EP4058403A1 - Procédé et dispositif de production d'hydrogène et de carbone pyrolytique à partir d'hydrocarbures - Google Patents

Procédé et dispositif de production d'hydrogène et de carbone pyrolytique à partir d'hydrocarbures

Info

Publication number
EP4058403A1
EP4058403A1 EP20807329.6A EP20807329A EP4058403A1 EP 4058403 A1 EP4058403 A1 EP 4058403A1 EP 20807329 A EP20807329 A EP 20807329A EP 4058403 A1 EP4058403 A1 EP 4058403A1
Authority
EP
European Patent Office
Prior art keywords
reactor
hydrocarbons
inert gas
carbon
electrodes
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
EP20807329.6A
Other languages
German (de)
English (en)
Inventor
Nicolai Antweiler
Karsten BÜKER
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ThyssenKrupp AG
ThyssenKrupp Industrial Solutions AG
Original Assignee
ThyssenKrupp AG
ThyssenKrupp Industrial Solutions AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by ThyssenKrupp AG, ThyssenKrupp Industrial Solutions AG filed Critical ThyssenKrupp AG
Publication of EP4058403A1 publication Critical patent/EP4058403A1/fr
Pending legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
    • C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
    • C01B3/28—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using moving solid particles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
    • B01J6/008—Pyrolysis reactions
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/05—Preparation or purification of carbon not covered by groups C01B32/15, C01B32/20, C01B32/25, C01B32/30
    • C—CHEMISTRY; METALLURGY
    • C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
    • C09C—TREATMENT OF INORGANIC MATERIALS, OTHER THAN FIBROUS FILLERS, TO ENHANCE THEIR PIGMENTING OR FILLING PROPERTIES ; PREPARATION OF CARBON BLACK  ; PREPARATION OF INORGANIC MATERIALS WHICH ARE NO SINGLE CHEMICAL COMPOUNDS AND WHICH ARE MAINLY USED AS PIGMENTS OR FILLERS
    • C09C1/00—Treatment of specific inorganic materials other than fibrous fillers; Preparation of carbon black
    • C09C1/44—Carbon
    • C09C1/48—Carbon black
    • C09C1/50—Furnace black ; Preparation thereof
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0266—Processes for making hydrogen or synthesis gas containing a decomposition step
    • C01B2203/0272—Processes for making hydrogen or synthesis gas containing a decomposition step containing a non-catalytic decomposition step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0266—Processes for making hydrogen or synthesis gas containing a decomposition step
    • C01B2203/0277—Processes for making hydrogen or synthesis gas containing a decomposition step containing a catalytic decomposition step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/085—Methods of heating the process for making hydrogen or synthesis gas by electric heating
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0872—Methods of cooling
    • C01B2203/0877—Methods of cooling by direct injection of fluid
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1241—Natural gas or methane
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/16—Controlling the process
    • C01B2203/169—Controlling the feed

Definitions

  • the invention is in the field of the pyrolytic decomposition of hydrocarbons and in particular of methane to hydrogen and pyrolytic carbon and relates in particular to a new method for a corresponding conversion in which the reactor has two electrodes spaced apart in the direction of flow of the hydrocarbons and wherein in the area of the reactor an inert gas component is fed in between the electrodes over the entire reactor cross-section.
  • the invention also relates to a device for carrying out a corresponding method.
  • hydrogen can be obtained from hydrocarbon fuels through oxidative and non-oxidative conversion processes.
  • Oxidative transformations involve the reaction of hydrocarbons with Oxidizing agents such as water, oxygen or combinations of water and oxygen (steam reforming, partial oxidation and autothermal reformation processes).
  • Oxidizing agents such as water, oxygen or combinations of water and oxygen (steam reforming, partial oxidation and autothermal reformation processes).
  • synthesis gas a mixture of hydrogen and carbon monoxide (synthesis gas) is formed in these processes, from which the hydrogen is separated off by gas conditioning (water gas shift reaction) and preferably oxidation reactions and CO 2 removal stages.
  • the total C0 2 emissions from these processes reach up to 0.5-0.6 m 3 per m 3 of hydrogen produced.
  • Non-oxidative processes involve the thermal decomposition (or dissociation, pyrolysis, cracking) of hydrocarbons into hydrogen and carbon.
  • the thermal decomposition of natural gas has been used for several decades as a means of producing carbon black, with hydrogen being an additional product of value that occurs in the process.
  • hydrocarbon vapor is decomposed into hydrogen and soot particles at a temperature of about 1400 ° C. over a preheated contact.
  • the process was carried out, for example, as a semi-continuous (cyclic) process using two tandem reactors.
  • No. 2,926,073 describes an improved device for producing soot and hydrogen from hydrocarbons by a continuous thermal decomposition process.
  • the Kvaerner Company from Norway has developed a methane decomposition process that generates hydrogen and soot at high temperatures (CB&H process, disclosed in Proc. 12th World Hydrogen Energy Conference, wholesome Aires 697, 1998).
  • CB&H process disclosed in Proc. 12th World Hydrogen Energy Conference, wholesome Aires 697, 1998.
  • the advantages of the plasma-chemical processes used in this process are high thermal efficiency (> 90%) and the purity of hydrogen (98% by volume).
  • the high energy requirement is a disadvantage.
  • Steinberg et al. have in Int. J. Hydrogen Energy, 24, 771, 1999 proposed a methane decomposition reactor which consists of a molten metal bath. In this reactor, methane bubbles are passed through a molten tin or copper bath at high temperatures (900 ° C and more).
  • the advantages of this system consist in an efficient heat transfer to the methane gas flow and an easy separability of the carbon from the liquid metal surface due to the density difference.
  • a high temperature regenerative gas heater for hydrogen and carbon production was developed by Spilrain et al. in Int. J. Hydrogen Energy, 24, 613, 1999.
  • the thermal decomposition of natural gas was carried out in the presence of a carrier gas (N 2 or H 2 ) which was preheated in the matrix of a regenerative gas heater to a temperature of 1627 ° C to 1727 ° C.
  • a problem with these previously described processes is the very high temperature required for the methane cracking. There have therefore been numerous attempts to lower the temperature required for the thermal decomposition of methane by using catalysts. Transition metals in particular have proven to be very active as catalysts for the methane decomposition reaction. One problem, however, is catalyst deactivation due to carbon deposits on the catalyst surface.
  • the US 3,284,161 describes a process for the continuous production of hydrogen by catalytic decomposition of gaseous Hydrocarbon streams.
  • the methane decomposition was carried out in a catalytic fluidized bed reactor in the temperature range from 815 to 1093 ° C.
  • Nickel, iron and cobalt catalysts (preferably Ni / Al 2 0 3 ) were used in this process.
  • the carbon contaminated catalyst was continuously removed from the reactor and placed in a regeneration area where the carbon was burned off. The regenerated catalyst was then recycled to the reactor.
  • No. 5,650,132 describes a method for producing hydrogen from methane and other hydrocarbons by bringing it into contact with fine particles of a carbon-based material that is produced by arc discharge between carbon electrodes and that has an external surface area of at least 1 m 2 / g.
  • the carbon-based material additionally included soot obtained from the thermal decomposition of various organic compounds or the combustion of fuels, carbon nanotubes, activated carbon, fullerenes C60 or C70, and finely divided diamond.
  • the optimal conditions for methane conversion include: methane dilution with an inert gas (preferably to a methane concentration of 0.8 to 5% by volume), a temperature range of 400 to 1200 ° C and residence times of about 50 seconds.
  • US 2007/111051 describes a process for the C0 2 -free production of hydrogen and carbon by thermocatalytic decomposition of hydrocarbon fuels over carbon-based catalysts in the absence of air and water.
  • a catalyst in this case for example activated carbon "Darco ® -KB-B" is used, which has a surface area of 1,500 m 2 / g, a total pore volume of 1.8 ml / g and a particle size of 15 ⁇ m.
  • the actual decomposition of the hydrocarbon feedstock occurs in the context of this process at temperatures in the range of about 850 to 1000 ° C.
  • the actual reactor space is formed by a cylindrical porous ceramic matrix through which an inert gas, for example in the form of nitrogen (N 2 ) gas, is introduced into the reactor space.
  • an inert gas for example in the form of nitrogen (N 2 ) gas
  • a reactor is completely surrounded by a heating medium in order to provide the energy required for the process.
  • a structure is difficult to implement, particularly in the case of larger reactors, and requires significant amounts of energy.
  • one or more pairs of electrodes can be arranged in the reactor, via which the reaction gases are heated by resistance, for example by having a conductive material such as carbon particles between the electrodes.
  • the invention therefore relates to a process for the production of hydrogen and pyrolysis carbon from hydrocarbons, the hydrocarbons being converted to hydrogen and carbon in a reactor at temperatures of 1000 ° C or more, and the reactor having two electrodes spaced apart in the direction of flow of the hydrocarbons , characterized in that in the area of the reactor between the electrodes an inert gas component is supplied over the entire reactor cross-section and that the reactor contains carbon particles in the area between the electrodes.
  • an inert gas component such as nitrogen, is fed in over the entire reactor cross-section.
  • inert gas component denotes a gas or mixture of gases that is chemically inert with respect to the hydrocarbons in the reactor and does not react with them. This does not rule out that the inert gas component contains or consists of constituents that are inert with respect to the products generated in the reaction, in particular with respect to the carbon generated.
  • hydrogen is a gas that can form methane with carbon under suitable conditions, which can be used within the scope of the invention to break down carbon deposits on the walls of the reactor.
  • the statement that the inert gas component is fed into the reactor "over the entire reactor cross-section" is not to be understood to mean that an inert gas component is to be introduced in the entire area between the two electrodes.
  • the inert gas component is preferably introduced between the electrodes only in a partial area of the reactor wall. This can be done, for example, by one or more feed devices.
  • the inert gas component is preferably introduced into the reactor space via one or more feed devices which are arranged on the reactor wall orthogonally to the direction of flow of the hydrocarbons introduced into the reactor.
  • the carbon particles can be stationary in the area of the reactor between the two electrodes, but it is also possible that the carbon particles are in motion in this area. In the context of the present invention, it is preferred if the carbon particles are passed through the reactor against the direction of flow of the hydrocarbons, since in this way the formation of conductivity bridges (due to the adhesion of carbon formed in the reaction) and thus a non-uniform temperature profile in the reactor can be largely suppressed .
  • hydrocarbons to be included in the process according to the invention are not subject to any relevant restrictions as long as the release of hydrogen and the formation of carbon in the temperature range above 1000 ° C. are possible.
  • Suitable hydrocarbons are, for example, gaseous or liquid hydrocarbons such as methane, propane, gasoline, diesel, residual oil or crude oil at normal temperature and normal pressure.
  • Preferred hydrocarbons in the context of the present invention are gaseous hydrocarbons such as methane and propane, of which methane is particularly preferred.
  • the conversion of these hydrocarbons takes place according to the reaction equations. where n is greater than 1 and m is equal to or less than (2n + 2). Both reactions are endothermic.
  • the inert gas component is preferably an inert gas, such as nitrogen or argon, or a gas which is inert towards the hydrocarbons, such as the hydrogen gas generated in the reaction.
  • the “inert gas” should essentially, ie preferably 80% by volume, more preferably at least 90% by volume, and even more preferably at least 95% by volume, consist of an inert gas; If the process is carried out appropriately, small proportions of non-inert gases, such as methane, can be tolerated. In principle, however, in these cases the temperature of the inert gas introduced should be selected below the decomposition temperature of methane gas in order to prevent soot formation in the feed for the inert gas component. Both the inert gas component and the hydrocarbons should be free of oxidizing or oxidized constituents.
  • the carbon particles used can expediently be those which, in the range above 1000 ° C., promote pyrolytic decomposition of the hydrocarbons and are electrically conductive.
  • Particularly suitable carbon particles within the scope of the invention include the products commercially available as DARCO® KB-B (from Norit Americas Inc.), Black Pearls2000 (from CABOT Corp.) or XC-72 (from CABOT Corp.). In principle, however, any material made of carbon can be used, such as calcined petroleum coke, coking coal or the pyrolysis carbon generated in the process.
  • the process is operated in the starting phase with carbon particles that have been produced separately for this purpose.
  • part of the pyrolysis carbon generated in the course of the process can be used as carbon particles.
  • preference is given to predominantly using pyrolysis carbon and particularly preferably using pyrolysis carbon exclusively from the process after the start phase, ie after sufficient pyrolysis carbon has been generated in the reactor to operate the process with it.
  • the term “predominantly” here denotes a proportion of at least 60% by weight, preferably at least 70% by weight, more preferably at least 80% by weight, and even more preferably at least 90% by weight, based on the total amount of carbon particles.
  • the reaction zone in the reactor space is arranged vertically and the hydrocarbons pass through the reaction zone from bottom to top and the carbon particles pass through the reaction zone from top to bottom.
  • This procedure ensures, on the one hand, that a temperature transfer between the hydrocarbons fed to the reactor chamber and the carbon particles is made possible.
  • carbon generated from the hydrocarbons is largely deposited on the carbon particles and, in the case of non-static carbon particles, transported with the carbon particles downwards out of the reaction chamber, while the product gas generated in the reactor chamber is discharged from the top of the reactor. This ensures that the resulting product gas is essentially free of carbon formed in the reactor space.
  • the process according to the invention is particularly advantageous if the temperature in the reaction zone of the reactor is kept in the range from 1000 ° C to 1900 ° C, preferably in the range from 1200 ° C to 1500 ° C.
  • the inert gas component has a temperature which is lower than the temperature required for the decomposition of hydrocarbons to carbon and hydrogen.
  • Appropriate process management can ensure in the area where the inert gas component is fed into the reactor space that the reactor wall is colder in this area than in the rest of the reactor, so that soot formation is suppressed in the vicinity of the inlet of the inert gas component.
  • a cooler inert gas ensures that no carbon forms in the supply lines for the inert gas to the reactor, which could clog the lines.
  • the inert gas component fed in has a temperature of less than 1000.degree. C., preferably less than 900.degree. C.
  • hydrogen is an inert gas, for example in relation to the pyrolysis reaction of methane to hydrogen and carbon, and can be used as an inert gas component in the context of the present invention.
  • the process according to the invention is therefore designed such that part of the product gas generated in the process, preferably 5 to 30% by volume and in particular 10 to 25% by volume, is fed to the reactor as an inert gas component.
  • the hydrocarbons should expediently be fed into the reactor at a flow rate which ensures an extensive (i.e. at least 20%) to essentially complete (i.e. at least 70%) conversion of the hydrocarbons to hydrogen and carbon.
  • the process according to the invention is particularly advantageous if the inert gas component is fed into the reactor at a flow rate in the range from 0.001 m / s to 100 m / s, preferably 0.1 m / s to 10 m / s.
  • a particularly favorable process procedure is established when they are fed into the at a flow rate in the range from 0.5 m / h to 100 m / h and preferably 1 m / h to 10 m / h Reactor are fed.
  • Another aspect of the present invention relates to a device for the pyrolytic conversion of hydrocarbons to hydrogen and carbon, comprising a reactor 1 with a reactor chamber, which has two electrodes 2 which are spaced apart in relation to the flow direction of the hydrocarbons and via which the reactor is heated by resistance can, and has a supply device for an inert gas which is attached in the region between the electrodes of the reactor and which extends over the entire cross-section of the reactor.
  • This device is useful with supply lines for starting product (eg methane) and Koh len material particles as Catalytic converter and includes exhausts for carbon particles and product gas.
  • the feed device is preferably attached orthogonally to the intended direction of flow of hydrocarbons and carbon particles in the reactor.
  • the feed device comprises a distributor for inert gas components which is fluidly connected to the reactor space (i.e. e.g. via a continuous gap which intersects the reactor space, this forms an inlet opening).
  • the reactor cross-section in the device described above is expediently round, in particular circular or oval.
  • the device can furthermore advantageously be further developed in that the feed device is designed such that the reaction cross-section tapers above and / or below the inlet opening of the inert gas component into the reactor. It is particularly preferred that the reactor cross-section tapers above and below the gas inlet opening.
  • the tapering above the inlet opening 6 ensures exposed abrasion of the pyrolysis layer that is being formed and reduces the probability of carbon particles being located in the area of the inlet of the inert gas.
  • the cross-sectional taper below the inlet opening 7 reduces the dynamic pressure of the feed gas or hydrocarbon gas flow on the inlet opening.
  • the feed device is designed in such a way that the reactor cross-section in the area between the electrodes with the exception of the inlet opening of the inert gas component from the feed device is uniform, that is, with the exception of this inlet opening in the reactor cross-section in the area there is no tapering or widening between the electrodes.
  • the inlet opening of the feed device which is set back in comparison to the reactor wall, the gas velocity is slightly reduced in this area.
  • the inert gas introduced radially has a sufficiently low temperature, the radial temperature profile becomes low wall temperatures shifted, which in turn leads to reduced pyrolysis in this area.
  • the height Hl of a gap through which the inert gas component is fed into the reactor, or the pressure loss Dr between the gas pressure PI in the distributor of the feed line and the gas pressure P2 in the reactor is expedient to set an area which ensures a distribution of the gas component over the entire cross section (ie the pressure in the area PI is greater by Dr than the pressure in the reactor P2). Dr is dependent on the geometry and the conditions in the reactor.
  • the geometry of the distributor of the inert gas in the feed device is designed so that no carbon particles can enter the distributor geometry and a pyrolysis carbon bridge can form over this due to a longer residence time.
  • the inert gas is introduced into the reactor at an angle of 30 ° to 60 °, preferably about 45 °, counter to the direction of flow of the hydrocarbons.
  • the product gas formed during the process consists, under favorable conditions, to a substantial extent of hydrogen with only small amounts of methane.
  • the product gas is therefore suitable for partial recycling of the product gas stream as an inert gas in the reactor space.
  • the device according to the invention has a discharge line for product gas 13 formed in the reactor, and that the discharge line has a branch line 14 via which part of the product gas is fed back into the reactor via the feed device for inert gas. Since, as indicated above, the pressure for feeding the inert gas into the reactor space in the area of the feed line must be higher than in the reactor space itself, it is useful if the device in the area of the branch line 14 has a compressor 15 with which the inert Gas is compressed to a higher pressure.
  • product gas H 2
  • inert gas has the additional advantage that the product gas stream in the area of the feed line has a temperature which is significantly below the pyrolysis temperature of methane.
  • the pressures present in the reactor space (usually in the range from 10 to 15 bar) are therefore in equilibrium for the CH reaction H 2 + C stuck on the side of methane.
  • the equilibrium is also on the methane side, so that the H 2 -containing gas flow introduced radially leads to methanation of the carbon present or to chemical carbon removal.
  • the methane formed pyrolyses again to hydrogen and carbon, so that continuous cleaning of the feed areas for the inert gas is possible within the scope of the process by this process management.
  • Figure 1 shows a reactor 1 designed according to the invention with two spaced electrodes 2 and a carbon bed 3 extending beyond both electrodes the reactor is conducted.
  • the reactor cross-section is tapered 6.7 below and above the distributor structure 5.
  • an increased gas velocity is realized in these tapered areas, which reduces the probability of the presence of carbon particles in this area.
  • the tapering also acts as a deflection for gas flowing through.
  • a pyrolysis carbon layer 8 forms on the inner wall of the reactor in the course of the process.
  • FIG. 2 shows different variants of the feed line for inert gas into the reactor space, variants A and B being designed with tapering of the reactor cross-section in the area above and below the feed line for the inert gas, while in variant C a feed line is designed in such a way that that the reactor cross-section in the area between the electrodes with the exception of the outlet for inert gas from the feed device is uniform.
  • FIG. 3 shows a gas distributor construction according to the invention, where H 1 is the gap height through which the gas from the distributor space into the reactor space flows in, indicates.
  • PI denotes the manifold pressure
  • P2 the reactor pressure
  • Dr the pressure loss between manifold pressure and reactor pressure.
  • FIG. 4 shows a diagram of a device according to the invention with a reactor 1, a feed line for hydrocarbon starting material 10, a feed line for carbon particles 11, a discharge line for carbon particles 12 and a discharge line for product gas 13.
  • a junction 14 is provided via which part of the product gas can be passed into a compressor 15 and from there again into the reactor.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Carbon And Carbon Compounds (AREA)

Abstract

L'invention concerne un procédé de production d'hydrogène et de carbone pyrolytique à partir d'hydrocarbures, les hydrocarbures étant mis à réagir dans un réacteur à des températures de 1000 °C ou plus pour former de l'hydrogène et du carbone, et le réacteur a deux électrodes espacées l'une de l'autre dans la direction d'écoulement des hydrocarbures, un composant de gaz inerte étant amené sur toute la section transversale du réacteur dans la zone du réacteur entre les électrodes, et le réacteur contenant des particules de carbone dans la région entre les deux électrodes. L'introduction d'un composant de gaz inerte sur toute la section transversale du réacteur empêche un dépôt de carbone dans cette région de la paroi interne du réacteur, de telle sorte que la formation de ponts de réactivité sur la paroi interne du réacteur est efficacement supprimée. L'invention concerne également un dispositif correspondant qui est conçu pour mettre en œuvre le procédé proposé.
EP20807329.6A 2019-11-13 2020-11-12 Procédé et dispositif de production d'hydrogène et de carbone pyrolytique à partir d'hydrocarbures Pending EP4058403A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102019130600.0A DE102019130600A1 (de) 2019-11-13 2019-11-13 Verfahren und Vorrichtung zur Herstellung von Wasserstoff und Pyrolysekohlenstoff aus Kohlenwasserstoffen
PCT/EP2020/081928 WO2021094464A1 (fr) 2019-11-13 2020-11-12 Procédé et dispositif de production d'hydrogène et de carbone pyrolytique à partir d'hydrocarbures

Publications (1)

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EP4058403A1 true EP4058403A1 (fr) 2022-09-21

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Country Status (5)

Country Link
US (1) US20230025624A1 (fr)
EP (1) EP4058403A1 (fr)
CN (1) CN114630807B (fr)
DE (1) DE102019130600A1 (fr)
WO (1) WO2021094464A1 (fr)

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CN116253307A (zh) * 2023-02-07 2023-06-13 中国航天空气动力技术研究院 一种高纯纳米炭黑制备方法
WO2024192463A1 (fr) * 2023-03-17 2024-09-26 Future Fuels CRC Ltd Procédé de production d'hydrogène

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US7588746B1 (en) * 2006-05-10 2009-09-15 University Of Central Florida Research Foundation, Inc. Process and apparatus for hydrogen and carbon production via carbon aerosol-catalyzed dissociation of hydrocarbons
JP5407003B1 (ja) * 2013-06-25 2014-02-05 Ｓａｉｓｅｉ合同会社 メタンガス分解装置
DE102015218098A1 (de) * 2015-09-21 2017-03-23 Deutsche Lufthansa Ag Verfahren zur thermischen Spaltung von Kohlenwasserstoffen und korrespondierende Vorrichtung
DE102015219861A1 (de) * 2015-10-13 2017-04-13 Deutsche Lufthansa Ag Vorrichtung und Verfahren zur Erzeugung von Synthesegas

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CN114630807A (zh) 2022-06-14
WO2021094464A1 (fr) 2021-05-20
CN114630807B (zh) 2024-08-30
DE102019130600A1 (de) 2021-05-20

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