type of mixer (for example, mixer with wetting), corresponding to the starting raw material. In the method 400, livestock emulsion 404 mixed with liquid fuel 406 from approximately 0.5 about.% to approximately 20 about. %. Mixing biofuel with liquid fuel leads to row of mineral properties of hybrid fuel. Addition of biofuel also improves ability of fuel, also reduces viscosity obtained hybrid fuel and reduces temperature of solidification.

[0116] on Figure 5 method is 500 of producing product of mixture of water/fuel 508 (also called product water - in - oil (of W/about)). In some versions of the integrated method 100, method 500 may be used as process mixing water/fuel 108. Method 500 includes mixing reactor 502, in which water supplied to 504, fuel product 506 and, optionally, emulsifier 508 to produce mixture water/fuel 510. Fuel product 506 can be biofuel emulsion 404 and/or liquid fuel 406, as described above. Mixing reactor 502 disperses water 504 in continuous phase fuel 506.

[0117] in some variants, mixing reactor 502 includes electrolytic element, ultrasonic wave generator and converter and/or mixing device. In this case methods and devices, discovered patent in the U.S. 2010/0095580, entitled EmulsionFuel, and sort the Process and sort Apparatus for Laptops in production Thereof, filed before the 15 January 2007 Da (switched on in this description as references), is used for mixing water 504, fuel product 506 and emulsifier 508. At the same time, in other versions of is used methods and devices, discovered patent in the U.S. 2010/0122488, entitled ECO Emulsion, filed before the 4 April 2008 Da (switched on in this description as references), for formation of mixture 510. As already discussed in the given application, some ion-exchange resins and mineral substances (for example, tourmaline and silicon dioxide) is used for preliminary treatment of water, used in the method. Data materials and methods also used in versions of the present invention.

[0118] in additional alternatives, mixing reactor 502 includes device micronising, for example, any of commercial products Nanomizer production of company Nanomizer, Inc.Yokohama, Kanagawa, japan. Methods of using and additional information specified device are disclosed in the patent the U.S. 2010/0186288, entitled The Method for Laptops in production care EmulsionFuel and sort Apparatus for Laptops in production care of The Fuel, filed before the 31 August 2007 Da. In addition, commercially available surface - active substances production of company Nanomizer, Inc. (for example, NanoemerGFA-and-001) is used in some variants of the method 500 for emulsifier 508. Optional emulsifier 508 is selected based on emulgiruemoi composition fuel. Difference oil origin may affect the productivity.

[0119] in other versions, mixing reactor 502 is a reactor with high force shift, tuned for combining water 504, fuel product 506 and emulsifier 508. This may be one device or several devices, connected in series or in parallel. In general, reactor with high force shift is a mechanical device, capable to bubbles and/or drop submicron and micron-size in reaction mixture, flowing through reactor with high force shift. Reactors with high force shift mixed the reacting components mixture by particle destruction liquid STI and/or gas mixture. Reactor with high force shift may be any one or more from gomogenizatsionnykh valve systems, colloid mills and/or high speed mixers.

[0120] in gomogenizatsionnykh valve systems, liquid st, to be treated, is pumped under very high pressure through narrow gap valve in conditions with low pressure (as described above). Gradients of pressure on valve and as a result of turbulence and cavitation is divided into any particles in liquid STI. High speed mixers usually have blades, rotors, and/or cutting blades, which rotate at high speed in liquid STI to produce particles, average size of which is more than 20 micron.

[0121] at the same time, the typical structure of a colloid mill includes conical or disk rotor, which is separated from additional stator with liquid stnym cooling with the aid of tightly controlled gap rotorstatora. Usually rotors are actuated by means of electric motor direct drive or belt mechanism. When rotor rotates at high speeds, it pumps liquid st between outer surface of the rotor and the stator inner surface, and shear force, generated in the course of rupture liquid STI. Many colloidal mill with corresponding control is achieved average size of particles of 0.1 - 25 mcm in treated liquid STI. These capabilities is colloidal mill, suitable for different applications, including colloidal treatment emulsion and based on oil/water.

[0122] as indicated above, mixing reactor 502 disperses water 504 in fuel product 506, which is, as a rule, continuous phase. Suitable colloidal mill incurred, for example, companies IKA® the Works, Inc.Wilmington, N.C. and APV the North the America, Inc.Wilmington, Mass. In some variants mixing reactor 502 includes Dispax production of Lucinda® company IKA® the Works, Inc. patent in the U.S. 2009/0001316, entitled The System and sort the Process for Laptops in production care the Liquid the Product the From Emitting Gas to, supplied 17 January 2008 Da (is connected in this description as references) are disclosed system and methods of using devices with high force shift. Any of these methods and/or systems can be used in reactor used with high force shift and or any other device for mixing with high force shift, open in this document.

[0123] stability mixture 510 depends on at least partially from size of particles of water 504. Size of water particles is determined, in particular, by means of oxidation - potential (AFP) water. Purpose of the consists in, to drop size of water in the mixture 508 was 1 - 5 mcm. In some variants, water 504 is treated so, that negative oxidation water reach from approximately -100 eV to approximately -500 eV. Mixture water/fuel (i.e., emulsion), having negative oxidation water, as accepted, have to increase the nnoi efficiency (else was on 30%) as compared with one only fuel.

[0124] mixture type, open in this description, demonstrate considerable advantages at operation in engine and at heating and, as accepted, lead to reduction of emissions of greenhouse gases (pg), carbon dioxide, hydrocarbon and of no emissions_{of X} .

[0125] on fig. 6 method is 600 compounds liquid fuel 602 and oxygen-containing additive 604 in the mixing reactor 606. Liquid fuel 602 may be any from types of liquid fuel, disclosed in this description, including any versions of the biofuel emulsion, described above. Method 600 also includes mixing reactor 608 for mixing complex additives 610 for preparing hybrid fuel 612. Mixing reactors 606 and 608 can be any mixers, known professionals in the given engineering, and can include any versions mixers with wetting. Mixing reactors 606 and 608 may be single mixer. As shown on fig. 6, method 600 can include mixing of oxygen-containing additives 604 and other complexes additives 610 (shown solid lines), or additive can be submerged (it is shown dotted double lines).

[0126] in some variants, kislorodsoderzhashchaya additive 604 can include commercially accessible kislorodsoderzhashchuyu additive, such as methyl - tert - butyl ether (mvte), tertiary amilmetilovyi ether (tame) and other. In other versions of livestock emulsion 222 is used as liquid fuel 602, in which mixed alcohol serves as oxygen-containing additive, and is not required any additional oxygen-containing compounds. In additional alternatives, oxygen and/or carbon dioxide include light gas 302 in the process of producing liquid fuel product 328, and is not required in any additional oxygen-containing compounds. In such version, methods, discovered patent in the U.S. 2005/0288541, entitled Gas to t the Liquid the Conversion the Process, filed before the 2 December 2004 Da (is connected in this description as references), can be used for oxygenation of liquid fuel product 328.

[0127] in some versions of implementation, complex additives 610 may include one or more of the following additives: additive for increasing resistance to oxidation, additive for control of viscosity, corrosion inhibitor, additive for adjustment of lubricating capacity and/or additive for ny to increase the fuel cetane number. In some versions of implementation additive represents ether glycol. In some versions of implementation additive has effect WiFi client continuously ny chilling temperature of hybrid fuel 612. Specific examples additives include the following: dimethyl ether (DME), antiwear additive, as disclosed in the patent the U.S. 4.185, 594, and commercially available additive, increasing the cetane number.

[0128] as already mentioned above in the description to Figure 1, method 100 is a flexible process and above described subprocesses can be changed or submerged, depending on presence of certain initial material and/or the desired product. For example, in one embodiment of the method 100, livestock emulsion from the process 102, is subjected for interaction with natural gas in the method 300. The is considered to be, that aromatic hydrocarbons, present in the biofuel emulsion is subjected to cracking or other converted into nonaromatic compounds, which provides the possibility of more effective and ecologically pure fuel combustion as compared with a single biofuel emulsion.

[0129] on fig. 7 method is 700 of producing initial types of raw materials of hybrid fuel from heavy types of oil. As was explained above, one of the aspects of the invention consists in the fact, that common method 100 is flexible and can be completely is integrated with different methods for obtaining oil, oil processing, production of fuel and/or chemical industry. Method 700 is a illustrative an example of one possible versions of integration method 100 with by transformation in liquid STI (types of fuel, gas oil, fuel) hydrocarbons, which are solid or have high boiling temperature, otyagoshchennye metals, sulfur, deposits, by means of water or oxygen-containing gas, represented in common form, as method 702. Method 702 is described specifically in patent the U.S. 2010/0260649. As explained in it, method 702 includes preliminary heating raw material 5 in heater 8 to temperature below preset temperature reactor 10. This raw material is introduced injectors 4 in empty reactor 10 (T. E. without catalyst). Raw material is treated by gas jet or superheated steam steam from superheater 2, to activate that raw material. Jet gas may be, for example, from gas 704, which can include carbon dioxide. Activated products in raw material is stabilized at selected temperature and at selected pressure in reactor and then is passed through row of extractors 13 for separation of heavy and light hydrocarbons and demetallization of raw material. Useful products, appearing in the form of emulsions water/hydrocarbon, usually is destroyed in deemulgatore 16 with formation of water, compromised different impurities. Light phase, final containing hydrocarbons is heated in heater 98 and separated on part of normal products, in accordance with for processing in extractor 18 similarly 13.

[0130] heavy fractions of 708 from extractor 18, can be returned to in method in the form of crude material 5. in addition, heavy fraction 708 can be used as initial liquid fuel 304 in the method 300. In addition, other types heavy oil 710 and/or liquid fuel product 712, such, as any described above, can be supplied in the form of crude material 5. so, in this case, intermediate and/or final products from method 100 may be are integrated in as raw material in method 702.

[0131] in addition to integration materials, prepared by 100, in method of 702, in the versions of the present invention is integrated materials, obtained by 702 in method 100. For example, product of light gas 714 can be obtained as product from extractors 13. Product of light gas 714 can be used as initial raw material of light gas (for example, light gas 302 method 300) for any processes from liquid fuel, described in this document. In addition, oxygen-containing fuel 716 can be obtained as product from extractors 13. In some variants, oxygen-containing fuel 716 can be integrated in method 100 as replacement of biofuel emulsion 102. Similar manner, in some versions of implementation, liquid diesel fuel 718 may be used as initial liquid fuel 304 in the method 300.

[0132] on fig. 8 method is 800 of producing raw material from carbon-containing materials for use in methods of producing hybrid fuel, disclosed in this description. In the method 800, carbon-containing initial material 802, such as coal, biomass and/or petroleum coke, catalyst 804, such as alkali metal, and pairs of 806, is fed into reactor hydro metanizatsii 808. Reactor 808 generates multiple gases, including methane, by reaction of initial material in the presence of catalyst and water steam at to increase the nnykh temperatures and pressure. Small unreacted carbon-containing substance is removed from crude gaseous product by means of, for example, cyclone 810, and gases is cooled and purified in several processes 810, 812, for removing undesirable impurities and other by-products 814, including carbon oxide, hydrogen, carbon dioxide and hydrogen sulfide, to produce flow of light gas 816, which includes methane. Illustrative materials carbon-containing raw material include, without limiting, cellulose raw material (T. E. wood chips).

[0133] hydro metanizatsiya carbon-containing material to methane usually includes four separate reaction:

Pairs - Carbon: With + H₂ 0 ->WITH + H₂

Conversion of water gas: with + H₂ 0 ->H₂ - + C0₂

With metanizatsiya: with + troublesome zone₂ ->CH₄ + H₂ 0

Hydro Gasification: 2h₂ + WITH ->CH₄

[0134] in reaction of hydro metanizatsii, result is "straight" gas flow crude product, enriched with methane, which can be further purified and additionally enriched with methane for, to provide final product of light gas 816. Such approach differs from normal processes gasification, such, which are based on partial combustion/oxidation of carbon source, where singaz (carbon oxide + hydrogen) is main product (with direct to produce small amount of methane or without it), which can then be subjected to additional treatment to obtain methane (by means of catalytic metanizatsii presented reaction) or any amount of other higher hydrocarbon products. When methane is a desired final product, reaction hydro metanizatsii provides possibility to increase the efficiency of ny and more low cost methane, than in traditional methods gasification. In some variants, methods, discovered patent in the U.S. 2010/0292350, entitled For Laptops processes cpu Hydrotnethanation care of a CarbonaceousFeedstock, filed before the 12 May 2010 Da (is connected in this description as references) is used as method 800.

[0135] method 800 may be is integrated with methods of 300 and 700 so, that light gas 816, produced by the 800, can be light gas 302. Similar manner, carbon dioxide from by-products 814 may be gas 704, used in method 700. In addition, heavy fractions of 708 from method 700 can be initial carbon-containing raw material 802 for method of 800.

[0136] on fig. 9a - 9d displayed various versions reactors non-thermal plasma, described in the present invention. In said versions, singaz is obtained by methods using non-thermal plasma. Radicals, obtained in production of syngas, used directly in subsequent reactions with oil. In some versions of implementation nonthermal plasma is a plasma sliding arc discharge. Plasma sliding arc discharge uses dynamic discharge for plasma generation, while corona discharge produces plasma with static discharge. In some versions of implementation sliding arc has two divergent electrode. Arc is formed, when gas goes to due to application of high voltage. Gas pushes out arc down along the length of the reactor. Addition of, as gas reaches end of reactor, arc switched off. The other arc is then generated at gas inlet.

[0137] on fig. 9a is represented by device 900 for producing liquid fuel product, in particular, for preparing hybrid fuel. In submitted version, device 900 is a reactor with sliding by arc discharge, which is a version of a specific reactor non-thermal plasma. In version of realisation, submitted on fig. 9a, liquid st and gas are to - processes in reactor. Plasma acts simultaneously on liquid st and gas. In some versions of the integrated method 100, device 900 may be used for the process of producing of light gas/liquid fuel 104. Similar manner, in some versions of the method 300, device 900 may be used for reactor vessel 310, including, in some versions of implementation, pump/compressor 306 and ejector 308. In addition, in the method 350, device 900 may be used for activation of source 352.

[0138] device 900 includes inlet hole 901 for introduction of light gas, liquid fuel (for example, alcohol or oil) or their mixture. Device 900 additionally includes electrodes 903 and high-voltnye connectors 908. High voltnye connectors 908 is connected to power source, and voltage is supplied to electrodes 903. In some versions of implementation, high voltnye connectors supplied to approximately 90 kV, which corresponds to approximately 20 kW direct current, 30 kHz. Electrodes 903 are in liquid stnom connection with inlet hole 901 (in some versions of implementation by track, determined by prechamber 911). In some versions of implementation electrodes 903 represent cathodes slightly accurate force (that is made from metals slightly accurate force). Illustrative cathode slightly accurate force includes, without limiting, thorium. When voltage from high V connectors 908, is formed electric discharge or arc 904, which passes along the whole length of electrodes. Device 900 additionally includes output zone 905, which is located in liquid stnom connection with by, certain electrodes. In some versions of implementation zone outlet 905 optionally includes and is in liquid stnom connection with coils Helmholtz 906, heating spiral 912 and catalytic clamp 913. Outlet hole 910 for outlet of oil also is in liquid stnom connection with zone outlet 905. The second inlet hole 902 is provided and is in liquid stnom connection with zone outlet 905, so, that zone of outlet 905 is located between electrodes 903 and second inlet opening of 902. Device 900 additionally includes outlet hole 907. In some versions of implementation, capacitor 909 is made for collection of outgoing fuel from device.

[0139] after introduction into the device 900 through the first inlet hole 901, liquid fuel moves along track, a certain with the use of electrodes 903 and, optionally, prechamber 903. Under action of electric arc 904, there are formed free radicals. Electric arc 904 pushes out liquid fuel and inducing reaction products by track, a certain electrodes 903 to zone outlet 905. In the zone of outlet 905 free radicals are in close contact with liquid styu, introduced in device 900 through the second inlet hole 902, so, is obtained liquid fuel product. In some versions of implementation liquid st, administrated through the second inlet hole 902, is a rebuilt liquid st, such as the reformulated oil. In some versions of implementation mixture of free radicals and liquid STI, introduced through the second inlet hole 902, further contact with catalyst 913. Catalysts, which are useful for inclusions in device 900, include catalysts, described in the present invention. In some versions of implementation heating spiral 912 provide heating reaction mixture, while in some versions of implementation, Helmholtz coils 906 generated magnetic field, promoting development of the process of formation of liquid fuel. Hybrid fuel, formed in device 900 is removed from device through outlet hole 907. At output of the device 900, produced hybrid fuel can be subjected to additional treatment, as it is determined in integrated method 100.

[0140] configuration device 900 allows for realization of the method, where liquid st, administrated through the second inlet hole 902, is in close contact with free radicals, generated action of electrodes to liquid fuel, are shaped free radicals. Being brought contact, provided by configuration device 900, provides unobstructed connection of two reagents, without using additional energy, as at usual treatment of fuel. In addition, was found, that hybrid fuel, obtained from device 900, demonstrates spider nnuyu viscosity and increase of volume of, and also spider nnoe content of polyaromatic compounds.

[0141] on fig. 0.9B is represented by device 920 for producing liquid fuel product, in particular, for preparing hybrid fuel. In illustrated version, device 920 represents another variant of reactor with sliding by arc discharge, which is a a specific version of realisation reactor non-thermal plasma. In version of realisation, illustrated on fig. 0.9B, liquid st reacts with singazom and radicals, while electrons react with liquid styami in catalytic chamber. As in case of device 900, in some versions of the integrated method 100, device 920 may be used for process light gas/liquid fuel 104. Similar manner, in some versions of the method 300, device 920 can be used for reactor vessel 310, including, in some versions of implementation, pump/compressor 306 and ejector 308. In addition, in the method 350, device 920 may be used for activation of source 352.

[0142] device 920 includes many components are device 900, including electrodes 903, which at supply voltage through high voltnye compounds 908, is created arc 904. Similar manner, device 920 includes output zone 905, which optionally is in liquid stnom connection with catalyst 913, Helmholtz coils 906 and heating coils 912. Device 920 also includes outlet hole 907 and capacitor 909.

[0143] device 920 includes inlet hole 921. Inlet hole 921 device 920 provides input of light gas. Unlike it, inlet hole 901 device 900 (Figure 9 and) includes input mixture gas and liquid STI, which facilitates joint treatment liquid STI and gas electrodes reactor with sliding by arc discharge. In device 920, liquid st in form of oil or of reprocessed oil, is introduced through the second inlet holes 922a and 922. In some versions of implementation rebuilt oil is introduced through inlet hole 922a, while oil is introduced through inlet hole 922. In some versions of implementation soluble catalyst also is introduced through inlet hole 922. Inlet holes 922a and 922 are in liquid stnom connection with zone outlet 905 so, that they are accessible for close contact with products of reactor with sliding by arc discharge. For example, in some versions of implementation, liquid st reacts with singazom and radicals, formed by in reactor non-thermal plasma, while electrons interact with liquid styami in zone of output of 905. In some versions of implementation zone outlet 905 is a catalytic chamber. As in device 920, after, as reaction products are mixed to form liquid fuel product, hybrid fuel is removed through the outlet hole of 907.

[0144] on fig. 9C is represented by device 940 for producing liquid fuel product, in particular, for preparing hybrid fuel. In illustrated version, device 940 is a other version of realisation reactor with sliding by arc discharge, which is a version of a specific reactor non-thermal plasma. In version of realisation, illustrated on fig. 9C, singaz, and radicals, and electrons, created by sliding arc, killed them in the moving flow liquid STI, optionally containing catalytic layer. As in devices 900 and 920, in some versions of the integrated method 100, device 940 may be used for process of light gas/liquid fuel 104. In addition, in some versions of the method 300, device 940 can be used for reactor vessel 310, including, in some versions of implementation, pump/compressor 306 and ejector 308. In addition, in the method 350, device 940 may be used for activation of source 352.

[0145] device 940 includes many components are device 900 and 920, including electrodes 903, which at supply voltage through high voltnye compounds 908, is created arc 904. In version of realization of the device 940, zone outlet 905, which optionally is in liquid stnom connection with layer of catalyst 913, Helmholtz coils 906 and heating coils 912.

[0146] device 940 includes inlet hole 941. Inlet hole 941 device 940 provides input of light gas. In device 940, liquid st in form of oil or of reprocessed oil is introduced through the second inlet hole 942. Inlet hole 942 is in liquid stnom connection with zone outlet 905 so, that reaction products from reactor with sliding by arc discharge, directly harsh moving flow liquid STI, supplied through the inlet opening 942, so, being in close contact with products of reactor with sliding by arc discharge. After the, as reaction products are mixed to form liquid fuel product, hybrid fuel is removed, using outlet hole 907, through separator 909. In some versions of implementation, separator 909 is also condenser. In device 940, output from the system of heavy and light oil is provided through separator 909.

[0147] on fig. 9d it is shown device 960 for production of product of liquid fuel, in particular, for preparing hybrid fuel. In illustrated version, device 960 is a reactor with sliding by arc discharge, which is a version of a specific reactor non-thermal plasma. In version of realisation, illustrated on fig.

9d, reactor non-thermal plasma is made in form of "plate" several microplasma reactors. Output of reactors with plates device 960 encounters drops liquid STI or thin films. In some versions of the integrated method 100, device 960 can be used for process of light gas/liquid fuel 104. In addition, in some versions of the method 300, device 960 can be used for reactor vessel 310, including, in some versions of implementation, pump/compressor 306 and ejector 308. In addition, in the method 350, device 960 may be used for activation of source 352.

[0148] device 960 includes inlet hole 961 for introduction of light gas in the chamber of light gas 961a. Device 960 additionally includes ceramic plate 963, which has holes 964, through which gas is carried out to zone of output of 965. Wire 968 superimposed over the ceramic plate 963, and they are in electrical connection with the power source of the 966 for supply of voltage (for example, 6 - 1000 v pulse). As the gas crosses ceramic plate 963, supplied to voltage creates multiple arcs in each from holes 964, so providing reaction with light gas, and results to formation of free radicals, which are transported in outlet zone 965.

[0149] device 960 additionally includes the second inlet hole 962 for input of liquid STI in liquid stnuyu chamber 962a. In some versions of implementation, liquid st, which is introduced through the second inlet hole 962, is oil or mixture of oils. In some versions of implementation, liquid st, administrated through the second inlet hole 962, is a rebuilt liquid st, such as the reformulated oil. Liquid st is transported through plate diffuser 969 in outlet zone 965. After introduction into the outlet zone 965, diffundirovavshaya liquid st comes in being brought contact with reaction products of light gas, which were conducted through ceramic plate 963, to produce, so, hybrid electric fuel product. Optionally, catalyst layer 973 is present in zone of output of 965. In addition, optional heaters 972 is heated device 960. After mixing of reaction products, they come out from the device through the outlet hole of 967. In some versions of implementation optional vacuum pump is located between zone output 965 and outlet hole 967. At output of the device 960, produced hybrid fuel may be additionally processed, as it is determined in integrated method 100.

[0150] on fig. 9a-and-9d, configuration of each device 900, 920, 940, and 960 method provides for, where liquid st is in close contact with free radicals, generated action of electrodes to liquid fuel, are shaped free radicals. Being brought contact, provided by configuration of each device, provides direct connection reagents, without using additional energy, as at usual treatment of fuel. In addition, authors was, that hybrid fuel, produced by means of devices 900, 920, 940 and 960 demonstrates spider nnuyu viscosity and increase of volume of, and also spider nnoe content of polyaromatic and aromatic compounds.

[0151] hybrid types of fuel 120 obtained by means of embodiment of the method 100 show excellent characteristics productivity as compared with competing types of fuel (for example, biodizelnym fuel, fuel "green diesel", types of straight-run fuel from vegetable oils, emulsionnymi types of fuel oil/water and common types of fuel). For example, certain versions of the types of hybrid fuel can be alternative "the drop-In of" fuel, and not fed with ordinary types of fuel. Some hybrid types of fuel have relatively low temperature of chilling and cloud, can to withstand much multiple of cycles of freezing/thawing and have relative to the long stability (for example, more than 1 year). So, some hybrid types of fuel, discovered in this description, are suitable for use in cold weather. In one exemplary example, hybrid fuel, containing approximately 20 about.% diesel fuel of new generation (called Next Generation Diesel) (available for gaining in the Global the Energy the Resources, LLC more care Fort Apartments on Wayne, Ind.) and approximately 80 about.% GDIESEL™ (available for gaining in the Advanced RefiningConcepts care the RENO, ν℮ν.), unexpectedly shown WiFi client continuously tracks the chilling temperature to approximately 25 °f (14 theoretically) with respect to separate fuel components. The same hybrid fuel also unexpectedly shown WiFi client continuously tracks the cloud temperature of to approximately 5 °f (3 theoretically). In accordance with some of the methods, mixture of hybrid fuel, discovered in this description, include to approximately 20% biofuel emulsion (for example, result process 102 on Figure 1 or 222 on Figure 2). In some versions of implementation, mixture of hybrid fuel, discovered in this description, include from approximately 5% to approximately 10% biofuel emulsion. In addition, in some versions of implementation, in hybrid fuel is present to approximately 20% water.

[0152] additional the claimed version of realisation of hybrid fuel involves combining activated natural gas and/or hydrogen with diesel fuel of new generation with application of 350, described above. Is considered to be, that such hybrid fuel will demonstrate spider ned emission s02, as compared with diesel fuel of new generation, only due to increase ratio of hydrogen to carbon in fuel.

[0153] in some versions of implementation of hybrid kinds of fuel, disclosed in this description, increased lubricating capacity and/or viscosity of the liquid fuel owing to the biofuel emulsion. So, diesel with ultra-low content of sulfur (ULSD) can be used as liquid fuel in some compositions, not subjected discomfort from low lubricating capacity and/or low viscosity ULSD. In addition, demand decreases in use of additive for ny to increase the lubricating ability of, that allows to avoid increasing the cost of and technological complexity. In some versions of implementation, composition, containing ULSD, have more low viscosity and congelation point, than ULSD, usual vulnerable hydro cleaning, or biotoplivnaya emulsion.

[0154] additional advantages of the present invention consist in the fact, that some hybrid types of fuel, discovered in this description, show spider nnym ejection greenhouse gases, spider nnym ejection solid particles and initial for them is raw material, containing materials, produced with use of carbon dioxide (for example, vegetable oils). Total WiFi client continuously tracks the ejection, as expected, is approximately 50% for some methods of producing hybrid kinds of fuel. At the same time, expected WiFi client continuously tracks of carbon dioxide emission and solid particles on 30% from the end use. So, application of such types of hybrid fuel has less influence on the environment. Additionally, certain versions of the hybrid types of fuel allow for avoiding stage transesterification, characteristic for many biodizelnykh products. So, data hybrid types of fuel will not contain glycerin, methyl esters of fatty acids (of Fame) or ethyl esters of fatty acids (FAEE), which usually are at least, in small amounts, in typical biodizelnykh products. Since normative recommendations not depending presence data by-products in some types of fuel (such as fuel for jet engines), said hybrid types of fuel are useful for transportation of existing pipeline infrastructure, in contrast to most typical biodizelnykh fuel products. In addition, avoiding process transesterification, can be to reduce investments, operational costs, complexity of and time of this method. It reduces cost production of such hybrid kinds of fuel.

[0155] the described advantages of show, that versions of the present invention provide alternative "the drop-In of" types of fuel, which correspond to to ASTM and the Pan parameters biofuel and emissions greenhouse gases, based on specific properties of complete cycle of fuel production and evaluation of analysis of operational resource. Versions of hybrid kinds of fuel, are analyzed as an alternative "the drop-In of" fuel, since they can be used as independent fuel, not only as additive to fuel. Since certain hybrid types of liquid fuel is obtained due to the use of natural gas, demand in liquid oil is reduced. In addition, methods for preparing liquid fuel can be adapted for remote regions, where in the present time there is delivery not used natural gas.

[0156] versions of hybrid kinds of fuel, produced embodiments methods, described in the present invention, demonstrate desired characteristics, the described, with preservation of signs, characteristic for normal kinds of fuel. N1aprimer, hybrid types of fuel, the described in the present invention, have high content of energy on pound/gallon, are able to withstand several cycles freezing, are stable, have suitable viscosity and value of cetane number of (for replacement of fuel of diesel type), equivalent content of phosphorus, compatible curves distillation, favorable corrosion properties, as well as compatibility with existing sealing materials.

[0157] other illustrative versions can be described as follows:

[0158] some illustrative versions can include combining free radicals, formed from non-heat/nonequilibrium plasma using pure oxygen and/or other selected gases (and/or separately or in combination reforming of methane with oxygen, with, s02, water, hydrogen, hydrocarbon gases and their combinations/selected relations in mixture) for reforming, cracking, hydro genizatsii, methylation, oxidative desulfurization, desulfurization in presence of hydrogen, carbonylation, hydro formylation, alkylation of, polymerization and other types of reworks initial raw materials and/or chemical processes. Initial raw material and/or selected plasma gases also may include inert gas, such as argon, zeon, nitrogen or components are gas phase, such as with, ethane, butane, DME, ammonia, urea, singaz and T. d. Can be used plasma specific intensity, for, to provide originality reaction. Gas-phase reactions can cause dissociation of initial gas and/or stimulation gases to oscillatory/and/or rotational excited level. Selected volume rate can be used for producing desired products.

[0159] some illustrative versions can include selection of mixtures radicals, generated by non-thermal/nonequilibrium plasma, and various gases and series and/or koprotsessornoi of individual oil fractions for production of desired end hydrocarbon products.

[0160] some illustrative versions can include field oxygen radicals and/or stimulated fractions, generated by non-thermal/nonequilibrium plasma, for fragmentation and functionalizing oil flows, including:

a. breaking long-chain molecules

b of. Oxidizing desulphurisation and desulphurisation in presence of hydrogen - heavy types of oil, as well as polishing

of c. Creation of synthetic oil fractions in combination with diesel and other products with increase content of oxygen for to increase the fuel efficiency ny

[0161] some illustrative versions can include successive application of methods of producing desired final products.

[0162] some illustrative versions may involve application of the methods of treatment of in production of oil (well), in process of treatment (processing) and in final use of engines.

[0163] some illustrative versions can include combining natural gas and/or oxygen with fuel for, so to fuel volume and improve its characteristics.

[0164] necessity oxygen-containing fractions described above in this document. Some illustrative versions can include expansion of addition of method of oxygen with plasma/free radical. In addition, understanding, which the authors included for heavy oil, described in the present invention above, and some represented versions, may involve application of oxygen plasma and hydrogen/methane radical reactions for achievement of registries targets. Represented some versions also may include method of oxidative desulfurization by means of plasma, generated free radicals, in combination with desulfurizatsiei in presence of hydrogen. References can be used to types of biofuel.

[0165] should be understand, that volume of of the present invention is not restricted described above of the methods, and, peer, includes modification and finishing the, that was described. All references, the described, are connected in its whole fullness as references in this description.