RU2671822C1 - Device and method for plasma-chemical hydrocracking and installation equipped therewith - Google Patents

Abstract

FIELD: technological processes.SUBSTANCE: claimed invention relates to a device and method for plasma-chemical hydrocracking of high-boiling hydrocarbons. Device for plasma-chemical hydrocracking is described, comprising a reactor having a reactor vessel, a chamber for unreacted hydrocarbons, a chamber for unreacted hydrocarbons, the working chamber and the partition separating the chamber for unreacted hydrocarbons and the working chamber, and in the partition there are channels for the communication of the working chamber with the chamber for unreacted hydrocarbons, plasma torch placed with the possibility of plasma flow feeding into the working chamber of the reactor, a tubular element to surround at least part of the longitudinal length of the plasma flow inside the reactor, the tubular element has an outer circumferential wall, an inner circumferential wall and a slit space between the two circumferential walls, connected to the supply of a hydrogen-containing medium, the inner circumferential wall has through channels for passage of the hydrogen-containing medium from the gap space to the plasma flow and thereby defines a mixing zone for mixing the plasma flow and the hydrogen-containing medium in the working chamber, the mixing zone together with the partition at least partially define the reaction zone inside the working chamber, which has a narrowing in the type of gas-dynamic nozzle, a supply for supplying liquid hydrocarbons into the unreacted hydrocarbons chamber limited by the partition, the partition on its side facing the reaction zone of the working chamber, forms a surface for spreading a layer of liquid hydrocarbons, the outlet for the resulting gaseous hydrocarbons, located in the chamber for the reacted hydrocarbons, the narrowing of the reaction zone of the working chamber is located in front of the outlet for the obtained gaseous hydrocarbons along the process stream, the outlet for unreacted liquid hydrocarbons, located in the chamber for unreacted hydrocarbons. Method of plasma-chemical hydrocracking, carried out with the use of this device, includes the following steps: creating a plasma stream, introducing a hydrogen-containing medium into the plasma stream and their reaction with obtaining a secondary hydrogen-containing coolant, injecting liquid hydrocarbons into the reactor, acting the layer of liquid hydrocarbons with secondary hydrogen-containing coolant for overheating and explosive boiling up and the vapor-droplet mixture obtained as a result of explosive boiling up with obtaining a reacting gas-vapor mixture from a vapor-droplet mixture of hydrocarbons and components of a secondary hydrogen-containing coolant, directing flow of the specified reacting gas-vapor mixture in the constriction made by the type of gas-dynamic nozzle and mixing the components of the mixture in the specified gas-dynamic nozzle with increasing degree of mixing as it approaches the exit of the gas-dynamic nozzle and obtaining gaseous hydrocarbons, releasing gaseous hydrocarbons from the gas-dynamic nozzle and thereby their expansion, removing gaseous hydrocarbons from the reactor. In addition, an invention concerning a plasma chemical hydrocracking unit comprising said plasma chemical hydrocracking device is described.EFFECT: increase in the intensity of vaporization of hydrocarbons during plasma-chemical hydrocracking and an increase in the rate of mixing of the components of vaporous hydrocarbons and the hydrogen-containing medium with a significant acceleration of the rate of chemical reactions of these components.22 cl, 6 dwg

Description

The claimed invention relates to a device and method for plasmachemical hydrocracking of high boiling hydrocarbons. In addition, the invention relates to an apparatus for plasmachemical hydrocracking containing the specified device for plasmachemical hydrocracking.

As an example of this kind of technology, publication RU 2,411,286 can be considered. This publication discloses a device for plasma hydrocracking, which contains a tubular reactor, a plasmatron, a supply of hydrocarbons to the lower part of the reactor, removal of unreacted liquid hydrocarbons from the reactor, and removal of the obtained gaseous hydrocarbons from the reactor. A baffle is provided in the reactor that divides the reactor into lower and upper chambers. A supply (pipe) for supplying water gas (steam) passes through the partition with a gap, and liquid hydrocarbons enter the upper chamber through the specified gap between the pipe and the partition from the lower chamber of the reactor. Water vapor through the inlet for supplying water gas in countercurrent is fed into the plasma stream so that the plasma stream diverges conically and falls exactly on the annular gap through which liquid hydrocarbons enter.

The specified device is aimed at the structural separation of the source of water gas from the plasma torch, which is realized due to the location of the plasma torch and the supply of water vapor on different sides of the reactor.

Moreover, in RU 2 411 286 it is additionally noted that water vapor is not only a means for changing the direction of the plasma jet flow from axial to radial, but also serves as a source of additional ions resulting from the pyrolysis of water gas in a collision with a plasma stream, which in turn, according to the authors, it should increase the intensity of the hydrocracking process.

However, this solution has a disadvantage consisting in low productivity due to the transfer of hydrocarbons to a vapor state during the evaporation process, the intensity of which is significantly inferior to the boiling process.

This problem is also recognized by the authors of the solution in accordance with RU 2,411,286, who, in their subsequent development disclosed in RU 2,574,732, tried to solve this problem by changing the principle of operation of the device. According to RU 2 574 732, water is sprayed by a plasma stream so that in the form of separate drops it enters the surface of liquid hydrocarbons. Due to this, microzones are formed with a temperature difference between the surface layer of hydrocarbons and water, which leads to the appearance at the boundaries of such zones of hydrocarbon molecules with higher kinetic energy than neighboring water molecules, which, in turn, leads to the breaking of intermolecular bonds and evaporation these hydrocarbon molecules.

However, this process is only local in nature and is associated with additional difficulties in maintaining the necessary specific conditions for the continuous course of the evaporation process. Accordingly, this solution also does not provide the proper intensity of hydrocarbon vaporization.

In addition, the problem of a low intensity of the process due to an ineffective evaporation process in both known solutions is exacerbated by the insufficient reaction rate of vaporous hydrocarbons and plasma / water vapor ions (splitting and hydrogenation). This is due to the short exposure time for the implementation of these reactions due to the rapid withdrawal of products from the reaction zone and the high decaying effect of the chemical reactions occurring in the vapor mixture, associated with a slight mixing of the components of the vapor mixture.

The objective of the present invention is to develop a solution that would increase the intensity of vaporization of hydrocarbons during plasmachemical hydrocracking and provide an increased mixing speed of components of vaporous hydrocarbons and a hydrogen-containing medium and thereby significantly accelerate the rate of chemical reactions of these components.

This problem is solved using a device for plasmachemical hydrocracking containing

a reactor having a reactor vessel, a chamber for unreacted hydrocarbons, a chamber for unreacted hydrocarbons, a working chamber and a partition separating the chamber for unreacted hydrocarbons and a working chamber, and in the partition there are channels for communicating the working chamber with the chamber for unreacted hydrocarbons,

a plasma torch arranged to feed a plasma stream into the working chamber of the reactor,

a tube-shaped element for surrounding at least a portion of the longitudinal extent of the plasma flow inside the reactor, wherein the tube-shaped element has an outer circumferential wall, an inner circumferential wall and a gap space between both circumferential walls connected to the supply of a hydrogen-containing medium, the inner circumferential wall having through channels for passage of a hydrogen-containing medium from the gap space to the plasma flow and thereby determines the mixing zone in the working chamber for mixing the plasma flow and hydrogen soda zhaschey medium, wherein the mixing zone together with a partition at least partially define the reaction zone within a processing chamber having a restriction on the type of the gas-dynamic nozzle,

an inlet for supplying liquid hydrocarbons (also called raw materials or feed hydrocarbons) to the unreacted hydrocarbon chamber bounded by a partition, the partition on its side facing the reaction zone of the working chamber forming a surface for spreading a layer of liquid hydrocarbons,

removal of the obtained gaseous hydrocarbons located in the chamber for the reacted hydrocarbons, wherein the narrowing of the reaction zone of the working chamber is located in front of the outlet of the obtained gaseous hydrocarbons along the process stream,

removal of unreacted liquid hydrocarbons located in the chamber for unreacted hydrocarbons.

The basis of the invention is the idea of using, not for the plasma itself, for the action on hydrocarbons, but for the production of a hydrogen-containing medium of a high-temperature and more reactive hydrogen-containing secondary coolant (hereinafter referred to as the secondary coolant torch). Moreover, this effect is carried out in such a way that the evaporation of liquid hydrocarbons occurs in the form of explosive boiling, and the high vibrational energy of the components of the secondary coolant that occurs during its formation is used to conduct chemical reactions with the components of the evaporated hydrocarbons under conditions in which the mixing speed is sufficiently high.

For the indicated preparation of a secondary coolant plume, a hydrogen-containing medium is introduced into the plasma stream. The introduction of a hydrogen-containing medium into the plasma stream is carried out using the specified tube-like element consisting of two circumferential walls and a gap space between them. As the specified hydrogen-containing medium, a liquid and / or gaseous hydrogen-containing medium is used.

Since in order to ensure the indicated input of the medium, the tube-shaped element covers the plasma jet, it must be cooled until conditions are created on its surface under which the temperature of the inner circumferential wall will not exceed the allowable temperature, above which the wall may burn out. For this cooling, the same hydrogen-containing medium is used, which is fed into the plasma stream. As indicated above, the hydrogen-containing medium may be gaseous, but for the best cooling of the tube-like element, a liquid hydrogen-containing medium is preferred.

Passing through the slit space, the specified hydrogen-containing medium absorbs the heat of the inner wall of the tube-shaped element and partially or almost completely evaporates and through the through channels enters the inner cavity of the tube-shaped element, creating a layer of still existing liquid on the surface of the inner wall. Under the action of the heat flux from the side of the plasma jet, the liquid hydrogen-containing medium evaporates and a protective layer is created from the liquid vapor above the liquid layer, that is, two protective layers are obtained: liquid and vapor. The incoming liquid hydrogen-containing medium, carried away by the plasma jet, spreads along the inner wall with a very thin layer. Due to evaporation, the thickness of the vapor layer above the liquid grows in the direction of the plasma flow to the area where the liquid evaporates completely. Since the vapor density is many times less than the density of the liquid, the thickness of the vapor layer is greater than the thickness of the liquid layer. Since the thermal conductivity of the vapor is many times less than the thermal conductivity of the liquid, the thermal resistance of the vapor layer is several times higher than the thermal resistance of the liquid layer. Therefore, the vapor layer is the main protective layer of the inner wall of the tube-like element. It should be understood that in the case of using a gaseous hydrogen-containing medium, only a vapor / gas protective layer will be present here.

The vapor of a liquid hydrogen-containing medium and / or gaseous hydrogen-containing medium is mixed with a plasma jet, heated to high temperatures and undergo pyrolysis with the formation of hydrogen radicals and to obtain a high-temperature plume of a secondary hydrogen-containing coolant.

Thus, the tube-shaped element is a part of the working chamber and a means restricting the plasma jet in space, receiving the heat flux from the plasma jet and preventing heat leakage from the plasma jet, supplying a hydrogen-containing medium for mixing with the plasma, and also a means of intensifying mass and heat transfer of the hydrogen-containing medium and plasma and means of focusing the torch of the secondary coolant, including by possible profiling of the cross section of the tube-like element.

The high-temperature secondary heat carrier torch obtained and sent using a tube-like element is an extremely effective means of heating liquid hydrocarbons, leading to their explosive boiling, which is the most intense process of evaporation of liquid hydrocarbons during their cracking.

The introduction of the specified liquid hydrocarbons into the reactor is carried out through channels made for communication of the working chamber with the chamber for unreacted hydrocarbons in the partition separating the chamber for unreacted hydrocarbons and the working chamber. Thus, the partition provides a surface for the spreading of liquid hydrocarbons, so that a free surface of liquid hydrocarbons is formed.

This surface of liquid hydrocarbons is affected by the high-temperature secondary heat transfer torch described above. The liquid phase of hydrocarbons due to the relatively low thermal conductivity and high heat flux from the side of the plume of the hydrogen-containing coolant in a thin surface layer goes into an overheated state, accompanied by periodic explosive boiling to obtain a vapor-droplet mixture stream. The term "vapor-droplet mixture" means the mixture obtained from explosive boiling from drops of liquid and steam of unreacted hydrocarbons.

Surface explosive boiling prevents overheating of the deeper layers of the liquid phase of hydrocarbons and their coking.

Most of the thermal energy spent on overheating of the liquid is converted into mechanical compression energy and kinetic energy of the moving specified vapor-droplet mixture. The consequence of explosive boiling of raw materials is the resulting pressure pulse. The experiments showed that the process of explosive boiling of a liquid is accompanied by characteristic undamped periodic fluctuations in temperature and pressure in the reaction zone. The physical mechanism of temperature fluctuations can be explained by shielding the heat flux from a torch of the secondary hydrogen-containing coolant to the surface of a liquid hydrocarbon due to a vapor-droplet mixture, and the mechanism of pressure fluctuations downstream by the pressure pulse mentioned above during explosive boiling. The pressure waves arising from explosive boiling accelerate the splitting of long hydrocarbon molecules.

After the demolition of the vapor-droplet mixture of hydrocarbons by the torch stream of the secondary coolant, the process repeats - the place of the removed liquid is occupied by a new hydrocarbon sublayer, rapid heating and repeated explosive boiling of the liquid phase of hydrocarbons. The process is repeated continuously.

The effective removal of the resulting vapor-droplet mixture from the torch action zone is also facilitated by the indicated tube-like element due to its directing secondary coolant action. In other words, the tube-shaped element is not only a means of providing an effective thermal and reaction effect on liquid hydrocarbons, but also at the same time a means for efficiently removing the obtained vapor-droplet mixture and thereby for faster subsequent boiling of a new portion of liquid hydrocarbons, i.e., a means of intensifying the process.

The proceeding hydrocracking process can conditionally be divided into the following stages: mixing of the components, cracking reaction, and hydrogenation reaction.

One of the factors causing the mixing of the components is the relative position of the surface of liquid hydrocarbons and the torch stream of the secondary coolant. Due to the fact that explosive boiling occurs with the ejection of a vapor-droplet mixture of the destroyed thin surface layer of liquid hydrocarbons at least partially in the direction of the coolant flow, partial interpenetration of the hydrogen-containing coolant plume and the vapor-droplet mixture of hydrocarbons formed as a result of explosive boiling also occur.

The second factor contributing to the mixing of the components is the turbulence that occurs during explosive boiling.

Due to the large difference in the temperatures of the secondary coolant and the vapor-droplet mixture of hydrocarbons due to explosive boiling, the mixing intensity in this zone is high. At the same time, hydrocracking of partially mixed raw materials takes place in the mixing zone to produce gaseous hydrocarbons as target products. It is clear that for the continuity of the phase transition process, a constant supply of energy is required, which is carried out by the indicated heat carrier torch onto the surface of liquid hydrocarbons at certain pressure and temperature on this surface, flow rate of liquid hydrocarbons and parameters of the plasma jet (plasma-forming medium, gas-dynamic pressure of the jet, distance from the nozzle exit , the consumption of the plasma-forming medium, the useful power of the plasma torch, the geometry of the plasma jet, etc.). The choice of process parameters allows you to configure the hydrocracking device to a specific ratio of the resulting products. The distribution of processes for obtaining a secondary hydrogen-containing coolant, explosive boiling, mixing, cracking, and hydrogenation over the space of the working chamber is the basis for actively controlling the hydrocracking process.

The rate of cracking and hydrogenation reactions is determined by temperature and pressure. At low temperatures, the reaction rate is relatively low and less than the mixing rate of the components. Downstream due to heat exchange with a coolant, a higher temperature develops. Here, cracking and hydrogenation reactions proceed at a high speed, and the process speed is determined by the mixing rate.

In order to achieve efficiency and high productivity of the hydrocracking process, the invention provides for a constriction made as a gas-dynamic nozzle, into which a vapor-droplet mixture stream carried by the secondary heat carrier torch is directed and in which the mixture components are mixed to produce a reactive gas-vapor mixture, and the degree of mixing is increased in said gas-dynamic nozzle as you approach the exit of the gas-dynamic nozzle.

Thus, the main purpose of the gas-dynamic nozzle according to the invention is to create a regime of effective mixing (mixing) of the components of a vapor-droplet mixture of hydrocarbons with the torch components of a secondary coolant to produce a reactive gas-vapor mixture.

This is achieved by the fact that the cross section along the length of the gas-dynamic nozzle changes by narrowing down to the pinch of the nozzle. In this case, prior to clamping, a substantially turbulent flow regime with acceleration of the flow is preferably realized, and behind the clamping there is a flow accompanied by deceleration of the flow due to its expansion. The constriction creates a negative pressure gradient (accelerating flow), the expansion behind the pinch creates a positive pressure gradient (slowing flow). Both effects intensify turbulence in the flow, provide a high mixing rate and, consequently, the rate of hydrocracking reactions, that is, affect the cracking and hydrogenation of hydrocarbons themselves, and at least partially affect the composition of the resulting hydrocracking products. This, in turn, reduces the conversion time of the feedstock (feed hydrocarbons) and, accordingly, the residence time of the feedstock and hydrocracking products in the working chamber, increases the productivity of the device and reduces its size, in particular, the dimensions of the reactor.

The expansion and braking of the stream of the reacted mixture emerging from the gas-dynamic nozzle leads to the completion of hydrocracking reactions in it and thereby fixation of the composition of hydrocracking products (the so-called "quenching") in the form of gaseous hydrocarbons, and the completion of the reaction occurs mainly at the initial stage of braking due to a sharp increase flow turbulence. Under the "gaseous hydrocarbons" in this description refers to a mixture of condensable and non-condensable hydrocracking products at a temperature at the outlet of the reactor.

To create a plasma flow, any type of low-temperature plasma generator can be used within the framework of the invention, which makes it possible to obtain a plasma jet, for example, an electric arc generator of direct or alternating current plasma, an RF generator, a microwave generator, and / or combinations thereof.

As the plasma-forming medium, various gases can be used, for example, air, nitrogen, hydrogen, gaseous hydrocarbons, inert gases, gas mixtures, for example, a mixture of carbon monoxide and hydrogen known as synthesis gas, as well as water vapor. However, the use of water vapor as a plasma-forming medium for producing a plasma jet in the claimed invention is preferred, since the steam-water plasma jet has the following features:

- steam-water plasma contains a multicomponent mixture of chemically, catalytically, electrically active particles, including oxygen, hydrogen, hydroxyl groups, clusters of water molecules in a molecular, atomic and ionized state;

- in the plasma torch with vapor-vortex stabilization of the electric arc there is a separation of plasma components, namely, hydrogen is concentrated along the axis of the plasma torch and near it, and by its properties the electric arc is mainly burning in hydrogen; heavier oxygen molecules are collected at the periphery of the arc channel; the intermediate position is occupied by hydroxyl groups; directly at the periphery near the walls of the arc chamber there is superheated water vapor in the form of clusters (associates) of water molecules; that is, steam-water plasma is a carrier of the active hydrogen necessary for the hydrogenation reaction;

- in the steam-water plasma jet flowing from the nozzle of the plasma torch, due to the decay of the vortex swirl and heat exchange with the environment, there is a decrease in the mass-average temperature along the jet, partial recombination of the plasma components, removal and scattering in the surrounding space of a multicomponent plume of active particles descending from the plasma jet ;

- the steam-water plasma jet is surrounded by a coat of superheated water vapor, which in the plume descending from the plasma jet is present in the form of clusters - large groups of water molecules that carry a significant electric charge carried from the plasma jet;

 - steam-water plasma jet is a powerful source of ultraviolet radiation, which is an activator of cracking of hydrocarbon feedstocks.

As already noted, a liquid or gaseous medium, or a combination thereof, can be used as a hydrogen-containing medium. Water, light hydrocarbons, oxygen-containing compounds of hydrocarbons are used as a liquid hydrogen-containing medium, and water vapor, gaseous hydrocarbons are used as a gaseous hydrogen-containing medium.

It turned out to be preferable to use water / water vapor as a hydrogen-containing medium, since the oxygen in its composition participates in the oxidation reaction with the components of the reacting gas-vapor mixture, which occurs with the release of heat, as a result of which the plasma torch power can be chosen lower.

In this case, it can be provided that the supply of a hydrogen-containing medium occurs only through the slotted space of the tube-shaped element. Alternatively, it is possible to supply a hydrogen-containing medium to the mixing zone of the working chamber both through the slotted space of the tube-shaped element, so directly into the mixing zone. In particular, it may be preferable to supply a liquid hydrogen-containing medium through the slit space of the tube-like element, and a gaseous hydrogen-containing medium directly into the mixing zone through an input located, for example, adjacent to the plasma torch nozzle.

In the framework of the invention, liquid hydrocarbons are supplied countercurrently to the flame of the hydrogen-containing coolant in such a way that the free surface of the liquid phase of hydrocarbons relative to the axis of the flame of the hydrogen-containing coolant is at an angle of 0 ... 90 °. This can be realized due to the fact that the plasma torch is located vertically or at some angle to the horizontal.

In accordance with the invention, the use of a gas-dynamic nozzle for discharging a reactive gas-vapor mixture in combination with the spatial position of the tube-like element allows the device to be made in horizontal, inclined or vertical designs, using various types of nozzles (annular gas-dynamic nozzle with a central body, flat slot nozzle, tubular or conical axisymmetric nozzle, etc.). The choice of the type of gas-dynamic nozzle is determined depending on the layout of the device.

In the framework of the invention, it may be provided that the tube-shaped element is made in the form of a separate part, which is installed in the plasma torch. Alternatively, the tube-like element may be integrally formed with the reactor vessel. It may also be provided that the tube-like element is located at a distance of the circumferential wall of the reactor vessel or, with its outer circumferential wall or inner circumferential wall, can form part of the reactor vessel / its circumferential wall.

Within the framework of the invention, a partition may be provided in the form of a bowl, conical body, flat plate, curved plate. The choice of the shape of the septum may be due to the desired shape of the gas-dynamic nozzle and the necessary conditions for the evaporation of liquid hydrocarbons and their flow in the nozzle and / or direction to it.

It is also envisaged within the framework of the invention that the baffle can completely form a gas-dynamic nozzle, i.e. the nozzle is made in the form of an internal channel (preferably, but not necessarily, for the case of a relatively massive partition) or a hole (preferably, but not necessarily, for the case of a relatively thin or thin-walled partition). Alternatively, the baffle can form a gas-dynamic nozzle only partially, and the other part is formed by a tube-shaped element and / or additional elements located inside the reactor, for example, additional internal walls of the reactor. Thus, the gas-dynamic nozzle, as already partially indicated above, can be in the form of an annular gas-dynamic nozzle with a central body, a flat slotted nozzle, a tubular or conical axisymmetric nozzle, etc.

The device according to the invention may optionally comprise a separator which serves to separate the obtained hot gaseous hydrocarbons by condensation. To do this, the specified separator communicates with the provided outlet for the removal of gaseous hydrocarbons from the reactor. Separation can be carried out with or without forced cooling. Such a separator allows you to return part of the obtained hydrocarbons back to the process in the form of a hydrogen-containing medium or in the form of liquid hydrocarbons. This contributes to the continuity of the process and the support of the necessary process conditions, in particular, the returned hydrocarbons already have an elevated temperature, since their preliminary heating is not required and there is no possible excessive cooling effect on the process. In addition, the separator can prevent the unwanted removal of excessively heavy hydrocarbon fractions along with light hydrocarbons already satisfying the requirements.

Within the framework of the invention, an additional supply for supplying a hydrogen-containing medium to the mixing zone of the working chamber of the reactor can also be provided. This inlet may be suitable for introducing a hydrogen-containing medium directly into the mixing zone or through a tube-shaped element. Direct supply to the mixing zone can be especially preferred if hydrocarbons returned from the separator connected after the reactor are used as the hydrogen-containing medium, since these hydrocarbons are already sufficiently heated (especially in the case of separation without forced cooling) and their supply through the tube-shaped element may not provide the desired cooling for the tubular element.

To regulate the working process in the claimed invention may be provided for regulation by changing the initial temperature (heating) of the raw material; changes in the residence time of raw materials in the reactor; changes in the power of the plasma generator, the flow rate of a hydrogen-containing liquid and a hydrogen-containing gas, pressure in the reactor, the level of raw materials in the reactor, etc. The specified regulation can be carried out by means known to the specialist.

To monitor the working process in the invention, various sensors can be used, in particular, a sensor for the level of raw materials in the reactor; raw material flow sensor; temperature sensor of raw materials at the inlet to the reactor, temperature sensor of raw materials in the reaction zone of the device; exhaust gas temperature sensor; pressure sensor in the reactor.

In the framework of the invention, it can be provided that the thickness or maximum thickness of the liquid hydrocarbon layer spreading over the septum is determined by the geometrical shape of the septum, for example, concave, curved or flat, or by the level of the location of the outlet of unreacted liquid hydrocarbons.

In the framework of the invention, the positioning of the plasma generator at the end of the tube-shaped element in combination with the power of the plasma generator deposited in the plasma jet makes it possible to control the temperature and gas-dynamic pressure of the plasma jet and the torch of the secondary hydrogen-containing coolant on the section of the open end of the tube-shaped element (facing the liquid hydrocarbons to be processed) .

The positioning of the tube-shaped element surrounding the plasma jet relative to the surface of the liquid hydrocarbon feedstock allows the creation of reactors of various spatial orientations and configurations. The position of the tube-shaped element relative to the septum and thereby relative to the surface of liquid hydrocarbons can be constantly set or can be changed depending on the necessary process parameters.

The problem is also solved by the method of plasma chemical hydrocracking, which is carried out using the device described above and is characterized by the following steps:

Creating a plasma flow,

Entering a hydrogen-containing medium into the plasma stream and their reaction to obtain a secondary hydrogen-containing coolant,

Injecting liquid hydrocarbons into the reactor,

The effect of the secondary hydrogen-containing coolant on the layer of liquid hydrocarbons for overheating and explosive boiling and on the vapor-droplet mixture resulting from explosive boiling to obtain a reacting vapor-gas mixture from a vapor-droplet mixture of hydrocarbons and components of the secondary hydrogen-containing coolant,

The direction of flow of the indicated reactive vapor-gas mixture to the constriction and mixing of the mixture components in the specified gas-dynamic nozzle as a gas-dynamic nozzle with an increase in the degree of mixing as it approaches the exit of the gas-dynamic nozzle and the production of gaseous hydrocarbons,

The release of gaseous hydrocarbons from the gas-dynamic nozzle and thereby their expansion, and then

The removal of gaseous hydrocarbons from the reactor.

This method is equally characteristic of all the advantages indicated above for the plasma chemical hydrocracking device.

According to the invention, it is possible to direct the reacting vapor-gas mixture in the nozzle narrowing at different speeds, the maximum possible flow rate of the reacting vapor-gas mixture being equal to the speed of sound. The specific speed and its setting is determined by the chemical composition of the reacting vapor-gas mixture and its temperature. Thus, the working chamber of the reactor can be configured both to the mode when the sound velocity of the flow in the nozzle is not reached, and to the mode when the speed of sound is reached in the nozzle. By changing the power of the plasma generator and, accordingly, the intensity of the process of converting a liquid hydrocarbon into a reacting gas-vapor mixture, a wide range of changes in the pressure drops across the nozzle is realized. This makes it possible to configure the operation of the device in many modes and control the composition of hydrocracking products.

The resulting hydrocracking products in the form of gaseous hydrocarbons, as already noted, contain a condensable phase (condensable products) and non-condensable hydrocarbon gases (non-condensable products). Therefore, preferably, the method may include the step of separating the condensed phase from hydrocarbon gases. Both condensable and non-condensed products (light hydrocarbons) can be targeted hydrocracking products and be discharged accordingly.

Preferably, it can also be provided that at least a portion of the gaseous hydrocarbons can be returned back to the process. Thus, part of the gaseous hydrocarbons can be fed back into the cavity of the tube-shaped element, i.e., into the mixing zone of the working chamber of the claimed device, in the form of a gaseous hydrogen-containing medium. In the case of using a separator for separating gaseous hydrocarbons into condensable and non-condensable products, at least part of the non-condensable products may be returned to the process in the form of a gaseous hydrogen-containing medium, and at least part of the condensed products may be returned to the process in the form of a liquid hydrogen-containing medium and / or part of the condensed products is in the form of liquid hydrocarbons (raw materials). The supply of condensed products back to the process as liquid hydrocarbons is preferable in the case of initial production and separation in the separator of relatively heavy hydrocarbons, which require additional processing into lighter hydrocarbons.

To increase the efficiency of the hydrocracking process, preheating of the hydrocarbon feed may preferably be provided as a preliminary step of the inventive process. At the same time, one proceeds from the established fact that the closer the temperature of the liquid hydrocarbons supplied to the reactor is to the surface temperature of the liquid during explosive boiling, the greater the mass transfer of the liquid (mass flux density of the liquid substance). For example, for fuel oil, in the temperature range from +25 ° С to 400 ° С, the dependence of the saturated vapor pressure on temperature is exponential and has a large gradient starting from 250-280 ° С, as a result of which it is preferable to feed the raw materials to a reactor with a temperature of 280-300 ° C, while the hydrocracking process itself is carried out at a temperature in a thin surface layer of the liquid phase of the feed in the evaporation zone, preferably from 430 to 570 ° C.

Also, the problem is solved using the installation for the implementation of plasmachemical hydrocracking, which includes at least one of the above-described device for plasmachemical hydrocracking.

This installation has the advantages that were discussed above when describing the claimed device and method.

The installation may include a device or devices for supplying a gaseous and / or liquid hydrogen-containing medium, which is fed into the mixing zone of the reactor and used as a hydrogen donor, a device for supplying liquid hydrocarbons to the reactor, and a device for withdrawing unreacted hydrocarbons from the reactor.

Preferably, the inventive installation may also include a device for preheating liquid hydrocarbons before they are fed to the reactor.

Also, the installation as an option may include a device for storing and feeding into the reactor an additional hydrogen-containing medium, for example, a gaseous hydrogen-containing medium, which is supplied directly to the mixing zone of the working chamber of the claimed device.

Preferably, the apparatus may include a device for separating condensable and non-condensable hydrocracking products contained in a mixture of gaseous hydrocarbons leaving the reactor.

Also, the inventive installation may include various means of monitoring and control / process control, for example, pressure sensors in the reactor, temperature sensors in the reactor, liquid hydrocarbon level sensors in the reactor, etc.

Further, the claimed invention is illustrated by examples of implementation using the drawings, which show:

Figure 1 is one embodiment of a device for plasmachemical hydrocracking in a sectional view;

Figure 2 a device for plasmachemical hydrocracking with figure 1 in perspective view;

Figure 3 is another embodiment of a device for plasmachemical hydrocracking in a sectional view;

Figure 4 is a device for plasmachemical hydrocracking with figure 3 in perspective view;

5 installation for plasmachemical hydrocracking, including a device for plasmachemical hydrocracking according to the invention;

6 is a schematic diagram of an apparatus for plasmachemical hydrocracking.

Figures 1 and 2 show one embodiment of a vertical embodiment of a plasma chemical hydrocracking device according to the invention. As the main components of the device for plasmachemical hydrocracking comprises a reactor 1, a plasmatron 2, a tube-shaped element 3 and a reactor wall 4.

The reactor 1 has or is a housing consisting of a side wall 5 and end walls 6, 7, namely the upper and lower end walls. The side wall 5 is closed around the perimeter and may have any shape, but is preferably cylindrical. The side wall 5 and the end walls 6, 7 are connected to each other and form a closed inner space of the reactor.

An inlet 8 is located in the end wall 7 of the reactor 1 for supplying liquid hydrocarbons to be treated. Alternative or additional supply 8 can be installed in the side wall 5 of the reactor.

In side wall 5 of the reactor there is a branch 9 for the removal of unreacted liquid hydrocarbons, as well as a branch 10 for the removal of gaseous hydrocarbons resulting from the processing. Additionally or alternatively, outlet 9 may also be located in the end wall 7 of the reactor, and outlet 10 may be located in the end wall 6 of the reactor. The throughput of these taps 9, 10 can be unregulated or adjustable through the use of conventional means of regulation known to those skilled in the art, for example, through valves.

The reactor 1 also has a baffle 4, which is located inside the reactor and divides its inner space into lower and upper regions.

The specified lower region of the reactor forms a chamber 11 for unreacted liquid hydrocarbons, which is filled with liquid hydrocarbons through the inlet 8, and excess liquid hydrocarbons are discharged through the specified outlet 9.

The upper region of the reactor includes a working chamber 12 of the reactor, in which the secondary coolant is formed, and liquid hydrocarbons are processed and converted into lighter gaseous fractions of hydrocarbons, and a chamber 13 for reacted hydrocarbons, which is connected to the working chamber 12 and which receives the working chamber 12 gaseous hydrocarbons. Further it will be explained in more detail.

The partition 4 in this case is made essentially in the form of an upwardly open bowl, which forms a receiving space for receiving a predetermined volume of unreacted liquid hydrocarbons to be treated, which spreads as a layer on the upwardly facing surface of the partition / bowl. For this, the partition 4 has through channels 14 through which liquid hydrocarbons pass from the chamber 11 for unreacted hydrocarbons located under the partition 4 to the specified receiving space of the partition.

The shape of the septum may differ from that shown in FIG. 1. For example, the partition may be a flat plate, a plate with a recess, a plate with an edge bent around the perimeter, a flat disk, etc.

The outlet 10 for the removal of gaseous hydrocarbons obtained after processing in the working chamber 12 is preferably located above the partition 4.

Further, in the shown embodiment, a tube-shaped element 3 is installed in the end wall 6 of the reactor, the lower end of which is located in the inner space of the reactor 1, and the upper end of which is connected to the plasmatron 2. It is obvious that other schemes for installing the plasmatron and tube-shaped element are possible. For example, a plasmatron can be mounted on the upper end wall of the reactor, and a tube-shaped element can be mounted on a plasmatron. Although it is shown in FIGS. 1 and 2 that the plasmatron and the tube-shaped element are arranged strictly vertically, it should be understood that a certain inclined arrangement of the plasmatron and / or tube-shaped element is possible.

As a plasma torch, for example, an electric arc plasmatron, a microwave plasmatron, an induction plasmatron, and the like can be used. In this case, the plasma torch produces a plasma jet with a mass-average temperature of up to 3000-6000 K. Air, inert gases, gaseous hydrocarbons, but preferably water vapor, are used as the plasma-forming medium.

The tube-shaped element 3 is made in the form of a double-walled pipe, in which the outer circumferential wall 15 and the inner circumferential wall 16 form a gap space 17 between themselves, which is closed from below.

The tube-shaped element 3 surrounds the plasma flow generated by the plasmatron 2 and introduces a hydrogen-containing medium into it. For this, the tube-shaped element 3 is connected to the supply 18 of a hydrogen-containing medium, through which the hydrogen-containing medium enters the specified slot space 17, and the inner circumferential wall 16 of the pipe-shaped element 3 is provided with through channels 19 for the passage of the hydrogen-containing medium from the gap space 17 to the plasma stream and mixing with him. Thus, the tube-shaped element 3 in the working chamber 12 of the reactor forms a mixing zone 20, in which the hydrogen-containing medium is mixed with the plasma stream to form the secondary coolant flame 21, with which the actual processing of liquid hydrocarbons takes place.

The tube-shaped element 3 shields the plasma flow from the surrounding internal space of the reactor and thereby avoids excessive heat loss. The hydrogen-containing medium, as already mentioned above, can be introduced into the slotted space 17 of the tube-shaped element 3 in liquid and / or gaseous form and, moreover, performs the function of cooling the inner circumferential wall 16 of the tube-shaped element 3, which helps to prevent its burning.

The lower end region of the tube-shaped element 3 ends in the indicated receiving space of the partition 4 above the level of liquid hydrocarbons spread there. An outer annular element 22 is provided in this lower end region, which in the case shown is a separate element, which can, in a manner known per se, detachably or integrally connect to the tube-like element 3. Alternatively, the ring element can be integral with the tube-like element 3.

The annular element 22 has an arcuate section 23, which, together with the arcuate section 24 of the inner surface of the partition / bowl, forms a tapering channel in the form of a gas-dynamic nozzle 25 (the so-called annular nozzle with a central body), which is clearly seen in Fig. 1.

It should be noted that this gas-dynamic nozzle can be formed by an arcuate section of only one of the elements (an annular element or a partition), while the other element has a reciprocal section, which is not arcuate, but, for example, flat. In addition, the sections forming the gas-dynamic nozzle do not have to have an arched contour, but can be made with a direct continuous contour, or have a contour formed by alternating straight and / or curved parts of different slopes. In addition, the specified tapering channel or gas-dynamic nozzle can be performed not by a continuous annular passage (the so-called annular nozzle), but, for example, in the form of a spiral channel, for which there must be corresponding spiral protrusions on one or both sections forming this channel.

Thus, the specified tube-shaped element 3 with the annular element 22 and the baffle 4 together define the reaction zone 26 of the working chamber 12 of the reactor, in which the secondary hydrocarbon, created upstream in the tube-shaped element of the torch 21, acts on liquid hydrocarbons, their rapid heating and explosive boiling, and moving (shown by arrows in FIG. 1) the resulting reacting vapor-gas mixture through the gas-dynamic nozzle 25 and, finally, exit from this nozzle. The spiral form of the nozzle or its portions indicated above as an option can contribute to additional mixing and thereby more complete reaction between the components of the gas-vapor mixture.

The specified exit from the gas-dynamic nozzle and, accordingly, from the specified reaction zone of the working chamber ends in the chamber 13 for reacted hydrocarbons. The chamber 13 for reacted hydrocarbons serves to receive the obtained gaseous hydrocarbons from the working chamber and expand them, as a result of which the reactions in the reacting gas-vapor mixture are largely stopped and thereby undesirable reverse reactions are eliminated.

The hot gaseous hydrocarbons thus fixed are then discharged from the chamber 13 for the reacted hydrocarbons through the outlet 10 for the obtained gaseous hydrocarbons.

In the shown embodiment, it is optionally provided that said outlet 10 for the obtained gaseous hydrocarbons is implemented as a plurality of holes in the side wall 4 of the reactor, which can optionally lead to an adjacent hot separator to prevent the entrainment of vapors of the heaviest hydrocarbons with a fast moving light stream gaseous hydrocarbons. Hot separation involves condensation and mechanical separation of the heavy hydrocarbon fraction due to a slight and natural decrease in pressure at the outlet of the reactor. There is no forced cooling in the hot separator. The separated hydrocarbon fraction may be the desired cracking product or returned to the process as a feed. However, as already noted, the presence of a hot separator is not necessary, but is provided only as one of the preferred options of the present invention.

A mixture of gaseous hydrocarbons enters a cold separator, where hydrocarbon gases and light hydrocarbon condensate are separated from it by forced cooling.

Hot and cold separation can be carried out as part of a known rectification process. As an option, it can also be provided that part of the gaseous and / or condensed light hydrocarbons can be returned to the process as a hydrogen-containing medium supplied to the mixing zone.

To control the process in a device for plasmachemical hydrocracking, agents known to the person skilled in the art can be used. In particular, Figs. 1 and 2 show a temperature sensor 27 of the reaction zone, as well as a port 28 for a temperature sensor for a gas-vapor mixture and a port 29 for a pressure sensor for a gas-vapor mixture. These and other sensors can be provided as an option. Various control possibilities may also be provided, for example, means may be provided for raising / lowering the septum and / or tube-like means to control the filling volume of the reaction chamber with liquid hydrocarbons and / or to control the size of the gas-dynamic nozzle. Means may also be provided for changing the intake and / or removal of unreacted liquid hydrocarbons and means for changing other parameters of the claimed device. These means of control or regulation, however, are not the subject of the claimed invention and therefore are not described in more detail here.

Figure 3 and 4 presents another embodiment of the claimed invention, which differs from the embodiment according to figures 1 and 2 in the horizontal orientation of the device for plasmachemical hydrocracking.

The reactor 1 here is also a housing with a side, preferably cylindrical wall 5 and two end walls 6, 7, namely the left and right end walls.

A plasma torch 2 is installed in the first end wall 6, which is located at a certain angle to the horizontal. In the second end wall 7 of the reactor, a branch 10 for the obtained gaseous hydrocarbons is provided.

The tube-like element 3, as in the embodiment of FIG. 1, is also double-walled, with a gap space 17 formed between two circumferential walls 15, 16. However, the inner circumferential wall 16 is integrally formed here with the side wall 5 of the reactor, in particular section of the side wall 5 of the reactor. Alternatively, the inner circumferential wall of the tube-like element may be embedded in the side wall of the reactor in a specially provided receiving location.

Through the through holes 19 made in the inner circumferential wall 16 of the tube-shaped element 3, a hydrogen-containing medium is introduced from the slotted space 17 of the tube-shaped element 3 into the plasma stream created by the plasmatron 2.

The partition 4 here is made in the form of a flat plate, although alternatively other forms of the partition (for example, a concave plate, a trough plate, etc.) can also be selected.

Under the partition 4 there is a chamber 11 for unreacted hydrocarbons, which enter through inlet 8, and their excess is discharged through outlet 9 for unreacted hydrocarbons.

Above the partition 4, the working chamber 12 of the reactor is located, and the partition 4 here passes from one end wall of the reactor 6 through the mixing zone 20, in which the introduced hydrogen-containing medium is mixed with the plasma flow, then along the reactor in the direction of the other end wall 7 of the reactor and ends at some distance from the second end wall 7.

Thus, the reaction zone 26 of the working chamber 12 is defined here essentially by the mixing zone 20, the partition 4 and the side wall 5 of the reactor.

The partition 4 between the mixing zone 20 and its end facing the second end wall 7 is provided at least in separate areas with through channels 14 (not shown here) for passing liquid hydrocarbons from the chamber 11 for unreacted hydrocarbons into the working chamber 12 and spreading there partition surface 4.

At least one, but in this case, two additional inner walls 30, 31 of the reactor are provided in the reactor section between the end of the partition 4 and the second end wall 7, which form a narrowing in the form of a slit-like gas-dynamic nozzle 25, into which the torch carried in the mixing zone is directed secondary coolant flow reacting vapor-gas mixture. This slotted gas-dynamic nozzle 25 serves for preliminary compression and acceleration of the flow, as well as subsequent expansion and deceleration of the flow, and thereby provides conditions for very intensive mixing of the components inside the flow of the reacting vapor-gas mixture and thereby the accelerated and more complete hydrocracking reaction.

The specified expansion and deceleration of the vapor-gas mixture, as in the case of the gas-dynamic nozzle 25 in the device of FIG. 1, occurs already behind the slot-hole gas-dynamic nozzle 25 and, thus, in the inlet zone of the chamber 13 for reacted hydrocarbons, which is formed - when viewed in the direction of flow - between gas-dynamic nozzle 25 and the second end wall 7 of the reactor, as in the device in figure 1. This expansion and retardation of the stream exiting the gas-dynamic nozzle leads to a substantially completed hydrocracking process in it and thereby to fixing ("quenching") of the gaseous hydrocarbons resulting from hydrocracking, which then leave the reactor through the outlet for the reacted hydrocarbons.

The additional internal walls 30, 31 of the reactor according to FIG. 3 extend laterally, however, their inclined passage is also possible, so that before exiting the nozzle 25 a more elongated channel arises, in which reactions can additionally proceed in the reacting gas-vapor mixture.

Said outlet 9 for unreacted hydrocarbons according to FIG. 3 is located after the partition 4 in the transition zone of the gas-dynamic nozzle 25 to the chamber 13 for unreacted hydrocarbons. However, alternatively, it can also be located under the partition 4.

It is clear that the gas-dynamic nozzle can be made here not only in the form of a flat slotted nozzle, but in another form, for example, in the form of a tubular nozzle, an annular nozzle, or the like.

Figure 3 also shows an optional hot separator 32 connected to the reactor 1 and connected to the outlet 10. The hot separator 32 provides the expansion of gaseous hydrocarbons leaving the reactor and their partial condensation. The condensed part of the hydrocarbons is discharged through the drain 33, and the non-condensed part of the hydrocarbons is discharged through the outlet 34.

Figure 5 presents a General view of the installation for plasmachemical hydrocracking, which includes a device for plasmachemical hydrocracking according to the invention.

The plasma chemical hydrocracking unit in this case is mounted inside a supporting frame including a base 35, as well as vertical 36 and horizontal beams 37. The specified frame can be equipped with walls and can therefore be a ready-made shipping container. Alternatively, the frame can be mounted inside the production room or the installation can be performed without the specified frame, so that its nodes are mounted directly in the production room.

Installation for plasmachemical hydrocracking contains a device for plasmachemical hydrocracking according to the invention, which in the presented embodiment is made in accordance with figure 1. So, in figure 5 you can see the plasmatron 2 and the reactor 1.

In the embodiment shown in FIG. 5, the plasma chemical hydrocracking installation comprises a device 38 for preheating liquid hydrocarbons, a pump 39 for supplying liquid hydrocarbons to the reactor 1, a device for supplying a liquid hydrogen-containing medium to the reactor 1, a device for supplying a gaseous hydrogen-containing medium to the reactor 1 , a device 41 for separating condensable and non-condensable products (for example, in the form of a cold separator separated from the reactor 1), a reservoir 42 for collecting cracked products, a device 43 for the withdrawal of unreacted hydrocarbons from the reactor (for example, branch 9), means 44 (plasma-generating steam generator), 45 (plasma generator power supply), 46 (reverse water supply system for cooling the plasma generator, power supply, cold separator), etc. in the form of equipment, combined structurally and functionally to convert electrical energy into heat with a plasma stream.

It is clear that simpler versions of the claimed installation are quite possible, in which some of these devices can be abandoned. For example, you can use equipment that is already available at the place of use of the installation for plasma chemical hydrocracking, in particular, a pump, heater, etc. As an option, this installation can also be equipped with its own power plant to provide the energy necessary for its operation.

Figure 6 shows a schematic flow diagram of an installation for plasmachemical hydrocracking, an example of which below will explain the process of its operation and some additional technical features of the installation.

On line I, liquid hydrocarbons enter a pump 39, which feeds them through a preheater 38 to reactor 1. In the reactor, liquid hydrocarbons fill a chamber for unreacted hydrocarbons and then enter a working chamber 12 of the reactor.

The predetermined flow of hydrocarbons is provided by the pump 39. The entire hydrocarbon transport line is preferably thermally insulated, the working part of the pump, as well as the connecting pipelines, are preferably provided with electric heating.

Plasma-forming medium 2 is supplied via line II to a plasma torch 2 (for example, air, inert gases, gaseous hydrocarbons, but preferably water vapor). The plasma stream generated by the plasmatron 2 is fed into the mixing zone of the working chamber of the reactor 1.

On line III, using a device 47 for supplying a liquid hydrogen-containing medium (for example, a pump with a flow regulator), a liquid hydrogen-containing medium, preferably water, is fed into the reactor 1 (in the mixing zone of the working chamber).

Via line IV, a gaseous hydrogen-containing medium is supplied to a reactor 1 (into the mixing zone of the working chamber) using a suitable device 48 for supplying a gaseous hydrogen-containing medium. This line is provided here as an option or only for periodic use.

Cracking products (gaseous hydrocarbons) from the reactor enter the device 41 for separating condensable and non-condensable products, in which the first stage is the cooling of gaseous hydrocarbons and the condensation of light fractions, and in the second stage, the resulting gas-liquid mixture of hydrocarbons is divided into two parts - liquid and gaseous. The device 41 can be made, for example, in the form of the above-mentioned cold separator or have it in the form of one of the nodes. Optionally, the flow rate of gaseous hydrocarbons and the pressure in the reactor are controlled here by means of a regulating device 49 (for example, a needle valve) connected in line between the reactor 1 and the device 41.

After separation of the condensable and non-condensable cracked products, the condensed products are fed via line VI to the reservoir 42 for collecting the (liquid) cracked products, and the non-condensable products (gaseous hydrocarbons) can be partially or completely returned to the reactor 1 as a hydrogen-containing medium using said device 48 or can be removed from the process along line V. Line V may include a filter (for example, to prevent gas entrainment of the liquid fraction), a gas meter to determine its amount, fire pregraditel and gas burner, or discharge into the atmosphere.

Liquid hydrocarbons are fed to reactor 1 continuously. Unreacted hydrocarbons are removed from the reactor and using the device 43 for outputting unreacted hydrocarbons and sent for re-processing.

Claims (35)

1. Device for plasmachemical hydrocracking, containing a reactor having a reactor vessel, a chamber for unreacted hydrocarbons, a chamber for unreacted hydrocarbons, a working chamber and a partition separating the chamber for unreacted hydrocarbons and a working chamber, and in the partition there are channels for communicating the working chamber with the chamber for unreacted hydrocarbons, a plasma torch arranged to feed a plasma stream into the working chamber of the reactor, a tube-shaped element for surrounding at least a portion of the longitudinal extent of the plasma flow inside the reactor, wherein the tube-shaped element has an outer circumferential wall, an inner circumferential wall and a gap space between both circumferential walls connected to the supply of a hydrogen-containing medium, the inner circumferential wall having through channels for passage of a hydrogen-containing medium from the gap space to the plasma flow and thereby determines the mixing zone in the working chamber for mixing the plasma flow and hydrogen soda zhaschey medium, wherein the mixing zone together with a partition at least partially define the reaction zone within a processing chamber having a restriction on the type of the gas-dynamic nozzle, an inlet for supplying liquid hydrocarbons to the unreacted hydrocarbon chamber bounded by the baffle, the baffle on its side facing the reaction zone of the working chamber forming a surface for spreading the liquid hydrocarbon layer, an outlet for the obtained gaseous hydrocarbons located in the chamber for the reacted hydrocarbons, wherein the narrowing of the reaction zone of the working chamber is located in front of the outlet for the obtained gaseous hydrocarbons along the process stream, a tap for unreacted liquid hydrocarbons located in the chamber for unreacted hydrocarbons. 2. The device according to claim 1, characterized in that the plasma torch is located vertically or at an angle to the horizontal. 3. The device according to claim 1, characterized in that the tube-shaped element is made in the form of a separate part installed in the reactor. 4. The device according to claim 1, characterized in that the tube-shaped element is made in one piece with the reactor vessel. 5. The device according to claim 1, characterized in that the partition is made in the form of a bowl. 6. The device according to claim 1, characterized in that the partition is made in the form of a flat plate. 7. The device according to claim 1, characterized in that the gas-dynamic nozzle is made in the form of an annular gas-dynamic nozzle with a central body, a flat slotted nozzle, a tubular or conical axisymmetric nozzle. 8. The device according to claim 1, characterized in that the nozzle is formed in the partition. 9. The device according to claim 1, characterized in that the nozzle is formed by a partition and a tube-shaped element. 10. The device according to claim 1, characterized in that the nozzle is formed using internal walls located inside the reactor. 11. The device according to claim 1, characterized in that it provides a separator that communicates with the said outlet for the removal of gaseous hydrocarbons and serves to separate the resulting hot gaseous hydrocarbons through condensation. 12. The device according to claim 1, characterized in that there is an additional supply for supplying a hydrogen-containing medium to the mixing zone directly or through a tube-shaped element. 13. The method of plasma chemical hydrocracking, carried out using the device according to claim 1, comprising the following steps: creating a plasma flow, introducing a hydrogen-containing medium into the plasma stream and their reaction to obtain a secondary hydrogen-containing coolant, introduction of liquid hydrocarbons into the reactor, the effect of the secondary hydrogen-containing coolant on the layer of liquid hydrocarbons for overheating and explosive boiling and on the vapor-droplet mixture resulting from explosive boiling to obtain a reacting vapor-gas mixture from a vapor-droplet mixture of hydrocarbons and components of the secondary hydrogen-containing coolant, the direction of the flow of the indicated reactive gas-vapor mixture in the narrowing and mixing of the mixture components in the specified gas-dynamic nozzle as a gas-dynamic nozzle with an increase in the degree of mixing as it approaches the exit of the gas-dynamic nozzle and obtaining gaseous hydrocarbons, the release of gaseous hydrocarbons from the gas-dynamic nozzle and thereby their expansion, removal of gaseous hydrocarbons from the reactor. 14. The method according to p. 13, characterized in that it includes the step of preheating liquid hydrocarbons before they are fed to the reactor. 15. The method according to item 13, wherein the unreacted hydrocarbons discharged from the reactor are returned to the reactor for processing. 16. The method according to item 13, wherein the gaseous hydrocarbons discharged from the reactor are separated into condensable and non-condensable products. 17. The method according to clause 16, characterized in that at least a portion of the condensable or non-condensable products are returned back to the reactor as a hydrogen-containing medium for introduction into the plasma stream. 18. The method according to clause 16, wherein at least a portion of the non-condensable products are diverted as the target product. 19. The method according to clause 16, characterized in that at least a portion of the condensed products is diverted as the target product. 20. The method according to clause 16, characterized in that part of the condensed products are returned back to the reactor as liquid hydrocarbons for reprocessing. 21. Installation for plasmachemical hydrocracking, comprising at least one device for plasmachemical hydrocracking according to claim 1. 22. Installation according to item 21, characterized in that it is mounted inside a transport container.

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