Method and apparatus for producing hydrogen and carbon nanofibres

Abstract

The invention relates to the chemical industry, and more particularly to technology for producing hydrogen and carbon nanofibres by the catalytic pyrolysis of light hydrocarbons, and can be used in various fields of activity (for example, the chemical industry, hydrogen energy production, and other industrial sectors). The technical result is an increase in the yield of hydrogen and of carbon nanomaterial in the form of carbon nanofibres. This technical result is achieved by the present solution to the problem of implementing a continuous process for producing hydrogen and carbon nanofibres in a device having a vertical reactor with a fluidized catalyst bed, where the continuous operation of the device is provided by a system for continuously supplying a catalyst and a system for discharging carbon nanofibres.

Description

[0001] METHOD AND APPARATUS FOR PRODUCING HYDROGEN AND CARBON NANOFIBERS.

[0002] The invention relates to the chemical industry, in particular to the technology of producing hydrogen and carbon nanofibers using the method of catalytic pyrolysis of light hydrocarbons, and can be used in various fields of application (for example, the chemical industry, hydrogen energy and other industries).

[0003] LEVEL OF TECHNOLOGY

[0004] There are several known methods for producing carbon nanomaterials and hydrogen based on the process of decomposition of hydrocarbon gases and their mixtures in the presence of catalysts with transition metals.

[0005] The prior art discloses a method for decomposing methane and a mixture of technical propane and butane according to GOST 20448-90 in the presence of a powdered catalyst containing nickel metals, the process being carried out in a wide temperature range from 600-1500°C (Patent of the Russian Federation No. 2353718, D01F 9 / 127, 9 / 10, priority from 25.07.2007, published on 27.04.2009).

[0006] Also known is a method for decomposing methane in the presence of active metals, which includes metals Co, Fe, Ni, Mo applied to MgO, S1O2 and AI2O3 in various combinations and percentages, at a synthesis temperature of 800-1000°C (Patent of the Russian Federation No. 2338686, C01B 31 / 00, priority from 01.03.2007, published on 20.11.2008).

[0007] In addition, a method is known for decomposing methane and a propane-butane mixture in the presence of active metals, which includes metals VI-VIII (for example, Fe, Co, Ni, Mg, Al, etc.), at a synthesis temperature of 550-1000°C (RU Patent No. 2373995, B01J 37 / 00, priority from 01.11.2008, published on 27.11.2009). A device for the corresponding purpose, described in the patent [RU No. 2462293], is also known for obtaining nanofibrous carbon materials and hydrogen from hydrocarbon gases, along with which a methane-hydrogen mixture is also formed. The known device consists of a frame on which an electric furnace is fixed, inside which a reactor is placed horizontally, and vibrators that provide vibration of the frame, due to which the carbon material moves from the place of loading the initial catalyst to the place of unloading the finished product. The continuous reactor itself includes a housing in the form of a horizontal pipe, closed on both sides by flanges.The reaction space is divided into sections by transverse partitions located at the bottom of the reactor uniformly along its entire length. Continuous supply of catalyst to the reactor is carried out through the catalyst inlet pipe. The initial hydrocarbon is fed to the reactor through the gas supply pipe, mixed with the reaction mixture, passing through a horizontal recirculation pipe, and contacts the vibro-fluidized catalyst bed, on the particles of which carbon material is formed. Heating of the catalyst bed to the reaction temperature is carried out using an electric furnace. Unloading of the finished carbon material is carried out through the lower pipe. Removal of gaseous products, in particular the methane-hydrogen mixture, is carried out through the upper pipe.

[0008] A device [Patent RU 198292 U1] for producing a methane-hydrogen mixture is known from the prior art, consisting of a frame on which an electric furnace is installed, inside which a reactor is placed horizontally, while the device is also equipped with flexible hoses - inlet and outlet sleeves, wound onto the inlet and outlet pipes, fixed at one end to the reactor, and the other on support bearings secured to the frame, a connecting rod connecting a large pulley located on the frame with a small pulley secured to an electric drive, which is fixed to the frame, a drive belt connecting the large pulley with the inlet pipe, characterized in that the device additionally contains an ejector with a diffuser and a flow damper, which are secured to the reactor along the central axis of the reactor zone.The device operates in horizontal mode and uses an ejector with a diffuser and a flow damper, which results in a long and deeper interaction of the initial gas flow with the catalyst due to its intensive mixing.

[0009] A common drawback of these methods is that the presented devices do not provide sufficiently high productivity for carbon material and hydrogen in the case of reactor scaling.

[0010] The closest in technical essence and achieved result is the method for producing nanofibrous carbon material and hydrogen, which is further considered as a prototype (Patent of the Russian Federation No. 2790169, C01B 32 / 15 B82Y 40 / 00 C01B 32 / 05 B01J 8 / 16 B01J 23 / 74). This source describes a group of solutions that are interconnected to such an extent that they form a single inventive concept, which is two independent methods for producing carbon nanomaterial and hydrogen (variants) and a device for implementing the claimed methods. In the first variant of the method for producing carbon nanomaterial and hydrogen, the technical result is achieved due to the fact that the method for producing carbon nanomaterial and hydrogen is carried out by decomposing hydrocarbons in the presence of catalysts containing transition metals of the iron subgroup, at a temperature of 550-800 ° C,by contacting the initial hydrocarbon gas with a vibro-fluidized catalyst bed moving in a horizontal direction, with continuous counter-current supply of the catalyst and the initial hydrocarbon gas and continuous removal of the resulting gaseous and solid reaction products, wherein the catalytic process is carried out in a vibro-fluidized catalyst bed divided along its movement by partitions impermeable to the dispersed material into two or more sections so that the resulting reaction product moves over the partition from one section to another, wherein the initial hydrocarbon gas is introduced into the base of the reactor, by means of a distribution manifold in contact with the spray nozzles. In the second version of the method for producing carbon nanomaterial and hydrogen, the technical result is solved due to the fact that the method for producing carbon nanomaterial and hydrogen is carried out by decomposing hydrocarbons in the presence of catalysts,containing transition metals of the iron subgroup, at a temperature of 550-800°C, by contacting the initial hydrocarbon gas with a vibro-fluidized catalyst bed moving in a horizontal direction, with a continuous counter-current feed of the catalyst and the initial hydrocarbon gas and a continuous removal of the resulting gaseous and solid reaction products, wherein the catalytic process is carried out in a vibro-fluidized catalyst bed divided along its course of movement by partitions impermeable to the dispersed material into two or more sections so that the resulting reaction product moves over the partition from one section to another, wherein the initial hydrocarbon gas is introduced into the reactor through two pipes independent of each other in the lower part of the reactor by means of a distribution manifold in contact with the spray nozzles, and in the upper part of the reactor by ensuring gas recirculation by the ejection method,with a gas recirculation rate of at least 3. The device is a horizontal reactor, the lower reaction space of which is divided into sections by transverse partitions impermeable to dispersed material, with a separated system for feeding and removing solid and gaseous reaction products, by implementing a catalytic reaction in combination with hydrocarbon gas recirculation modes due to the presence of an ejector device, in the vibro-fluidized bed mode, while the lower reaction space of the horizontal reactor is equipped with a collector and spray nozzles for uniform distribution of hydrocarbon gas into the base of the reactor.

[0011] PROBLEMS

[0012] The device specified as a prototype does not provide full interaction of the initial hydrocarbon gas flow through the collector system and spray nozzles with the catalyst, i.e. during reactor operation, a hydrocarbon gas flow breakthrough occurs through the catalyst layer. Thus, part of the hydrocarbon gas does not interact with the catalyst, and accordingly, the productivity of the device for hydrogen and carbon nanomaterial decreases.

[0013] The technical result of the invention is an increase in productivity for hydrogen and carbon nanomaterial, which is carbon nanofibers.

[0014] DISCLOSURE OF THE ESSENCE OF THE INVENTION

[0015] The technical result is achieved by solving the problem of carrying out the process of obtaining hydrogen and carbon nanofibers in a device with a vertical reactor with a boiling (fluidized) catalyst bed in a continuous mode, while the continuous operation of the device is ensured by a continuous catalyst supply system and a carbon nanofiber unloading system.

[0016] In order to achieve the technical result, it is proposed to implement a method for producing hydrogen and carbon nanofibers by catalytic pyrolysis of light hydrocarbons. The raw material, which is methane, natural gas, associated petroleum gas or a mixture of technical propane and butane, pre-cleaned from catalytic poisons and pre-heated to 500 ... 750 °C, enters the fluidized bed reactor, where a catalyst containing transition metals of the iron subgroup, with granule sizes from 0.1 to 3 mm, is also continuously fed, where the reaction occurs at a temperature of 500 ...750 °C and a pressure of 1 to 10 atm, wherein the catalyst is fed above a perforated mesh with a hole size of no more than 0.09 mm, located in the lower part of the reactor, and the raw material is fed below the perforated mesh, after which the catalyst, becoming covered with carbon material during the reaction, falls under its own weight onto the perforated mesh, which is part of the carbon product unloading system, where the carbon material is unloaded, and the hydrogen formed during the reaction and unreacted raw material are sent for separation, after which the hydrogen is removed as a product, and the unreacted raw material is recycled for preheating and fed back into the reactor.

[0017] The achievement of the technical result is ensured by an installation that includes a hydrocarbon feedstock feedstock unit, which is methane, natural gas, associated petroleum gas or a mixture of technical propane and butane, a heating furnace and a device for cleaning the feedstock from catalytic poisons, a reactor, a catalyst feeder, in which the catalyst feeder is connected directly to the reactor, and a perforated mesh with holes no larger than 0 is installed in the lower part of the reactor.09 mm, the catalyst is fed above the perforated mesh, and the feedstock is fed below the perforated mesh, wherein the perforated mesh is part of the carbon material (nano product) unloading system, and the outlet of the produced hydrogen and unreacted hydrocarbon feedstock from the reactor is diverted to a device for separating hydrogen from hydrocarbons, made according to the molecular sieve principle, from which the recirculation line of unreacted feedstock is diverted to the feedstock heating furnaces in front of the reactor, wherein a fluidized bed reactor is used as the reactor.

[0018] DESCRIPTION OF DRAWINGS

[0019] The invention is illustrated by drawings. Fig. 1 shows the general scheme of the installation. The installation consists of the following equipment: 1. Frame

[0020] 2. Raw gas supply unit

[0021] 3. Raw material preheating furnace

[0022] 4. Block for cleaning from catalytic poisons

[0023] 5. High-temperature raw material heating furnace

[0024] 6. Catalyst dispenser

[0025] 7. Reactor block

[0026] 8. Reactor heater

[0027] 9. Vertical rector

[0028] 10. Carbon product discharge system (type I and II)

[0029] Also, various options for the implementation of the carbon product unloading system are highlighted separately, where:

[0030] 11. Carbon product collection bin

[0031] 12. Perforated mesh

[0032] 13. Chamber with outlet valve

[0033] 14. Shoulder blades

[0034] 15. Rod (rotor)

[0035] 16. Rod rotation drive

[0036] 17. Gateway

[0037] 18. Cyclone

[0038] 19. Heat exchanger

[0039] 20. Device for separating hydrogen from hydrocarbons

[0040] DESCRIPTION IN STATICS

[0041] The unit consists of a number of elements and process devices. All elements of the unit are fixed on the frame (1). The frame (1), in particular, can be made in the form of a welded metal or prefabricated aluminum structure. The feed gas supply unit (2) is a set of devices, namely gas flow regulators with flow meters, pressure gauges, with purification from mechanical impurities, and, depending on the specific design of the unit, other shut-off and control valves. Further along the feedstock supply line there is a preheating furnace (3). After it there is a unit for purification from catalytic poisons (4) (mercaptans, odorants), which is an adsorber or several adsorbers. Next is a high-temperature feedstock heating furnace (5).The design of this part of the plant with two furnaces (3, 5) is due to the need to heat the gas before cleaning it from catalytic poisons to ensure an effective working temperature of the adsorbent, as well as to reduce the heat load on the high-temperature furnace for heating the raw material (5).

[0042] A catalyst dispenser (6), for example, of the screw type, is fixed in front of the upper part of the reactor (9) of the reactor block (7). The reactor block (7) consists of a heater (8), which is a casing around the reactor (9) itself. The vertical reactor (9) has a carbon product discharge system (10) in the lower part.

[0043] The reactor (9), in particular, can be made in the form of a vertical fluidized bed reactor with a variable diameter. The reactor can also be made in the form of a fixed bed reactor.

[0044] In particular, the plant can be implemented with two reactors (both fixed bed and fluidized bed) for the purpose of optionally increasing the plant's productivity or parallel testing of another operating mode or another catalyst without stopping the main production. The embodiments with a fixed bed reactor and with two reactors are not the subject of claims within the framework of the present invention.

[0045] The discharge system (10) is a mechanism located at the bottom of the vertical reactor (9) that ensures the extraction of carbon nanomaterial. The discharge system (10) in both variants disclosed below is intended only for the fluidized bed reactor.

[0046] According to the first embodiment of the invention, the carbon nanomaterial unloading system consists of a carbon product collection bin (11), a perforated mesh (12) with holes no larger than 0.09 mm, onto which the catalyst is fed from the catalyst dispenser (6), a horizontal chamber with an outlet valve (13), a blade (14), secured to a rod (rotor) (15), equipped with a rod rotation drive (16), located inside the reactor.

[0047] According to the second embodiment of the invention, the carbon product unloading system consists of a carbon product collection bin (11), a sluice (17), the surface of which is a perforated mesh (12) with holes no larger than 0.09 mm, onto which the catalyst is fed from the catalyst dispenser (6). The sluice can be one or two flaps that open vertically (downward).

[0048] After the reactor block (7) there is a cyclone (18), then a heat exchanger (19), a device for separating hydrogen from hydrocarbons (20). The device (20) is made according to the principle of a molecular sieve.

[0049] Then one process pipeline removes the product - hydrogen, and the other, removing hydrocarbons, is sent for recycling to the process feedstock supply line before the reactor block: for example, before the feedstock preheating furnace (3) or before the high-temperature feedstock heating furnace (5). DESCRIPTION IN DYNAMICS

[0050] The method according to the invention, implemented using the above-described installation, is carried out as follows. The feedstock (methane, natural gas, associated petroleum gas or a mixture of industrial propane and butane) is fed through the feedstock gas feed unit (2), heated to a temperature of 90 to 150 °C in the feedstock preheating furnace (3), and passes through the catalytic poisons purification unit (4), where it is purified from mercaptans and odorants. Then, the feedstock passes through the high-temperature feedstock heating furnace (5), where it is heated to a temperature of 500... 750 °C, while simultaneously with the feedstock being fed through the catalyst feed dispenser (6), consisting of at least metals of groups 9, 10, 11 of the periodic table of chemical elements with granule sizes from 0.1 to 3 mm, the catalyst is fed into the vertical reactor (9). In this case, the vertical reactor 9 is equipped with a carbon product unloading system (10).The feedstock enters the vertical reactor (9) heated by the reactor heater (8), the temperature inside which reaches 500-750°C at pressures from 1 to 10 atm, where a catalytic reaction occurs, described by the equation:.

[0051] Thanks to the perforated mesh (12) with holes no larger than 0.09 mm, the catalyst does not spill onto the bottom of the vertical reactor (9), and when the feedstock is supplied at a rate necessary to create a suspended catalyst bed, the catalyst bed goes into a boiling (pseudo-fluidized) mode, with the feedstock fully interacting with the catalyst without breakthrough, due to which the maximum possible conversion of the initial hydrocarbon for the loaded catalyst occurs at the specified process parameters. The quality of the process is determined by the technological modes of this process.

[0052] As a result of the chemical reaction, hydrogen and carbon are formed, which are granules from 0.2 to 4 mm, consisting mainly of carbon nanofibers. When the ratio of the mass of the loaded catalyst to the calculated mass of carbon nanofibers is not less than 1:50, the carbon nanofibers are unloaded thanks to the carbon product unloading system (10), namely:

[0053] The carbon product unloading system (10) according to the first embodiment of the invention operates as follows. The rotation of the blades (14) is started by starting the rotation drive (16) of the rod (15). The flow is provided to the horizontal chamber with the outlet valve (13), which is in the open state, due to which the carbon nanofibers are poured into the collection bin (I). After unloading the carbon nanofibers, the chamber with the outlet valve (13) is closed.

[0054] The carbon product discharge system (10) according to the second embodiment of the invention operates as follows. The catalyst, becoming covered with carbon, settles on the perforated mesh (12), which is the surface of the sluice (17). Then, when the settled catalyst accumulates, the sluice (17) is activated: the sluice doors open, discharge into the carbon product collection bin (11) occurs, and the doors close.

[0055] Next, hydrogen and undecomposed hydrocarbons pass through a cyclone (18), enter a heat exchanger (19), after which gases with a temperature of 25 to 60 °C enter a device for separating hydrogen from hydrocarbons (20), where hydrogen is separated from undecomposed hydrocarbons, which after separation are sent back for recycling, entering the process pipeline in front of the furnace (3) or furnace (5), and hydrogen is removed from the plant as a commercial product.

[0056] The achievement of the technical result and industrial applicability are demonstrated by the following examples:

[0057] Example 1. A catalyst containing 82 wt.% Ni, 8 wt.% Cu and 10 wt.% Al2O3 is fed into a vertical reactor through a catalyst feed system. At the same time, methane is fed through a feedstock feed unit and passes through a system for cleaning from catalytic poisons. Then the methane passes through a feedstock preheating unit, where it is heated to a temperature of 550 °C. Then the methane enters a vertical reactor heated by a furnace, the temperature inside which reaches 600 °C at 1 atm, while the catalyst is in a fluidized state. Methane, interacting with the catalyst, partially decomposes into hydrogen and carbon nanomaterial. The methane flow rate is set equal to 2000 l / h. The catalyst flow rate is 5 g / h. The catalyst particle size is 1 mm. The gaseous reaction products, which are a mixture of unreacted methane and hydrogen, are removed from the vertical reactor.Then the system passes through the carbon dust cleaning system, enters the heat exchanger, where the gases acquire a temperature of 45 °C, after which the gases enter the hydrogen separation system from hydrocarbons, which is a separation membrane, where hydrogen is separated from undecomposed methane, which after separation is fed back to the raw material preheating furnace. The productivity of carbon material is 0.25 kg / h, for hydrogen - 68 l / h. Unloading of carbon nanomaterial, which is granules with an average size of 3.5 mm, consisting mainly of carbon nanofibers, was carried out due to the work of the rotation of the blade system by starting the rotation system of the rod, which fell into a horizontal chamber with an outlet valve, which was in the open state, due to which the carbon nanofibers were poured into the collection bin, while the ratio of the mass of the loaded catalyst to the mass of carbon nanofibers was 1:185, i.e. the specific yield of carbon nanomaterial was 185 g per 1 g of catalyst.

[0058] Example 2. Similar to example 1, differs in that the process of unloading the carbon material is carried out through an unloading system consisting of a perforated hatch, which opened when the ratio of the mass of the loaded catalyst to the mass of the carbon nanofibers was 1:185, while the carbon nanofibers, under their own mass, fell into the lower part of the reactor and ended up in the collection bin.

[0059] Example 3. Similar to example 1, differs in that the productivity of carbon nanomaterial was 0.11 kg / hour, and of hydrogen - 29 l / hour. The specific yield of carbon nanomaterial was 181 g per 1 g of catalyst.

[0060] Example 4. Similar to example 1, differs in that the process is carried out at a temperature of 750°C. The productivity of carbon nanomaterial was 0.18 kg / hour, and of hydrogen - 48 l / hour. The specific yield of carbon nanomaterial was 314 g per 1 g of catalyst.

[0061] Example 5. Similar to example 2, differs in that the catalyst composition is 90 wt.% Ni and 10 wt.% Al2O3. The productivity of carbon nanomaterial was 0.18 kg / hour, and of hydrogen - 48 l / hour. The specific yield of carbon nanomaterial is 250 g per 1 g of catalyst.

[0062] Example 6. Similar to example 2, differs in that the catalyst composition is 82 wt.% Ni, 8 wt.% Cu and 10 wt.% Al2O3, the reactor pressure is 10 atm. The productivity of carbon nanomaterial was 0.08 kg / hour, and of hydrogen - 22 l / hour. The specific yield of carbon nanomaterial is 300 g per 1 g of catalyst.

[0063] Example 7. Similar to example 6, differs in that the reactor pressure is atmospheric, and natural gas was used as the initial hydrocarbon. The productivity of carbon nanomaterial was 0.3 kg / hour, and of hydrogen - 81 l / hour. The specific yield of carbon nanomaterial is 222 g per 1 g of catalyst.

[0064] Example 8. Similar to example 6, differs in that the reactor pressure is 3 atm, and a mixture of technical propane and butane at a temperature of 550 X2 was used as the initial hydrocarbon. The productivity of carbon nanomaterial was 0.08 kg / hour, and of hydrogen - 21 l / hour. The specific yield of carbon nanomaterial is 1090 g per 1 g of catalyst.

[0065] Example 9. Similar to example 4, differs in that the catalyst composition is 82 Ni, 8 Cu, 10 SiO2. The productivity of carbon nanomaterial was 0.36 kg / hour, and of hydrogen - 96 l / hour. The specific yield of carbon nanomaterial was 325 g per 1 g of catalyst.

[0066] Example 10. Similar to example 5, differs in that the pressure in the reactor is 5 atm at a temperature of 650 C. The productivity of carbon nanomaterial was 0.21 kg / hour, and of hydrogen - 57 l / hour. The specific yield of carbon nanomaterial is 300 g per 1 g of catalyst.

[0067] Example 11. Similar to example 10, differs in that the process temperature is 550 C. The productivity for carbon nanomaterial was 0.16 kg / hour, for hydrogen - 43 l / hour. The specific yield of carbon nanomaterial is 230 g per 1 g of catalyst.

[0068] Example 12. Similar to example 11, differs in that the catalyst composition is 90 Ni, 10 SiO2. The productivity of carbon nanomaterial was 0.17 kg / hour, and of hydrogen - 45 l / hour. The specific yield of carbon nanomaterial is 241 g per 1 g of catalyst.

[0069] Example 13. Similar to example 8, differs in that the pressure in the reactor is 5 atm at a temperature of 500 X2. The productivity of carbon nanomaterial was 0.1 kg / hour, and of hydrogen - 25 l / hour. The specific yield of carbon nanomaterial is 1308 g per 1 g of catalyst.

[0070] Example 14. Similar to example 7, differs in that the reactor pressure is 10 atm at a temperature of 750 C, and natural gas is used as the initial hydrocarbon. The productivity of carbon nanomaterial was 0.45 kg / hour, and of hydrogen - 121 l / hour. The specific yield of carbon nanomaterial is 333 g per 1 g of catalyst.

[0071] From the presented examples it follows that the invention allows to obtain hydrogen and carbon nanomaterial with high productivity. Based on the examples, the yields of products increased from 20 to 200% compared to the examples from the prototype.

[0072] Data on the main indicators of the process of obtaining hydrogen and carbon nanomaterial based on experimental data using the proposed method are given in Table 1.

[0073] Table 1.

Claims

CLAUSE OF INVENTION 1. A method for producing hydrogen and carbon nanofibers from the catalytic pyrolysis of light hydrocarbons, in which the raw material, which is methane, natural gas, associated petroleum gas or a mixture of technical propane and butane, pre-cleaned from catalytic poisons and mechanical impurities and pre-heated to 500... 750 °C, enters a fluidized bed reactor, into which a catalyst containing transition metals of the iron subgroup, with granule sizes from 0.1 to 3 mm, is also continuously fed, where a reaction occurs at a temperature of 500... 750 °C and a pressure of 1 to 10 atm., while the catalyst is fed above a perforated mesh with a hole size of no more than 0.09 mm., located in the lower part of the reactor, and the raw material is below the perforated mesh, after which the catalyst, becoming covered with carbon material during the reaction, falls under its own weight onto the perforated mesh, which is part of the carbon product unloading system, where the carbon material is unloaded, and the hydrogen formed during the reaction and unreacted raw material are sent for separation, after which the hydrogen is removed as a product, and the unreacted raw material is recycled for preheating and again fed into the reactor.

2. A method for producing hydrogen and carbon nanofibers according to claim 1, in which the raw material is preheated to a temperature of 90 to 150 °C, then purified from catalytic poisons and mechanically purified, then heated to a temperature of 500... 750 °C, after which it is fed into the reactor.

3. A method for producing hydrogen and carbon nanofibers according to claim 1, wherein the raw material is fed at a rate necessary to create a suspended catalyst bed.

4. A method for producing hydrogen and carbon nanofibers according to claim 1, in which, during the reaction, hydrogen and carbon are formed, which are granules from 0.2 to 4 mm, consisting predominantly of carbon nanofibers.

5. A method for producing hydrogen and carbon nanofibers according to claim 1, in which after the reactor, hydrogen and undecomposed hydrocarbons pass through a cyclone, enter a heat exchanger, after which they enter a device for separating hydrogen from hydrocarbons at a temperature of 25 to 60 °C.

6. A method for producing hydrogen and carbon nanofibers according to claim 1, in which the undecomposed raw material, after separation from hydrogen, is recycled and fed either before the raw material heating furnace or before the high-temperature raw material heating furnace.

7. A unit for producing hydrogen and carbon nanofibers, which includes a hydrocarbon feedstock feedstock unit, which is methane, natural gas, associated petroleum gas or a mixture of industrial propane and butane, a heating furnace and a feedstock purification unit for catalytic poisons and a device for purification from mechanical impurities, a reactor, a catalyst feeder in which the catalyst feeder is connected directly to the reactor, and a perforated mesh with openings no larger than 0 is installed in the lower part of the reactor.09 mm, which is part of the carbon material (nano product) unloading system, the catalyst feed inlet is located above the perforated mesh, and the feed inlet is located below the perforated mesh, and the reactor outlet of the produced hydrogen and unreacted hydrocarbon feedstock is diverted to a device for separating hydrogen from hydrocarbons, made according to the molecular sieve principle, from which the unreacted feedstock recirculation line is diverted to feedstock heating furnaces in front of the reactor, while a fluidized bed reactor is used as a reactor.

8. An installation for producing hydrogen and carbon nanofibers according to claim 7, in which the carbon nanomaterial unloading system consists of a perforated mesh, a horizontal chamber with a discharge valve, blades secured to a rod connected to a rod rotation drive, and a carbon nanomaterial collection bin.

9. An installation for producing hydrogen and carbon nanofibers according to claim 7, in which the carbon product unloading system consists of a carbon product collection bin and a gateway, the surface of which is a perforated mesh, wherein the gateway can be one or two flaps that open vertically downwards.

10. An installation for producing hydrogen and carbon nanofibers according to item 7, in which a cyclone is located after the reactor, then a heat exchanger, after which a device for separating hydrogen from hydrocarbons is located.

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