RU2304162C1 - Apparatus for producing of combustible mixture - Google Patents

Abstract

FIELD: fuel engineering, in particular, preparing of liquid hydrocarbon fuels.

SUBSTANCE: apparatus has reservoir 6 for basic hydrocarbon fuel and mixing reservoir 9, said reservoirs being connected with one another through pipeline and locking fittings. Reservoir 6 and reservoir 9 are equipped with level measuring devices. Output of mixing reservoir 9 is connected through circulation pump with inlet of disperser 8 whose outlet is connected to inlet of mixing reservoir 9. Apparatus is additionally provided with reservoir 1 for softened water, said reservoir 1 having cooling member, reservoir 3 designed for saturating of softened water with air and provided with level measuring device, pumps for feeding water through meter 4 from above reservoirs into disperser 8 and further to mixing reservoir 9. Disperser 8 is formed as acoustical radiator. Mixing reservoir 9 is joined to sulfur removal unit 10 furnished with separating device and positioned on pipeline for feeding of resultant hydraulically stabilized combustible mixture into accumulating reservoir 11. Apparatus of such construction allows desulphurized liquid aqueous-hydrocarbon mixture to be produced, said mixture being characterized by inseparability with time and being designed for increasing of fuel combusting process.

EFFECT: increased efficiency of fuel combustion process enhanced due to utilization of liquid aqueous-hydrocarbon mixture, and increased ecology controlling of process.

1 dwg, 1 tbl

Description

The invention relates to the field of fuel energy and relates to the quality of the preparation of liquid hydrocarbon fuels.

The development of power plants in the direction of improving efficiency, weight characteristics, reliability and resource makes high demands on the quality of liquid hydrocarbon fuels.

In recent years, new raw materials and technological methods of oil refining have appeared. This has led to a change in the physicochemical and operational properties of standard hydrocarbon fuels for power plants. To date, new experimental and calculated data on their properties have been accumulated (for example, characteristics of combustion, electrical, thermal stability, the effect of dissolved water on combustion characteristics, etc.), and new materials have also been obtained on the change in these properties depending on various factors.

However, currently, the disadvantages of the known liquid hydrocarbon fuels are:

1) it was established by direct observation that when burning separately such combustibles as kerosene, diesel fuel, gasoline, fuel oil, heating oil, etc., in the areas of a possible lack of oxygen solid products of incomplete combustion are formed, which leads to coking of the spraying nozzle openings and the appearance of dark smoke. The tendency to smoke is determined by the structure of the fuel, the presence of high molecular weight compounds and the size of atomization droplets. The larger the droplet and the less dissolved water is in the fuel, the larger the coke residue is, therefore the heat loss from the chemical incompleteness of combustion of these fuels in power plants is relatively large (the coefficient of completeness of combustion is 0.85-0.9);

2) over 95% of hydrocarbon fuels consumed in power plants contain up to 4.5% sulfur, from 0.005 to 0.15% vanadium, as well as sodium, calcium, iron and other elements. In this regard, during the combustion of liquid hydrocarbon fuels, ash-forming substances give compounds such as oxides of various metals, sulfur, silicon, vanadium, as well as sulfates, sulfides and other compounds that are deposited on the elements of the flow part of power plants and cause corrosion. Deposits are formed mainly due to sodium, calcium compounds, vanadium anhydride and other more complex compounds of vanadium and sodium, which are in a stream of gases in a molten form. Corrosion of the elements of the flow part of power plants is a chemical process that sharply intensifies with increasing temperature. Strong corrosion of parts of the flowing part of power plants is caused by vanadium pentoxide V ₂ O ₅ , as well as sodium sulfate Na ₂ SO ₄ . The most dangerous is vanadium corrosion, which is sharply intensified in the presence of sodium sulfate at a temperature of 650-700 ° C and above.

At temperatures above 800 ° C, sodium sulfate is also able to dissolve the protective layer of metal and cause corrosion;

3) during combustion of a fuel-air mixture in a flare, nitric oxide is formed as a result of oxidation of both nitrogen in the air (at high temperatures) and nitrogen entering the organic mass of fuel. In this and another case, the rate of formation of nitric oxide and its final concentration depend on the content of free oxygen in the volume of the burning torch and its temperature.

Nitrogen oxides cause diseases of the respiratory tract, nervous system and human vision, enhance the effects of other toxic substances, including carcinogens. In addition, nitric oxide is actively oxidized by air ozone by the following reaction:

NO + O ₃ → NO ₂ + O ₂ .

The occurrence of this reaction in high atmospheric layers leads to the destruction of the ozone layer, which protects all life on Earth from the harmful effects of the ultraviolet part of the spectrum of solar radiation.

At high humidity, a mixture of NO ₂ , carbohydrates, smoke and soot forms a toxic photochemical fog - smog.

Among those with high carcinogenic activity, 3,4-benzoperen (C ₂₀ H ₁₂ ) or gasoline-α-pyrene, which is formed during incomplete combustion of liquid hydrocarbon fuels as a result of their high-temperature pyrolysis, are attributed. The latter is one of the strongest carcinogens. Under natural conditions, C ₂₀ H _{12 is} very stable and, accumulating in the soil or present in the air, participates in the biological cycle, adversely affecting biological processes in living organisms.

When liquid hydrocarbon fuel is combusted, the metal sulfides present in it, interacting with atmospheric oxygen at high temperature, form:

2Na ₂ S + 3O ₂ → 2SO ₂ + 2Na ₂ O;

4FeS ₂ + 11O ₂ → 8SO ₂ + 2Fe ₂ O ₃ ;

2ZnS + 3O ₂ → 2SO ₂ + 2ZnO

etc.

Sulfur gas or sulphurous anhydride SO ₂ generated during the combustion of standard liquid hydrocarbon fuels in power plants and released into the environment, has a detrimental effect on plants.

Studies conducted in many countries have revealed the possibility of increasing the completeness of combustion and reducing the content of toxic components (nitrogen and sulfur oxides, carbon, coke residues, etc.) in exhaust gases by mixing in a certain ratio of water and hydrocarbon fuel. Moreover, a more complete combustion of the latter is achieved due to the gasification of part of the carbon and coke residues according to the equation:

C + H ₂ O = CO + H ₂

and subsequent afterburning of a mixture of gases CO and H ₂ .

A device for producing a combustible mixture is described in the application RB 1881, IPC B01F 3/08, 1996, including a water tank, a water supply pump, a filter, a control valve, a fuel oil tank, a fuel oil heater, a fuel pump, a fuel filter, a mixer, hydrodynamic dispersant, emulsion tank and bundle of binding pipelines. A disadvantage of the known device is that the resulting mixtures over time are stratified into water and fuel oil, and the content of sulfur compounds in them remains.

Of the known devices, the closest to the claimed one is the device described in US Pat. RU 2009403, 1994, including a tank for liquid hydrocarbon fuel, a water tank, a set of piping with shutoff valves, a mixing tank, the outlet of which is connected through the circulation pump to the inlet of the dispersant. A disadvantage of the known device is that in the resulting combustible mixtures, the content of sulfur compounds and solids remains.

The objective of the invention is to develop a device for the preparation of desulfurized non-separable liquid water-hydrocarbon mixture, increasing combustion efficiency and environmental friendliness.

The solution to this problem is achieved by the fact that the claimed device is equipped with containers for softened water with a cooling element, saturation of softened water with air, hydrocarbon feed with level meters, pipelines with shut-off and shut-off and control valves and pumps for supplying from the respective containers through water and hydrocarbon meters fuel through the dispersant to the mixing tank, while the dispersant is made in the form of a sound emitter, the output of which is communicated through pipelines and ornoy reinforcement with the mixing tanks and sulfur removal unit with a separating device mounted on the pipeline for supplying a gas mixture obtained Hydrostabilized to the collecting tank, pump and which is provided with a counter.

The essence of the invention is illustrated by the drawing, which schematically shows a General view of the described device.

The device comprises a storage tank 1 of softened water with a cooling element fixed therein and level meters (upper and lower). Capacity 1 is equipped with inlet, outlet pipelines, shut-off and shut-off and control valves, a temperature gauge and a pump for supplying softened water through the meter 2. The outer surface of the tank 1 and pipelines is covered with thermal insulation. As a pump, a centrifugal pump can be used.

Capacity 1 is intended for the accumulation, storage, cooling and delivery of softened water through the counter 2 to the saturation tank 3.

Counter 2 serves to instantly indicate the flow rate and turn off the feed when a given dose of the product is issued.

Saturation tank 3 contains inlet and outlet pipelines, stop and shut-off and control valves, level meters (upper and lower), pressure meters, a water spray attached to it, a water meter 4 and a circulation pump unit, which is designed for circulating pumping of softened water in the tank .

Capacity 3 is intended for accumulation, saturation of softened water with air, storage and delivery through the counter 4 of the required amount of water with a given flow rate to the pump unit 5.

The water meter 4 serves to dose the flow rate and the amount of saturated softened water to the pump unit 5.

Capacity 6 is equipped with inlet and outlet pipelines, shut-off and shut-off and control valves, level meters (upper and lower), a pump unit in fire and explosion-proof design, meter.

Capacity 6 is intended for accumulation, storage and delivery through the counter 7 of the original hydrocarbon fuel.

The pump unit contains a high pressure pump (up to 40 kgf / cm ² ), an electric drive, inlet and outlet pipelines, shut-off, shut-off, control and measuring valves and is intended for preliminary mixing of softened water saturated with water and initial hydrocarbon fuel supplied to the pump inlet and subsequent supply under a pressure of 10-40 kgf / cm ^{2 of a} water-hydrocarbon mixture into a hydrodynamic ultrasonic dispersant 8 with a given flow rate.

The hydrodynamic ultrasonic dispersant 8 is designed to create a sound field with characteristics: a frequency of 15-365 kHz, a variable sound pressure of 0.5-20.0 kgf / cm ² and a sound force of 0.16-365 W / cm ² in the pumped liquid.

The mixing tank 9 is equipped with inlet and outlet pipelines, shut-off, shut-off and control valves, level meters (upper and lower) and pressure. At the same time, the mixing tank through the stop valves, the binding pipelines, the pump unit 5, the hydrodynamic ultrasonic disperser 8 is looped around by itself and through the stop valves, the piping is connected to the sulfur removal unit 10.

Mixing tank 9 is designed for pumping a water-hydrocarbon mixture in a closed circuit (mixing tank - pumping unit - hydrodynamic ultrasonic dispersant - mixing tank).

The sulfur removal unit 10 is equipped inside with a separating device (for example, ultrafiltration elements), inlet and outlet pipelines, shut-off and control valves, level meters (upper and lower) and pressure.

The sulfur removal unit 10 is designed to remove sulfur and other mechanical impurities from the water-hydrocarbon mixture and transfer the resulting hydrostabilized combustible mixture purified from sulfur and mechanical impurities to the storage tank 11.

The storage tank of the hydrostabilized combustible mixture 11 contains inlet and outlet pipelines, shut-off and control valves, level meters (upper-lower), an auxiliary pump unit (for example, a centrifugal type), and a meter for the combustible mixture.

The storage capacity of the hydrostabilized combustible mixture 11 is intended, on the one hand, for the accumulation of a combustible mixture purified from sulfur and mechanical impurities, and on the other hand, provides a pump output of predetermined volumes of a combustible mixture. At the same time, the storage tank provides a drain of the combustible mixture and by gravity.

The proposed device operates as follows.

Preparatory work includes:

- the stop valves are opened, and the storage tank 1 is softened (desalted) cooled to 0-20 ° C with water to a certain upper level. Monitoring the filling of the tank is carried out by level meters (lower and upper). Upon reaching the limit level, the filling of the tank stops, the shut-off valve closes;

- the stop valves are opened, and the storage liquid 6 is filled with the initial liquid hydrocarbon fuel to the maximum upper level. Monitoring the filling of the tank is carried out by level meters (upper and lower). Upon reaching the limit level, the filling of the tank stops, the shut-off valve closes.

After preparatory work on the storage tank 1, the dispensing valves are opened, the auxiliary pump unit is turned on, and the calculated amount of softened water is fed into the saturation tank 3 through the counter 2. After the calculated amount of chilled softened water is delivered to the saturation tank, the auxiliary pump unit is turned off and closed storage tank 1 shut-off valves and pressurization of the saturation tank 3 is made with air purified from mechanical impurities to a pressure of 1.5-4.5 gf / cm ^2. After pressurizing the saturation tank, the shutoff valves open and the auxiliary pumping unit is turned on, which pumps water in a closed circuit (pumping unit - a water atomizer in the saturation tank - pumping unit), and during pumping, water is continuously monitored for air saturation. Upon reaching the maximum saturation of softened water with air, the auxiliary pump unit is turned off and the shut-off valves of the saturation tank are closed.

After completion of the process of saturating softened water with air at saturation tank 3, mixing tank 9, shut-off dispensing valves and air-saturated softened water with excess air pressure open through the water meter 4, the pump unit of dispersant 5, dispersant 8 is discharged into the mixing tank 9. When a predetermined volume of water is dispensed in the mixing tank, the water supply from the saturation tank is stopped, the shutoff valves on the tanks are closed. The outstanding shut-off valves on the mixing tank 9 are opened, the pump unit of the dispersant 5 is turned on, and the discharged volume of the air-saturated softened water is pumped in a closed circuit: the mixing tank 9 is the pump unit of the dispersant 5 - dispersant 8 is the mixing tank 9. During ring pumping when water under pressure passes through a hydrodynamic ultrasonic dispersant 8 in water, a sound field arises with the selected sound characteristics due to the dispersant setting.

Under the action of a sound field on water, cavitation arises in it, which is characterized by high local pressures and temperatures that occur during the collapse of cavitation bubbles.

In the powerful cavitation mode, without stopping the ultrasonic treatment, the dispensing valves are opened on the storage tank 6 and 70-97 parts of the original hydrocarbon fuel are introduced through the fuel meter 7 while stirring with air saturated with softened water, after which the shutoff valves and the mixture are closed on the fuel storage tank mix to achieve a degree of dispersion of 10 ⁵ -10 ⁸ cm ^-1 and reduce in the mixed mixture the total sulfur content to less than 0.001% (wt.).

After reaching the degree of dispersion of the mixture 10 ⁵ -10 ⁸ cm ^-1 and reducing the sulfur content in it to less than 0.001% (wt.), The inlet and outlet shut-off valves open on the sulfur removal unit 10, the inlet shut-off valves open on the storage tank 11, then the mixing tank closes the inlet valves and the water-hydrocarbon mixture under pressure is passed through the separating device of block 10, in which sulfur and solids are separated and the resulting hydrostabilized combustible mixture is sent to akopitelnuyu capacity of 11.

After delivery of the total volume of the obtained hydrostabilized combustible mixture from the mixing tank 9 to the storage tank 11, the dispersing pump unit 5 is turned off, and samples are taken for carrying out control analyzes of the mixture. At the same time, shutoff valves on block 10 are opened and sludge of mechanical impurities with sulfur is drained. Then the process of preparing a hydrostabilized combustible mixture is repeated until reaching the maximum upper level in the storage tank 11. Monitoring the filling of the tank 11 is carried out by level meters.

For the delivery of the obtained hydrostabilized combustible mixture from the storage tank 11, an outlet stop valve is opened, an auxiliary pump unit is turned on, and the mixture is discharged in a predetermined quantity into the consumer's container. After the delivery of the combustible mixture, the pump turns off and the shut-off valve closes.

The control of the issued dose of the combustible mixture from the storage tank 11 is carried out by level meters.

When mixing in an ultrasonic field during the collapse of cavitation bubbles in a short time (less than 1 μs), the gas in the bubble is heated to high temperatures (more than 1000 ° C) and high pressures develop (1500 kgf / cm ² ). An increase in temperature and pressure, in turn, promotes the formation and recombination of radicals, the decay of large molecules, and the synthesis of new chemical compounds. Thus, under the influence of cavitation, sound chemical reactions proceed in the feedstock.

The sector of these reactions is extremely diverse, as is the set of external factors affecting their thermodynamics and kinetics. Based on the values of the breaking energy of various bonds in the molecules, as well as the activation energy of certain transformations, cracking, isomerization, and demerization and trimerization reactions of high molecular weight paraffin hydrocarbons (alkanes), mono- and polycyclic aromatic hydrocarbons (arenes) predominantly develop unsaturated hydrocarbons (alkenes), various hetero-organic compounds containing sulfur atoms (sulfides, polysulfides, thiophanes, etc.), oxygen (naphthenic acids), metalloporphins data and other organometallic components containing atoms of sodium, calcium, iron, zinc, copper, vanadium and other trace elements, resinous sulfatene substances.

The kinetics of these sonochemical reactions is determined by the rate of formation and expenditure of radicals.

A feature of these sonochemical reactions is the pulsed nature of the formation of radicals due to the in-phase collapse of cavitation bubbles. The temperature inside the bubble is not evenly distributed, with a maximum at its center. Accordingly, the spatial distribution of radicals has a similar shape (spherically symmetric Gaussian distribution). The bubble is an autonomous system from the point of view of the nature of the reactions taking place - the radicals formed in neighboring bubbles practically do not interact with each other. The minimum radius of the cavitation bubble (R _min ≥10 ^-5 cm), and the initial number of radicals in it (~ 10 ⁴ -10 ⁶ ).

In industrial practice, this high-tech and high-energy method has not yet found wide application, which is primarily due to the lack of high-performance technological equipment, namely, devices that generate high-energy cavitation and at the same time transfer this energy to the processed technological environment.

To date, we have developed such equipment and mastered its production.

Thus, under the influence of ultrasound with the indicated characteristics, not only the mass transfer, heat transfer chemical processes in the feedstock (liquid hydrocarbon fuel + water) are accelerated, but are accompanied by profound changes at the molecular-ion level and resulting in a qualitatively new hydrocarbon fuel mixture. Confirmation of this is the conclusion of the All-Russian Research Institute for Oil Processing No. 23 / 45-2217 of 10/17/2001.

Lowering the water temperature from 20 to 0 ° C increases the level of cavitation activity and the degree of saturation of it with air, and accordingly carbon dioxide, oxygen and inert gases, the maximum of which is achieved at 0 ° C. An increase in water temperature reduces its level of cavitation activity and the degree of saturation of air, and at 65 ° C, cavitation in water is practically absent.

By simultaneously increasing the static (P ₀ ) and variable sound (P _a ) pressures at the optimum value of P ₀ / P _a = 0.4, one can repeatedly increase the level of cavitation activity of water and its degree of saturation with air. The upper limit of the level of cavitation activity of water in this case is limited only by the level of sound pressure that can be achieved using modern sources of sound energy.

The increase in static pressure greatly affects the nature of the cavitation area and the degree of saturation of water with air. The growth of P ₀ , on the one hand, leads to a decrease in the number of cavitation “nuclei”, and on the other hand, to the preservation of the number of pulsating bubbles. At a certain ratio of P ₀ / P _a large pulsating bubbles in the liquid may not exist at all.

However, it should be remembered that at Р ₀ ≥Р _а there are no conditions for cavitation in the liquid and the size of all bubbles becomes smaller than the critical size, as a result of which they pulsate in the sound field, changing little in size.

An increase in P a has _a double effect on the dynamics of cavitation density - on the one hand, the expansion phase of the bubble is delayed and the radii of cavitation bubbles R _max , the time of collapse of the bubbles Δt, and the time of shift of the phase of collapse t _max with respect to the oscillation period T increase (these parameters increase above some certain values) reduces cavitational activity of the bubbles; on the other hand, an increase in P _a to values above the threshold is certainly necessary, since otherwise cavitation does not occur. In addition, with an increase in P _a , the time increases during which the forces that keep the bubble in equilibrium are balanced by sound pressure, and the bubble can expand indefinitely. Therefore, an increase in P _a to a certain limit has an effect on the dynamics of the cavity, similar to a decrease in frequency.

The motion of vapor-gas bubbles in a sound field becomes unstable if Δt≥T / 2. In this case, the cavitation bubble degenerates into a pulsating one. Therefore, increasing P _a , we can expect an increase in the cavitational activity of a single bubble only under the condition Δt≤T / 2.

An increase in the oscillation frequency leads to a decrease in R _{max of the} cavitation cavity at a constant amplitude value of sound pressure. Such a result is clear if we take into account that with increasing frequency φ at a constant Р _{а the} time is reduced during which the sound pressure exceeds the external forces that keep the bubble in equilibrium, when it can expand unlimitedly due to the gas contained in it. Naturally, in this case, the bubble manages to grow to smaller sizes, if its radius was close to critical, then it can degenerate into a pulsating one, provided that the amplitude of sound pressure P _a remains constant.

A decrease in R _{max of} cavitation cavities with increasing φ contributes to an increase in the pressure of the vapor – gas mixture in the bubble and to the beginning of collapse, which reduces the intensity of the shock waves.

Changing the frequency of oscillations affects the dynamics of the cavitation cavity, the distribution of cavitation cavities in the fluid volume and the threshold of cavitation. A decrease in the maximum size of cavitation bubbles with increasing frequency reduces the screening effect at the emitter – liquid interface and contributes to a more uniform distribution of bubbles in the liquid volume. Simultaneously with an increase in the frequency, the absorption coefficient of sound energy in a liquid increases, due to the presence of viscous friction forces, and, consequently, the speed of acoustic flows increases, which also become smaller. However, with increasing frequency, the cavitation threshold increases and losses in the converters increase, and this leads to a weakening of the cavitation efficiency.

It is undesirable to lower the frequency too much, as this sharply increases the noise and makes sound insulation more complicated, and also increases the weight of the converter due to its active link. The vast majority of industrial plants operate in the frequency range from 15 to 365 kHz. This is the optimal range in terms of technological effect, process efficiency and safety.

Theoretical and experimental studies have established the alternating sound pressure and sound strength necessary to excite cavitation in tap water at various frequencies of 15-365 kHz, which are presented in table 1.

Table 1
Variable sound pressure and sound strength required to induce cavitation in tap water at various frequencies KHz frequency To stimulate cavitation, it is necessary Sound pressure, kgf / cm ² Sound power, W / cm ² 15.0 0.5-2.0 0.16-2.6 175.0 4.0 10.0 365,0 7.0-20.0 33.0-270.0

From the analysis of the data in the table it follows that in order to excite cavitation at higher frequencies, a greater sound power is required. The increase in the necessary sound power with increasing frequency is due to the fact that the formation of cavitation requires a certain time, which depends on the size and shape of the cavitation nuclei, as well as on the existing static pressure.

It should be noted that until the completion of the outer electron layer, the sulfur atom lacks only two electrons. Hence, it should be expected that sulfur will combine with elements whose atoms easily give up electrons, i.e. with metals in liquid hydrocarbon fuels, and hydrogen.

When an ultrasonic field acts with the selected sound characteristics (frequency 15-365 kHz, variable sound pressure 0.5-20 kgf / cm ² and sound power 0.16-270 W / cm ² ) on water saturated with air, cavitation occurs in it . Owing to cavitation and the strong ionization associated with it, free radicals OH and H are formed in water, i.e. water is activated, releases dissolved oxygen and carbon dioxide from water. The increase in temperature and pressure during the collapse of cavitation bubbles, in turn, promotes the formation and recombination of radicals, the decomposition of liquid hydrocarbon fuels, and the synthesis of new chemical compounds in the form of associates and the release of sulfur. The spectrum of these reactions is as follows:

Na ₂ S + H ₂ O + CO ₂ = H ₂ S + Na ₂ CO ₃ ;

CaS + H ₂ O + CO ₂ = H ₂ S + C ₂ CO ₃ ;

FeS + H ₂ O + CO ₂ = H ₂ S + FeCO ₃ ;

ZnS + H ₂ O + CO ₂ = H ₂ S + ZnCO ₃ ;

Al ₂ S ₃ + 6H ₂ O = 2Al (OH) ₃ + 3H ₂ S;

2H ₂ S + O ₂ = 2S + 2H ₂ O.

Released sulfur along with salts is separated by ultrasound.

The binding energy in the associates of the molecules of the combustible mixture of the proposed composition is significant, therefore, they are quite stable and do not break down mechanically and with increasing temperature.

When a hydrostabilized hydrocarbon combustible mixture is heated to 150-250 ° C, the physical state of water and combustible components in the associates changes. The boiling point of water is 170-200 ° C lower than the boiling point of liquid hydrocarbon fuels; as a result, the combustible part of the associate drop still remains in a liquid state, while water is already turning into steam. Due to this, a drop of associate under the action of expanding water vapor breaks into smaller parts, microexplosion occurs. Such additional droplet crushing intensifies the fuel combustion process by increasing the evaporation surface, improving the process of mixing fuel with air and the catalytic effect of water vapor on fuel combustion.

Water vapor under the influence of high temperatures partially combines with the carbon of the fuel, and partially with the particles of the coke residue of incomplete combustion by the gasification reaction:

C + H ₂ O = CO + H ₂ -131.4 kJ.

In this case, carbon monoxide and hydrogen will easily oxidize at the end of the flame (in the secondary flame), and other hydrocarbon compounds (benzopyrene) will not form. This ensures almost complete combustion of hydrocarbon fuel, which compensates for the heat consumption for gasification of part of the carbon and coke residues with water. In addition, as a result of relatively low temperatures (1700-1900 ° C), the formation of nitrogen oxides in the core of the torch sharply decreases - by 3-4 times in comparison with conventional combustion methods.

Sodium oxide, which is in a flare in a gaseous state, is bound by an excess of water vapor by reaction

Na ₂ O + H ₂ O = 2NaOH,

as a result of which the resulting sodium hydroxide, interacting with carbon dioxide by the reaction:

2NaOH + CO ₂ = Na ₂ CO ₃ + H ₂ O,

forms sodium carbonate. Similarly, sulfur oxide and vanadium pentoxide are bound by sodium hydroxide by the reaction:

SO ₂ + 2NaOH = Na ₂ SO ₄ + H ₂ O;

V ₂ O ₅ + 2NaOH = 2NaVO ₃ + H ₂ O.

The resulting sodium carbonate, sulfate and vanadate are emitted with exhaust gases into the atmosphere.

As the temperature of the exhaust gases decreases below 100 ° C, sodium carbonate is hydrolyzed according to the equation:

Na ₂ CO ₃ + H ₂ O → NaHCO ₃ + NaOH.

In this case, the nitrogen dioxide formed during combustion of NO ₂ interacts with sodium hydroxide NaOH with the formation of a mixture of salts of nitric and nitrous acids according to the equation:

2NO ₂ + 2NaOH = NaNO ₃ + NaNO ₂ + H ₂ O,

thereby reducing the combined effect of the corrosive effects of sodium sulfate, vanadium pentoxide, sodium oxide and nitrogen oxides by about 3-4 times on the elements of the flow part of power plants.

For standard grades of liquid hydrocarbon fuels, for example kerosene, the net calorific value is 42900-43400 kJ / kg, and for the resulting hydrostabilized multicomponent mixture based on kerosene, it is in the range 37514-41084 kJ / kg, which is 5.34-12.55 % lower than kerosene. However, due to the fact that the obtained hydrostabilized hydrocarbon multicomponent mixture based on kerosene has a chemical underburning practically equal to zero, this decrease in the calorific value of the mixture is completely compensated by its completeness of combustion.

The proposed device is implemented in an industrial environment. On this device, the obtained hydrostabilized hydrocarbon combustible mixture was tested under production conditions on a steam boiler D-900 with a block-liquid burner BGZ - 0.5. The consumption of the mixture was 4.8 kg / h less compared to the hourly consumption of the standard fuel used (diesel fuel). The resulting mixture was also tested on a D-243L diesel engine in accordance with the manufacturer's specifications. The results are positive.

Using the proposed device allows to obtain hydrostabilized non-separable combustible mixtures of liquid hydrocarbon fuels with water (stable associates). The use of hydrostabilized hydrocarbon fuels obtained by the proposed device in burner-combustion units reduces soot formation by a factor of 2–3, and even eliminates it completely in some combustion modes, heat losses from chemical underburning of fuel are reduced, and become equal to zero with an excess air coefficient of 1, 05, the formation of nitrogen oxides is reduced by a factor of 3-4, and the corrosion rate of elements of the burner-furnace apparatus is reduced by a factor of 3, nozzle nozzles are coked.

Claims (1)

A device for producing a combustible mixture, including a container for a source of hydrocarbon fuel interconnected by a pipeline and shutoff valves with level meters and a mixing tank equipped with level meters, the output of which by means of a circulation pump is connected to the input of the dispersant, the output of which, in turn, is connected to the entrance of the mixing tank, characterized in that it is additionally equipped with a tank for softened water with a cooling element and a tank for its saturation with air from the meter and levels, pumps for supplying water through the meter from the above tanks to the dispersant and then to the mixing tank, the dispersant is made in the form of a sound emitter, and the mixing tank is docked with a sulfur removal unit equipped with a separating device and installed on the pipeline for supplying the obtained hydrostabilized fuel mixtures in the storage tank.