EP4695014A1 - Réacteur pour la génération d'hydrogène - Google Patents

Réacteur pour la génération d'hydrogène

Info

Publication number
EP4695014A1
EP4695014A1 EP24732641.6A EP24732641A EP4695014A1 EP 4695014 A1 EP4695014 A1 EP 4695014A1 EP 24732641 A EP24732641 A EP 24732641A EP 4695014 A1 EP4695014 A1 EP 4695014A1
Authority
EP
European Patent Office
Prior art keywords
tube
reactor
catalyst
inner tube
reactor vessel
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
EP24732641.6A
Other languages
German (de)
English (en)
Inventor
Claus Krusch
Bastian Preusser
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.)
Siemens Energy Global GmbH and Co KG
Original Assignee
Siemens Energy Global GmbH and Co KG
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 Siemens Energy Global GmbH and Co KG filed Critical Siemens Energy Global GmbH and Co KG
Publication of EP4695014A1 publication Critical patent/EP4695014A1/fr
Pending legal-status Critical Current

Links

Classifications

    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
    • B01J8/025—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical in a cylindrical shaped bed
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/02—Apparatus characterised by being constructed of material selected for its chemically-resistant properties
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0207—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly horizontal
    • B01J8/0221—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly horizontal in a cylindrical shaped bed
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
    • B01J8/0257—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical in a cylindrical annular shaped bed
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0285—Heating or cooling the reactor
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • B01J8/067—Heating or cooling the reactor
    • 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; Reversible storage of hydrogen
    • C01B3/02—Production of hydrogen; Production of gaseous mixtures containing hydrogen
    • C01B3/04—Production of hydrogen; Production of gaseous mixtures containing hydrogen by decomposition of inorganic compounds
    • C01B3/047—Decomposition of ammonia
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00884—Means for supporting the bed of particles, e.g. grids, bars, perforated plates
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis

Definitions

  • the invention relates to a reactor for producing hydrogen and at least one further product from at least one reactant.
  • reactors In many areas of chemical process engineering, reactors, catalysts, heat exchangers and evaporators are used to split or synthesize substances.
  • the basic principle of such systems is based on the spatial separation of two material flows and the transfer of thermal energy through the reactor structure. High temperatures, possibly increased pressures and the presence of a catalyst are often required to activate these processes.
  • Two examples of such chemical processes are steam reforming and ammonia splitting (dehydration) to produce hydrogen (H 2 ) from hydrocarbons such as methane (CH 4 ) and ammonia (NH 3 ).
  • ammonia cracking ammonia is evaporated, heated and split into hydrogen and nitrogen in a reactor (cracker) at a temperature of up to 950 °C and a pressure of more than 1 bar using a nickel catalyst.
  • heat energy must be supplied by electrical heating or a burner.
  • a particular challenge here is the corrosive attack by the starting media (hydrocarbons, water vapor, ammonia) and by the reaction products (hydrogen, carbon, nitrogen) on the corrosion resistance of the reactor materials used.
  • the lack of corrosion resistance of metal-based systems (stainless steels and nickel-based alloys) under ammonia, hydrogen and nitrogen atmospheres represents the main limitation to achieving high conversion rates. If the heat input is not achieved by electrical heating, heating with a burner results in the additional requirement of resistance to oxidising atmospheres.
  • the main requirement is to achieve an adapted heat transfer performance with the highest possible efficiency and the lowest possible flow resistance or pressure loss.
  • a high efficiency is promoted by a high thermal conductivity of the reactor material and a large internal heat exchanger surface (heat transfer) with the smallest possible external surface (heat loss through radiation and convection) as well as the requirement for the lowest possible heat loss through the outflowing reaction products.
  • Plants for ammonia splitting currently only exist in the capacity range ⁇ 100 kg H2 /h and are constructed similarly to steam reformers.
  • Metal-based plant concepts for steam reforming are usually operated with beds of mostly extruded ceramic profiles (pellets) that are coated or vapor-deposited with the catalyst material.
  • the invention is based on the object of improving the corrosion resistance of a reactor for producing hydrogen and thus ensuring an increased service life.
  • a reactor for producing hydrogen and at least one further product from at least one reactant comprising a tubular reactor vessel in which a catalyst is contained in the form of a bed, wherein the reactor vessel is made of silicon-infiltrated silicon carbide (SiSiC).
  • SiSiC silicon-infiltrated silicon carbide
  • the ceramic tube vessel achieves a high level of corrosion resistance against the medium to be converted, ammonia, and against the reaction products, in particular against hydrogen and nitrogen, in the temperature range of 300 - 950 °C and pressures of 1 to 40 bar.
  • the ceramic material from which the reactor vessel is made is silicon-infiltrated silicon carbide (SiSiC).
  • SiSiC silicon-infiltrated silicon carbide
  • This material is characterized by a number of advantages in terms of mechanical, thermal and chemical properties. It meets the strength requirements in the temperature range from room temperature to 1100 °C due to the high stationary and unsteady thermal gradients. In addition, it has a high oxidation and corrosion resistance, a high thermal conductivity and a high thermal shock resistance. A further advantage is the rapid heating behavior due to the thermal-mechanical material properties of SiSiC and thus a short switch-on delay (this enables use in cyclically operated systems). The low weight when used The use of SiSiC also enables its use for non-stationary applications.
  • the catalyst bed is also made of a ceramic material, in particular silicon-infiltrated silicon carbide (SiSiC), and coated with a catalytic material.
  • the catalytic coating is nickel, for example.
  • the material of the coating is different, depending on the requirements.
  • the particle size and shape of the catalyst depends on the respective flow channel.
  • the most important geometric factor in relation to the activity of the catalytically coated bed is the ratio of the geometric surface of the particles to their volume.
  • the smallest possible particle size should be aimed for. However, this is counteracted by the requirement of the lowest possible pressure loss or flow resistance, which preferably requires a large particle size.
  • Cylindrical structures with one or more longitudinal bores and grooves on the outer surfaces to increase the surface area are advantageously used as catalyst particles.
  • Simple geometric structures such as spheres and solid cylinders are also suitable for smaller flow cross-sections.
  • the particle size depends on the respective flow channel. Examples of suitable particles are, depending on the size of the flow channel, particles with a diameter of 1 to 20 mm with a length of A diameter-to-particle ratio of 0.5 to 1.5 is provided.
  • the ratio of reactor diameter to particle diameter is usually 3 to 10.
  • the tubular reactor vessel is constructed from a cylindrical tube
  • the tube has a feed opening for the at least one reactant at one end and a discharge opening for the at least one product at the other end, and
  • the catalyst is located in a central region of the tube and is held in position by means of a fixing element through which flow can pass.
  • a fixing element through which flow can pass.
  • a cylindrical tube is understood here to be an essentially straight tube without significant bends.
  • the fixing element is porous so that the reactant stream and/or the product stream can flow through it.
  • the fixing element is preferably also made of SiSiC (silicon-infiltrated silicon carbide) or another ceramic material since it is located in the region of the highest process temperatures.
  • the pores of the fixing element are smaller than the diameter of the particles of the catalyst bed. If the tube is aligned vertically, only a single fixing element is required, which supports the catalyst bed from below. For example, If the pipe is arranged horizontally, two fixing elements on either side of the catalyst bed may be required.
  • the fixing element is advantageously attached to the cylindrical tube via a positive and/or force-fitting connection.
  • a connection is suitable for use at high temperatures, such as those that occur during operation of the reactor.
  • a material-fitting connection is also suitable.
  • a positive connection is particularly advantageous from a design point of view. In its simplest version, this can be made with a preferably ceramic Support rod that holds the fixing element in position.
  • the fixing element can be held by a pin mounted in the tube, a shoulder or a conical inner tube geometry.
  • the tubular reactor vessel is formed from a U-shaped tube with an apex, the tube is directed upwards with both ends and has a feed opening for the reactant at a first end and a discharge opening for the products at a second end, and the catalyst is located in the region of the apex of the tube.
  • the fixing element is omitted since the catalyst bed is held in the lower region, in the region of the apex of the tube, by the shape of the curved tube and the gravitational forces.
  • the tubular reactor vessel is formed from a W-shaped or multiple W-shaped tube, the tube having two or more lower vertices, the tube being directed upwards with both its ends and having a feed opening for the reactant at a first end and a discharge opening for the products at a second end, and the catalyst being located in the region of the lower vertices of the tube. At least two catalyst beds are provided. In this embodiment, no fixing element is required for the catalyst beds.
  • the W-shaped design of the ceramic tube offers the advantage of a longer path for the reactants in the reactor and a longer residence time.
  • the tubular reactor vessel comprises a cylindrical inner tube and a cylindrical outer tube, the inner tube and the outer tube extend vertically, the inner tube is arranged in the outer tube, in particular concentrically, and the diameter of the inner tube is smaller than the diameter of the outer tube, so that a flow channel is formed around the inner tube, the lower end of the inner tube is higher than the lower end of the outer tube, so that an intermediate space is formed in the region of the lower end of the outer tube, the outer tube has a feed opening for the reactant at its upper end and its lower end is closed, the inner tube has a discharge opening for the product at its upper end and its lower end is open, and the intermediate space is filled with the catalyst, wherein the lower end of the inner tube extends into the catalyst.
  • the main advantage of this design is that heat is exchanged between the inner tube and the outer tube.
  • the products in the inner tube which are at a high temperature, give off their heat to the reactants flowing in the opposite direction in the flow channel of the outer tube. These are heated in this way, so that the amount of heat that has to be supplied from the outside is lower.
  • a high level of efficiency is achieved by integrating the heat exchanger and reactor and by reducing heat losses due to the small external surface.
  • the tubular reactor vessel is preferably arranged in a heating device.
  • the tubular reactor vessel can be completely surrounded by the heating device, or it can be sufficient if only the area of the tube in which the catalyst is located and the chemical reaction takes place is surrounded by the heating device.
  • the heating device can be an electric heating device, contain a burner, or be based on another heating principle.
  • FIG 1 shows a first embodiment of a catalytic reactor
  • FIG 2 shows a second embodiment of a catalytic reactor
  • FIG 3 shows a third embodiment of a catalytic reactor.
  • FIG 1 shows a first catalytic reactor 2, i.e. a reactor for the catalytic conversion of at least one reactant, in this case ammonia NH 3 , into hydrogen H 2 and nitrogen N 2 .
  • the reactor 2 comprises a tubular reactor vessel 4 in which a catalyst 6 is contained in the form of a bed.
  • the reactor vessel 4 is made of a ceramic material, in this case silicon-infiltrated silicon carbide (SiSiC).
  • the bed 6 of catalytically coated particles is preferably also made of ceramic material due to its higher corrosion resistance.
  • Commercially available catalyst supports (beds) are based, for example, on aluminum oxide (Al 2 O 2 ) or steatite (magnesium silicate). In the exemplary embodiment shown, however, the catalyst 6 is also made of silicon-infiltrated silicon carbide (SiSiC).
  • the catalyst particles are also coated with a catalytic coating made of nickel.
  • the tubular reactor vessel 4 is formed from a straight, cylindrical tube 3.
  • the tube comprises connection flanges 8 at one or both ends.
  • the tube 3 is vertically aligned and has a supply opening 10 for the ammonia stream NH 3 at the upper end and a discharge opening 12 at the lower end for discharging the product gases hydrogen H 2 and nitrogen N 2 .
  • the catalyst 6 is located in a central region of the tube 4 and is held in position by means of a flow-through fixing element 14.
  • the fixing element 14 is in particular porous or designed as a honeycomb body and allows the product gases to flow through it.
  • the process gas flows through the tube in the longitudinal direction and is heated in the inlet area, close to the feed opening 10, by a heat flow Q supplied from the outside to the temperature level required for the subsequent cracking reaction of 700 to 950 °C (for high gas mass flows and high required conversion rates/purities also up to 1000 °C).
  • the required temperature level depends on the required degree of purity of the process gases after cracking and on the gas mass flow. Partial cracking takes place at a temperature of as little as 600 °C.
  • the technical advantage of the SiSiC tube reactor compared to a metallic solution is, however, in particular the corrosion resistance under the described atmospheres and at high temperatures.
  • the conversion rate i.e. the degree of conversion of ammonia NH 3 into hydrogen H 2 and nitrogen N 2 , depends on the gas temperature, the catalyst parameters and the gas mass flow.
  • the reactor according to FIG 2 differs from the first version in the shape of the reactor vessel 4 .
  • the ceramic tube 16 is based on a U-shaped tube geometry of the SiSiC tube .
  • This design variant enables the feed of the reactant gas and the discharge of the product gas from the same side .
  • the flow-through fixing element 14 according to FIG 1 is omitted, since the catalytically coated bed is located at the bottom apex of the U-tube 16 .
  • a heating device is provided.
  • device 18 is shown, in which the reactor vessel 4 is integrated, through which the heat for starting and maintaining the reaction is supplied, which is indicated by Q.
  • the reactor 2 consists of an outer tube 18 with a closed bottom and an inner tube 20 which is guided concentrically in the outer tube 18.
  • the inner tube 20 does not reach to the bottom of the outer tube 18, so that in the bottom region between the inner tube 20 and the outer tube 18 a gap is created which defines an intermediate space 22.
  • the bottom region of the outer tube 18 is filled with the ceramic, catalytically coated bed 6.
  • the inner tube 20 projects into this catalytic bed 6.
  • the reactant gas flowing into a flow channel 24 in the region of the annular gap between the outer tube 18 and the inner tube 20 flows in the direction of the outer tube bottom and flows through the catalytically coated bed 6, within which the splitting into hydrogen H 2 and nitrogen N 2 takes place.
  • the resulting product gas flows through the free space 22 into the inner tube and against the flow direction of the inflowing ammonia NH 3 in the direction of the discharge opening of the inner tube 20 and with heat release to the inflowing ammonia NH 3 via the wall of the inner tube 20.
  • the heat flows supplied from the outside of the reactor vessel 4, which are generated by a heating device (18 in FIG. 2), are designated by Q (FIG. 1 and FIG. 3 without representation of the heating device).
  • These heat flows are generated, for example, in a furnace chamber, either by heating with electrical resistance heating elements or by gas flames.
  • the furnace is a conventional high-temperature furnace, such as is used, for example, for ceramic firing or heat treatment, and in which the ceramic reactor tube, including the supply and discharge openings, is integrated through the furnace wall or walls.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

L'invention concerne un réacteur (2) pour générer de l'hydrogène et au moins un autre produit à partir d'au moins un réactif, le réacteur comprenant une cuve de réacteur tubulaire (4) qui contient un catalyseur (6) sous la forme d'un lit céramique. Une résistance à la corrosion améliorée contre divers milieux et ainsi une durée de vie accrue du réacteur (2) est obtenue par formation de la cuve de réacteur (4) à partir de carbure de silicium infiltré de silicium (SiSiC).
EP24732641.6A 2023-06-26 2024-06-12 Réacteur pour la génération d'hydrogène Pending EP4695014A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102023206000.0A DE102023206000A1 (de) 2023-06-26 2023-06-26 Reaktor zur Erzeugung von Wasserstoff
PCT/EP2024/066137 WO2025002798A1 (fr) 2023-06-26 2024-06-12 Réacteur pour la génération d'hydrogène

Publications (1)

Publication Number Publication Date
EP4695014A1 true EP4695014A1 (fr) 2026-02-18

Family

ID=91530088

Family Applications (1)

Application Number Title Priority Date Filing Date
EP24732641.6A Pending EP4695014A1 (fr) 2023-06-26 2024-06-12 Réacteur pour la génération d'hydrogène

Country Status (4)

Country Link
EP (1) EP4695014A1 (fr)
KR (1) KR20260019656A (fr)
DE (1) DE102023206000A1 (fr)
WO (1) WO2025002798A1 (fr)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102024201516A1 (de) * 2024-02-20 2025-08-21 Siemens Energy Global GmbH & Co. KG Reaktor für die chemische Prozesstechnik
CN119971916B (zh) * 2025-02-13 2025-11-18 华东理工大学 用于氨分解制氢的SiSiC泡沫陶瓷电驱动反应器及其制备方法

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB8613671D0 (en) 1986-06-05 1986-07-09 Bp Benzin Und Petroleum Ag Chemical process
DE10155628A1 (de) 2001-11-13 2003-05-22 Linde Ag Verfahren und Vorrichtung zur Durchführung endothermer Reaktionen
JP5015766B2 (ja) * 2005-02-04 2012-08-29 日本碍子株式会社 選択透過膜型反応器
DE102006010289B4 (de) 2006-03-02 2010-07-01 Deutsches Zentrum für Luft- und Raumfahrt e.V. Spaltung von Schwefelsäure
DE102010000980A1 (de) 2010-01-18 2011-07-21 Evonik Degussa GmbH, 45128 Katalytische Systeme zur kontinuierlichen Umsetzung von Siliciumtetrachlorid zu Trichlorsilan
EP3075707A1 (fr) * 2015-04-02 2016-10-05 Evonik Degussa GmbH Procédé d'hydrogénation de tétrachlorure de silicium en trichlorosilane à l'aide d'un mélange gazeux d'hydrogène et de chlorure d'hydrogène
TWI617536B (zh) * 2015-06-12 2018-03-11 薩比克環球科技公司 藉由甲烷之非氧化偶合製造烴類之方法
CN111632557B (zh) * 2020-06-23 2024-06-14 浙江大学 一种用于热化学硫碘循环制氢的新型硫酸分解装置和方法
CN112827432B (zh) * 2021-01-06 2021-12-10 清华大学 一种不均匀分布催化剂床加回流多管和螺纹外壁面的硫酸分解管

Also Published As

Publication number Publication date
KR20260019656A (ko) 2026-02-10
WO2025002798A1 (fr) 2025-01-02
DE102023206000A1 (de) 2025-01-02

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