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WO2025119981A1 - Système de réacteur en cascade et procédé de mise en œuvre d'une réaction endothermique - Google Patents

Système de réacteur en cascade et procédé de mise en œuvre d'une réaction endothermique Download PDF

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Publication number
WO2025119981A1
WO2025119981A1 PCT/EP2024/084686 EP2024084686W WO2025119981A1 WO 2025119981 A1 WO2025119981 A1 WO 2025119981A1 EP 2024084686 W EP2024084686 W EP 2024084686W WO 2025119981 A1 WO2025119981 A1 WO 2025119981A1
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stream
reactor
inlet
reactive
reactor system
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Martin BAUMGAERTL
Simone GUFFANTI
Gianluca Pauletto
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Sypox GmbH
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Sypox GmbH
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    • 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
    • B01J8/04—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 passing successively through two or more beds
    • B01J8/0496—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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • B01J19/0013—Controlling the temperature of the process
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    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/248—Reactors comprising multiple separated flow channels
    • B01J19/2485—Monolithic reactors
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    • 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
    • B01J8/0278—Feeding reactive fluids
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    • 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
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • 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
    • B01J8/04—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 passing successively through two or more beds
    • B01J8/0492—Feeding reactive fluids
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01J8/082—Controlling processes
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    • 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
    • C01B3/04—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of inorganic compounds, e.g. ammonia
    • C01B3/047—Decomposition of ammonia
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    • 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
    • C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
    • C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
    • C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
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    • 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
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/382—Multi-step processes
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    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
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    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00389—Controlling the temperature using electric heating or cooling elements
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    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00389—Controlling the temperature using electric heating or cooling elements
    • B01J2208/00415—Controlling the temperature using electric heating or cooling elements electric resistance heaters
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J2219/00049—Controlling or regulating processes
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    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
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    • B01J2219/00132—Controlling the temperature using electric heating or cooling elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00132—Controlling the temperature using electric heating or cooling elements
    • B01J2219/00135—Electric resistance heaters
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00162—Controlling or regulating processes controlling the pressure
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/2402—Monolithic-type reactors
    • B01J2219/2409—Heat exchange aspects
    • B01J2219/2416—Additional heat exchange means, e.g. electric resistance heater, coils
    • C—CHEMISTRY; METALLURGY
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    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
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    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0238—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a carbon dioxide reforming step
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    • 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
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • C01B2203/0261—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a catalytic partial oxidation step [CPO]
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    • 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
    • C01B2203/14—Details of the flowsheet
    • C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series

Definitions

  • the invention relates to an electrically heated cascaded reactor system for completing an endothermic reaction from a fed reactive mixture stream and a method thereof.
  • Typical high temperature endothermic processes employ heat generated via the combustion of a fuel.
  • steam methane reforming involves a hydrocarbon-steam mixture which flows through reactor tubes containing Ni-based catalyst pellets.
  • the necessary heat for the high-temperature reaction is generated in the surroundings of the reactor tubes using burners.
  • the generated heat is then transfer, mostly by radiation, across the wall of the reactor tubes.
  • Such configuration is commonly known in industry as fired furnace or fired box.
  • This technology is state of the art in processes like steam methane reforming, steam cracking, reverse water gas shift, and ammonia cracking. Limitations of this approach lie in the low efficiency of the firebox itself, the production of emissions via flue gases from the burners and the limited maximum operating temperature, which is determined by the mechanical stability of the tube material.
  • Electrically heated reactors present solutions to the described limitations of conventional fired furnaces. Additionally, the source of heating can be completely decarbonized when fossil fuel is replaced by renewable electricity.
  • EP3895795 introduces a reactor with an electrically heated structured ceramic catalyst having hollow flow paths within where the reactive mixture stream is flowing.
  • the resistive heating elements incorporated within these paths generate the heat necessary to power endothermic reactions.
  • a preferred design features coaxial wire heaters, possibly meandering through multiple paths.
  • a metallic macrostructure is coated with catalytically active material and heated by directing electricity through this metallic macrostructure. The generated heat is directly consumed by the catalyst to complete an endothermic reaction.
  • temperatures of the heating means can rise up to 1200°C, which will cause thermal expansion on the heating means, independent of being a wire, a metallic monolith or metal foam.
  • This combined with the reduced mechanical properties of the conductive material at high temperatures, increase the risk of mechanical deformation, failure and potential electrical shorts due to unwanted contacting of the heating means. This problem increases in severity with the length of the electrically heated bed.
  • Shorter electrically heated beds reduce expansion problems, which is often problematic for washcoated electrically heated beds, but at the same time require larger cross-sections to maintain an adequate catalyst volume for large scale reactor systems.
  • Larger cross-sections provide challenges in distributing the flow evenly across the whole catalytic bed, which is crucial to avoid hotspot formation and uneven conversion of the reactive mixture stream across the bed.
  • the heat consumption is strongly dependent on the molecules converted.
  • the electrical heating means provides an even heat generation throughout the entire bed. Small deviations in flow distribution can therefore have a huge influence on the temperature profile and uniformity within the catalyst bed.
  • the present invention relates to an electrically heated cascaded reactor system and a method to eliminate the above-mentioned disadvantages and bring new advantages to the relevant technical field.
  • Another object of the invention is to provide a cascaded reactor system that reduces the mechanical deformation and prevents the shortcutting of electric heating means.
  • Another object of the invention is to provide a cascaded reactor system that reduces uneven distribution of reactive mixture stream passing through the electrically heated catalytic bed, thus avoiding hotspot formation within said electrically heated catalytic bed.
  • the present invention relates to a reactor system for the production of carbon dioxide, synthesis gas, and hydrogen from a stream comprising a mixture of a nebulized liquid and/or gas hydrocarbon and/or methane-containing, and/or of a water steam, and/or of an oxidant stream and/or carbon dioxide and/or hydrogen and/or ammonia and/or volatile organic compounds (VOC) comprising at least two electrically heated reactors connected in series so that the outlet stream of the prior electrically heated reactor directly enters to the inlet section of the following electrically heated reactor.
  • VOC volatile organic compounds
  • the invention is a cascaded reactor system to carry out an endothermic reaction of a reactive mixture stream to be converted to a product gas or product stream characterized in that comprising
  • each reactor shell comprises at least one reactive stream duct, the stream inlet for receiving the fed reactive mixture stream, the stream outlet, a catalyst section provided inside said reactive stream duct between said stream inlet and stream outlet; an insulation filling at least partly encompassing said reactive stream duct, a catalyst bed accommodated in said catalyst section, where the reactive mixture stream undergoes a catalytic reaction, electrical heating means for heating said ceramic catalyst bed up to a predetermined reaction temperature; at least two electrical feeds passing through the inlet section connected to an electrical power supply provided outside of the reactive stream duct, and
  • the stream inlet of at least one reactor shell contains a separating device for creating a cold section within the inlet zone of said reactor shell wherein the electric feeds that bring electricity into the reactor shell are at least partly located within said cold section for preventing said electric feeds from exposition to high temperatures.
  • Another object of the present invention refers to a method for carrying out an endothermic reaction using a cascaded reactor system such as in claims 1-9 characterized in that comprising the steps of:
  • Figure 1 is a drawing illustrating sectional view of the system.
  • a stream comprising a mixture of a nebulized liquid and/or gas hydrocarbon and/or methane-containing, and/or of a water steam, and/or of an oxidant stream and/or carbon dioxide and/or hydrogen and/or ammonia and/or volatile organic compounds (VOC).
  • VOC volatile organic compounds
  • the present invention refers to a cascade reactor system comprising multiple reactor shells connected in series, each hosting an electrically heated structured ceramic catalyst and a compliant method for using this configuration for steam methane reforming process and/or dry reforming process and/or partial oxidation process and/or reverse water gas shift process and/or ammonia cracking and/or dehydrogenation reactions.
  • the outlet section of a previous electrically heated reactor and the inlet section of the subsequent electrically heated reactor in series are connected together by flanges or welding.
  • the advantage of this configuration is that next to the inlet gas section, a ‘cold section’ with temperatures below 500°C can be realized, in which it is possible to allocate the connections between the power supply and the electric heating means (see FIG. 1). Without this cold section, the electrical conductors and electrical connections could face temperatures of up to 1200 °C. These temperatures not only demand materials with high temperature stability, but also cause problems regarding corrosion, metal dusting and hydrogen embrittlement and in general reduce the lifetime of such connections dramatically compared to connections allocated within a cold section. Therefore, the implementation of a cold section at the inlet of at least one pressure vessel is the distinct feature that enables an in series assembly of electrically heated pressure vessels.
  • an in series configuration of electrically heated reactors offers many advantages compared to a single pressure vessel containing a single electrically heated bed at same production capacity.
  • the length of the electrically heated structured ceramic catalyst bed is designed to avoid excessive thermal expansion of the electric heating means, which may lead to electrical short cut of the electrical heating means itself or even with downstream equipment.
  • the length of the electrically heated structure catalyst bed is preferably between 100 mm and 2000 mm, more preferably between 200 mm and 1000 mm. Increasing the production capacity within a single electrically heated bed therefore typically involves an increase in cross section, and not in length of the electrically heated catalytic bed.
  • the cascaded reactor system (10) comprises a plurality of reactor shells (20).
  • Each reactor shell (20) comprises at least a stream inlet (25) and at least a stream outlet (26).
  • Each reactor shell (20) comprises a reactive stream duct (22) provided between said stream inlet (25) and said stream outlet (26). Said stream duct is encompassed by an insulation filling (60).
  • Each reactor shell (20) comprises a catalyst section (21) provided inside said reactive stream duct (22).
  • the catalyst section (21) comprises a structured ceramic catalyst bed (30) comprising a plurality of hollow flow paths (31) which are configured to allow the reactive mixture stream to pass through and coming in physical contact with the inner walls of the hollow flow paths (31) of the structured ceramic catalyst bed (30).
  • the catalyst section (21) comprises electrical heating means (40) for heating said structured ceramic catalyst bed (30) up to a predetermined reaction temperature.
  • At least two electrical feeds (51) passing through the inlet section connected to an electrical power supply (50) provided outside of the reactive stream duct (22).
  • a separating device is installed within the inlet section, creating a cold section (281), which is hosting the electrical connections between electric feeds and heating means. Providing electrical feeds (51) in the cold section significantly reduces heat exposure of electrical feeds (51).
  • the cascaded reactor system (10) it is possible to connect the electrical heating means (41) to the electrical feeds (51) in the cold section (281) of the reactor shells (20) which is the coldest part of the reacting stream duct (22). This, reduces he risk of failure, the need of maintenance and increases the lifetime of the connections between the electrical heating means (41) and the electrical feeds (51).
  • Reactor shells (20) are serially connected where the stream outlet (26) of a reactor shell (20) is connected to the stream inlet (25) of the next reactor shell (20). This provides, a continuous duct allowing reactive mixture stream to pass through starting from the stream inlet (25) of a first reactor shell (20) in series to the stream outlet (26) of the last reactor shell (20) in series. This allows to modularly increase the number of reactor shells (20) in order to increase production capacity, while maintaining a short length of the structured ceramic catalyst bed (30).
  • reactor shells (20) may be provided by flanges or welding. Thus a flanged or welded connection (27) is provided between subsequent reactor shells (20).
  • Modularly increasing the number of reactor shells (20) allows to partially compensate for a possible malfunctioning of one individual reactor shell (20) in series by separately controlling the power supplied to each unit.
  • Stream outlet (26) and stream inlet (25) of each reactor shell (20), is arranged in such way that reactor shells (20) can be serially connected.
  • the stream inlet (25) of a reactor shell (20) extends outward from a side surface of the reactive stream duct (22).
  • the stream outlet of a reactor shell (20) extends outward from another side surface that is at the opposite side of the stream inlet (25).
  • the stream inlet (25) extends along a first imaginary line and the stream outlet (26) extend along a second imaginary line that is parallel to the first imaginary line.
  • the modular setup of the cascaded reactor system (10) can be realized by means of connecting the stream outlet (26) of the preceding reactor shell (20) with the stream inlet (25) of the following reactor shell (20), forming a reactive stream duct (22) in a continuous pipeline whose length can be determined flexibly in accordance with the desired endothermic reaction yield, therefore leading to a scaled-up reactor system that is easier to assemble and perform maintenance thereon.
  • This preferred configuration allows scaling up of a system for carrying on an endothermic reaction in a compact way, such that the plurality of reactor shells (20) can be connected to each other serially in a vertical manner, allowing increased endothermic reaction yield per floor area that is occupied by a reactor system, much lower land footprint.
  • Each reactor shell (20) comprises an inlet chamber (28) between the stream inlet (25) and the catalyst section (21). Said inlet chamber is divided by a dividing device into a cold section and an inlet section. Electrical feeds (51) are entering the pressure vessel within the cold section of said inlet chamber (28).
  • said cold section (281) is accessible from a sealed flange (29) within the pressure vessel (reactor shell (20)). This allows easier access to the electrical connections through the removable sealing flange (29) in case of the need for maintenance or inspection, as well as allowing to perform such a task at each individual reactor shell (20) separately.
  • Stream inlets (25) and stream outlets (26) have matching structure that allows connecting to each other.
  • any individual reactor shell (20) among the serially connected plurality of such may have same or different specifications compared to the any individual reactor shell (20) for process optimization reasons, if desired. This allows an additional freedom for design optimization while scaling-up the system to carrying out an endothermic reaction.
  • the cascaded reactor system (10) comprises an insulation filling (60) that is at least partially encompassing the internal sections of the said plurality of reactor shells (10) along the entirety of the reactive stream duct (22), and configured in a way to not cause any obstruction to the flow of the reactive gas stream.
  • the catalytically active species supported on the structured ceramic catalyst bed (30) are transition metals of the d-block elements and/or combination of two or more active species possibly including alkali metals.
  • the structured ceramic catalyst bed (30) may undergo heterogeneous catalyst preparation as incipient wetness impregnation and/or impregnation and/or support wash coating and/or in-situ synthesis that are traditionally used in the synthesis of heterogeneous catalysts.
  • the electrical heating means (40) is arranged at the structured ceramic catalytic bed (30) within the hollow flow paths (31) so that the catalyst bed (30) is heated from inside.
  • the electrical heating means (40) is meandered (comprising meandered sections (41)) through some or all of the hollow flow paths (31). Thanks to this embodiment, the hollow flow paths (31) are heated up by the electrical heating means (40) so that the structured ceramic catalyst bed (30) is heated from inside.
  • the physical proximity (or contact) of the electrical heating means (40) with the structure ceramic catalyst bed (30) and the direct contact with the reactive mixture stream enhances the heat transfer via irradiation, convection, and conduction. The proximity will make it possible to operate the structured ceramic catalyst bed (30) at temperature between 300 °C to 1300 °C.
  • the cascaded reactor system (20) in which it is possible to modularly increase the number of reactor shells (20), it is possible to keep a desired gas space velocity of the reactive stream mixture by providing the same catalyst volume distributed on a multiplicity of relatively short and with relatively small cross section catalyst sections (21). This allows to reduces the mechanical deformation and the risk of shortcutting of the electrical heating means (41) and provides an even distribution of the reactive mixture stream.
  • the invention is also disclosing a method for carrying out an endothermic reaction utilizing the above described cascaded reactor system (10) comprising a plurality of reactor shells (20) connected in series, where a fed reactive stream flowing downstream is to be subjected to catalytic reaction when it interacts with the series of structured ceramic catalytic beds (30) along the entirety of the reactive stream duct (22).
  • the method comprises the steps of:
  • electrical energy is provided with the power supply (50) through the electrical feeds (51) to the electrical heating means (41) of each of the individual reactor shell (20) of the plurality of such, so that the structured ceramic catalyst bed (30) located at each reactor shell (20) is heated up.
  • the reactive mixture stream is fed to the first reactor shell (20) in series allowing the reactive stream mixture to pass through the hollow flow paths (31) of all of the structured ceramic catalyst beds (30) located in series along the reactive stream duct (22).
  • the reactive mixture stream is allowed to pass from the stream outlet (26) of the last reactor shell (20) in series.
  • the reactive mixture is a mixture of a nebulized liquid and/or gas hydrocarbon and/or methane- containing, and/or of a water steam, and/or of an oxidant stream and/or carbon dioxide and/or hydrogen and/or ammonia and/or volatile organic compounds (VOC).
  • a nebulized liquid and/or gas hydrocarbon and/or methane- containing and/or of a water steam, and/or of an oxidant stream and/or carbon dioxide and/or hydrogen and/or ammonia and/or volatile organic compounds (VOC).
  • VOC volatile organic compounds
  • the reactive mixture stream is fed to the cascaded reactor system (10) at the stream inlet (25) of the first reactor shell (20) in series at a temperature ranging from 25°C to 700°C and a pressure ranging from 1 and 150 bar.
  • the reactive mixture stream enters to the reactive stream duct (22) from the stream inlet (25) and fed through the hollow flow paths (31) located between the structured ceramic catalyst bed (30) and the electrical heating means (40) simultaneously reacting on the active phase of the catalyst and being heated up by the heat provided by the electrical heating means (40) up to temperature between 300°C and 1300°C.
  • the reactive mixture stream passes from the stream outlet (26) of the previous unit to the stream inlet (26) of the next unit in series at a temperature that can be modulated by controlling separately the power supply (50) of each reactor shell (20).

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (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 système de réacteur en cascade (10) et un procédé de mise en œuvre d'une réaction endothermique à partir d'un flux de mélange réactif alimenté caractérisé en ce qu'il comprend une pluralité d'enveloppes de réacteur (20) raccordées chacune en série comportant chacune au moins un conduit de flux réactif (22), une entrée de flux (25) destinée à recevoir le flux de mélange réactif alimenté, une sortie de flux (26), une section de catalyseur (21) prévue à l'intérieur dudit conduit de flux réactif (22) entre lesdites entrée de flux (25) et sortie de flux (26), un remplissage à isolation (60) entourant au moins en partie ledit conduit de flux réactif (22), un lit de catalyseur céramique (30) logé dans ladite section de catalyseur (21), le flux de mélange réactif étant soumis à une réaction catalytique, des moyens de chauffage électrique (40) pour chauffer ledit lit de catalyseur céramique structuré (30) jusqu'à une température de réaction prédéterminée, au moins deux alimentations électriques (51) traversant la section d'entrée raccordées à une alimentation électrique (50) prévue à l'extérieur du conduit de flux réactif (22), la section d'entrée d'au moins un récipient sous pression contenant un dispositif de séparation destiné à créer une section froide à l'intérieur de la zone d'entrée de ladite enveloppe de réacteur (20).
PCT/EP2024/084686 2023-12-05 2024-12-04 Système de réacteur en cascade et procédé de mise en œuvre d'une réaction endothermique Pending WO2025119981A1 (fr)

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Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2119710A1 (fr) * 2008-05-14 2009-11-18 Urea Casale S.A. Processus de production de mélamine haute qualité à partir de l'urée
US20100234557A1 (en) * 2006-01-30 2010-09-16 Hiroyuki Sato Process For Producing Aliphatic Polyester
EP3574991A1 (fr) 2018-05-31 2019-12-04 Haldor Topsøe A/S Reformage à la vapeur chauffée par un chauffage à résistance
EP3895795A1 (fr) 2020-04-18 2021-10-20 Gianluca Pauletto Réacteur comportant un catalyseur de céramique structuré chauffé électriquement
WO2022129338A1 (fr) * 2020-12-18 2022-06-23 Shell Internationale Research Maatschappij B.V. Procédé de production de gaz de synthèse à l'aide d'une conversion de gaz à l'eau inverse catalytique
US20220362736A1 (en) * 2019-10-01 2022-11-17 Haldor Topsøe A/S Offshore reforming installation or vessel
US20220410103A1 (en) * 2019-12-23 2022-12-29 Shell Oil Company Electrically heated reactor, a furnace comprising said reactor and a method for gas conversions using said reactor
US20230001368A1 (en) * 2019-12-04 2023-01-05 Haldor Topsøe A/S Gas heater

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20100234557A1 (en) * 2006-01-30 2010-09-16 Hiroyuki Sato Process For Producing Aliphatic Polyester
EP2119710A1 (fr) * 2008-05-14 2009-11-18 Urea Casale S.A. Processus de production de mélamine haute qualité à partir de l'urée
EP3574991A1 (fr) 2018-05-31 2019-12-04 Haldor Topsøe A/S Reformage à la vapeur chauffée par un chauffage à résistance
US20220362736A1 (en) * 2019-10-01 2022-11-17 Haldor Topsøe A/S Offshore reforming installation or vessel
US20230001368A1 (en) * 2019-12-04 2023-01-05 Haldor Topsøe A/S Gas heater
US20220410103A1 (en) * 2019-12-23 2022-12-29 Shell Oil Company Electrically heated reactor, a furnace comprising said reactor and a method for gas conversions using said reactor
EP3895795A1 (fr) 2020-04-18 2021-10-20 Gianluca Pauletto Réacteur comportant un catalyseur de céramique structuré chauffé électriquement
US20230149890A1 (en) * 2020-04-18 2023-05-18 Gianluca PAULETTO Reactor with electrically heated structured ceramic catalyst
WO2022129338A1 (fr) * 2020-12-18 2022-06-23 Shell Internationale Research Maatschappij B.V. Procédé de production de gaz de synthèse à l'aide d'une conversion de gaz à l'eau inverse catalytique

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