WO2021121451A1 - Procédé et réacteur pour réactions catalytiques exothermes en phase gazeuse - Google Patents

Procédé et réacteur pour réactions catalytiques exothermes en phase gazeuse Download PDF

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Publication number
WO2021121451A1
WO2021121451A1 PCT/DE2020/000304 DE2020000304W WO2021121451A1 WO 2021121451 A1 WO2021121451 A1 WO 2021121451A1 DE 2020000304 W DE2020000304 W DE 2020000304W WO 2021121451 A1 WO2021121451 A1 WO 2021121451A1
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flow
gas
corrugated
flow channels
webs
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PCT/DE2020/000304
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German (de)
English (en)
Inventor
Andreas Hartbrich
Alexander Jekow
Ruprecht Marxer
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Silica Verfahrenstechnik Gmbh
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Publication of WO2021121451A1 publication Critical patent/WO2021121451A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0438—Cooling or heating systems
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0446—Means for feeding or distributing gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0462—Temperature swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/72—Organic compounds not provided for in groups B01D53/48 - B01D53/70, e.g. hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/81—Solid phase processes
    • B01D53/82—Solid phase processes with stationary reactants
    • 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
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/248—Reactors comprising multiple separated flow channels
    • B01J19/249—Plate-type reactors
    • 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
    • B01J19/32—Packing elements in the form of grids or built-up elements for forming a unit or module inside the apparatus for mass or heat transfer
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • F28D21/0015—Heat and mass exchangers, e.g. with permeable walls
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D9/0025—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being formed by zig-zag bend plates
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D9/0031—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for one heat-exchange medium being formed by paired plates touching each other
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D9/0062—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for one heat-exchange medium being formed by spaced plates with inserted elements
    • F28D9/0075—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for one heat-exchange medium being formed by spaced plates with inserted elements the plates having openings therein for circulation of the heat-exchange medium from one conduit to another
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F3/00—Plate-like or laminated elements; Assemblies of plate-like or laminated elements
    • F28F3/02—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations
    • F28F3/04—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations the means being integral with the element
    • F28F3/048—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations the means being integral with the element in the form of ribs integral with the element or local variations in thickness of the element, e.g. grooves, microchannels
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/104—Alumina
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B01D2253/108—Zeolites
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/704—Solvents not covered by groups B01D2257/702 - B01D2257/7027
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/708—Volatile organic compounds V.O.C.'s
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/06—Polluted air
    • 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
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2451—Geometry of the reactor
    • B01J2219/2456—Geometry of the plates
    • B01J2219/2459—Corrugated plates
    • 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
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    • B01J2219/245—Plate-type reactors
    • B01J2219/2461—Heat exchange aspects
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2476—Construction materials
    • B01J2219/2477—Construction materials of the catalysts
    • B01J2219/2481—Catalysts in granular from between plates
    • 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
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    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/322—Basic shape of the elements
    • B01J2219/32203—Sheets
    • B01J2219/3221—Corrugated sheets
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/322—Basic shape of the elements
    • B01J2219/32203—Sheets
    • B01J2219/32248—Sheets comprising areas that are raised or sunken from the plane of the sheet
    • B01J2219/32251—Dimples, bossages, protrusions
    • 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
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/322—Basic shape of the elements
    • B01J2219/32279—Tubes or cylinders
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • 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
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/324—Composition or microstructure of the elements
    • B01J2219/32466—Composition or microstructure of the elements comprising catalytically active material
    • 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
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/324—Composition or microstructure of the elements
    • B01J2219/32466—Composition or microstructure of the elements comprising catalytically active material
    • B01J2219/32475—Composition or microstructure of the elements comprising catalytically active material involving heat exchange

Definitions

  • the invention relates to a method for the exothermic reaction between gases, for example for the catalytic treatment of a gas loaded with undesirable gaseous components, in particular process gases, in which a reaction gas such as oxygen, hydrogen or carbon monoxide is added to the process gas or carbon dioxide with hydrogen on a catalyst Reaction is brought about, the gas mixture is heated to reaction temperature in a heater and a plurality of flow channels filled with a catalyst bed via a supply-side distribution space of at least one plate heat exchanger, the corrugated and / or corrugated and / or corrugated and / or corrugated or profiled sheet pairs lying mirror-image one on top of the other by webs Profiled sheets are formed, flowed through in parallel divided partial flows, the undesired constituents being oxidized or burned on the catalyst of the catalyst bed and the heat of reaction through a flow channel Men, which are formed between the corrugated or profiled sheet metal pairs, in the cross flow of the cooling medium to the flow channels is indirectly discharged, and the partial flows after leaving the flow channels
  • the invention further relates to a reactor for carrying out the
  • Method with at least one plate heat exchanger which comprises a multiplicity of flow channels, which are arranged next to one another and filled with a catalyst bed, and flow spaces which are perpendicular to them and which are connected by
  • CONFIRMATION COPY Corrugated and / or profiled sheets lying mirror-inverted, connected by webs and combined into pairs of corrugated sheets are formed, the flow spaces being arranged between the pairs of corrugated sheets, and the flow channels for the passage of the partial flows separated from the process gas and reaction gas on the inflow side with a distribution space and on the outflow side with a collecting space are connected with open flow, the inflow-side distribution space being connected to a supply line for a mixture of process gas and reaction gas and the outflow-side collecting space being connected to a clean gas line, and the flow spaces opening into a distribution space for supplying and removing a cooling medium for indirect cooling of the catalyst bed.
  • catalysts made of platinum, palladium or mixtures thereof which are in a bed through which the gas to be cleaned flows (DE 33 18 098A1, DE 35 05 351 A1, DE 197 54 185 C1, DE 198 09 200 A1), or in a Bed arrangement of the catalyst between heat exchanger plates (DE 103 61 515 A1, EP 0 534 295 A1, EP 2 718 086 B1, EP 1 284 813 B1, DE 603 17 545 A2).
  • a complete description of a catalyst bed includes the shape, size and size distribution of the catalyst particles.
  • a catalyst bed in a fixed bed there is a very large ratio of the bed dimensions to the particle size, so that the disruptive influence of the wall delimiting the bed is negligible.
  • this interference is no longer negligible, because the bulk density is lowest directly on the wall and therefore results in a lower pressure loss, which leads to a higher flow velocity, the so-called edge accessibility.
  • the catalyst beds have a particle size distribution with a deviation from the mean particle size, as a result of which the particles with a smaller size fill the gaps between the larger particles, so that the bulk density in the vicinity of the wall also increases, so that the marginal accessibility is negligibly small . If the bulk density increases, the pressure loss also increases and the properties of the bed change with regard to the flow rate, the mixing properties and the interaction with the catalyst or the reaction behavior and heat transport (DE 20 2006 014 118 U1).
  • flow channels in cross-flow plate heat exchangers do not have a constant internal width due to production, so that the bulk density from flow channel to flow channel is not the same and the reaction behavior in the Flow channels is different.
  • the conversion reactions are predominantly exothermic in nature, i.e. the heat released during the oxidation can, due to the different reaction behavior, favor the formation of so-called hot spots in the catalyst bed, which makes the catalyst unusable.
  • an inner tube of a plate heat exchanger with a catalyst or with packing is known (DE 34 11 675 A1).
  • a device is proposed for heat and mass exchange between two or more flowable media or for initiating a reaction between the media with an inlet and an outlet for one medium and an inlet and outlet for the other medium and at least two enclosing pipes from where one is connected to the one and the other to the other inlet / outlet. Both ends of the inner tube are passed through the outer tube, which protrudes with its ends.
  • the inner tube can be filled with a catalyst or with packing.
  • a plurality of inner and outer tubes surrounding one another can also be arranged next to one another and the inner and outer tubes can also be formed with plates that are spaced apart from one another and run parallel to one another .
  • an apparatus in particular for use as a chemical reactor and / or adsorber and / or regenerator is known, which is constructed essentially cylindrically symmetrical about a preferred axis and contains at least two beds of particles that act catalytically and / or adsorptively and / or heat-storing.
  • the apparatus has means for supplying and removing gaseous or liquid media, which are assigned to the ends of the beds facing away from one another and the ends facing one another.
  • EP 1 975 539 A2 is a heat exchanger or chemical
  • a reactor comprising a heat exchange body defining one or more fluid flow channels and having a removable insert.
  • the insert includes a series of contact plates stacked along a common axis and press fit into one of the flow channels thereby providing secondary heat exchange surfaces in thermal contact with the primary wall surfaces.
  • the first possibility is to arrange the catalyst as a supported layer in the flow channel (EP 1 195 193 B1, EP 1 361 919 B1, EP 1 430 265 B1, DE 11 2006 000 447 T5, EP 1 434 652 B1, WO 03/095924 Al).
  • the particle size in these cases is less than 0.15 mm, so that this approach is suitable for flow channels with small cross-sections and closed flow channels of plate heat exchangers.
  • the catalyst or the adsorbent is introduced as a bed or packing into a relatively open, unimpeded flow passage with larger flow cross-sections (WO 2006/075 163 A2).
  • the particle sizes used here are more than 2 to 3 mm. If the catalyst packing is used up, it must be removed from the flow channels by pressing the packing through a rod inserted into the flow channel.
  • the invention is based on the object of providing a method and a reactor with which it is possible on an industrial scale cross-flow plate heat exchangers with slim flow channels for treating a gas loaded with undesirable constituents or for exothermic reaction between Use of gases by equalizing the reaction behavior of the catalyst bed in the flow channels of the heat exchanger, reducing the risk of blockage of the flow channels filled with catalyst and the formation of hot spots in the catalyst bed, the ability of the gas to pass the edge of the catalyst while at the same time increasing the economy and Security is largely avoided.
  • Mass transfer small cross-shear between the gas and the catalyst flow channels of the catalyst-filled cross-flow plate heat exchanger to be used and at the same time to utilize the run in the cross ⁇ or countercurrent to the flow channels of the mass transfer flow channels for the heat exchange with the catalyst in the form of a cooling during the oxidation.
  • Cross-flow plate heat exchanger with open flow channels from the distribution chamber to the collecting chamber with a clear width of at least 10 to a maximum of 120 mm, flow transitions between adjacent flow channels, flow baffles positioned in the flow channels and flow paths in the flow spaces for the cooling medium forming flow baffles and spacer plates in the following steps: a) simultaneous generation of turbulence in the partial flows of the mixture of process gas and reaction gas within the flow channels and in the cooling medium within the flow spaces, b) splitting the gas mixture of process gas and reaction gas into bypass flows during the catalytic reaction and introducing the bypass flows sideways into the passage openings of the flow transitions directed into the adjacent flow channels.
  • the turbulence in the gas mixture of process gas and reaction gas are generated according to a preferred embodiment of the method according to the invention by flow chicanes that are formed as expressions perpendicular and / or transverse to the flow direction in the wall of the flow channel at the same time as the corrugated bending or rolling of the corrugated sheets, wherein the expressions are aligned inwardly into the flow channel and / or outwardly into the flow space.
  • the flow chicanes contribute to the fact that the partial flow of the process gas entering the flow channel is also directed into the interior of the flow channel and turbulence is generated, which counteracts the formation of marginal accessibility along the wall of the flow channel.
  • the turbulence generated also has the advantage that the cooling medium from the to the outside in the flow spaces directed forms is swirled directly on the surface and thus improves the heat exchange.
  • the turbulence in the cooling medium positioned in the flow spaces between the corrugated sheet pairs flow directing ⁇ or spacer sheets are produced, wherein the cooling medium during the catalytic reaction in the cross current on to the flow channels, or can be performed more smoothly.
  • cooling medium In the event that the cooling medium is to be guided in multiple ways, adjacent flow spaces are alternately connected to one another, as a result of which the cooling medium is diverted from flow space to flow space.
  • the flow guide and spacer plates in the flow spaces between the pairs of corrugated sheets force a constant deflection of the cooling medium flowing past the flow channels, so that the indirect heat exchange with the catalytic converter is highly effective.
  • the flow guide and spacer plates ensure an exact distance between the corrugated sheet metal pairs lying above or below one another and enable a stable and compact design.
  • the method provides that the size of the passage opening for the bypass flow is determined by the number of flow transitions, the respective passage opening being adapted to a size and shape that is smaller than the size and shape of the smallest particle size of the catalyst bed.
  • the passage opening of a flow transition thus defines a cross-sectional area over which a certain amount of the partial flow divided by the process gas and entering the respective flow channel reaches the adjacent flow channel as a bypass flow, so that the size of the bypass flows with the cross-sectional area of all passage openings and their distribution along the webs determined and a uniform or uneven distribution of the bypass flows over the adsorbent in the respective adjacent flow channel can be achieved.
  • the number of flow transitions in the webs in the vicinity of the supply-side distribution space can be greater than the number of flow transitions in the webs close to the discharge-side distribution space, ie the number of flow transitions distributed along the webs can vary.
  • the flow transition can be formed from a recess / groove formed in the webs of the corrugated or profiled sheets when the corrugated or profiled sheets are placed on top of each other and covered by the area of the webs above or below them when the corrugated or profiled sheets are placed on top of one another and the webs lying on top of one another are firmly bonded by laser welding or brazing are connected, a weld seam being penetrated by the depression in the longitudinal direction of the webs and the depression being sealed gas-tight by weld seams in the transverse direction of the webs.
  • the flow transition is formed when the corrugated or profiled sheets are loosely laid one on top of the other from a flat gap between the webs, in that the webs are materially connected by laser line welding with weld seams in such a way that the gap interrupts the weld seam in the longitudinal direction of the webs and the gap by parallel lines on both sides Weld seams in the transverse direction of the webs is sealed gas-tight.
  • the clean gas can be fed to a cooler and condensed water can be separated from the clean gas.
  • the water content in the clean gas can be further reduced to a value of less than 1 ppmv.
  • the further embodiment of the method according to the invention provides that loose beds are used as the catalyst, which include the following materials: palladium, platinum, vanadium, tungsten, chromium, molybdenum, titanium, manganese, cobalt, nickel, silver, copper, zinc , Iron, aluminum, silicon, magnesium, phosphorus, beryllium and its oxides, barium, ruthenium or their Mixtures with an average particle size between 0.6 to 6.0 mm can be used.
  • the cooling medium used is water or a water-glycol mixture or thermal oil.
  • the plate heat exchanger is a modified cross-flow plate heat exchanger with flow channels open to flow from the distribution chamber to the collecting chamber with the following features: a) the flow channels have a clear width of at least 10 to a maximum of 120 mm , b) Adjacent flow channels are connected by flow transitions formed in the webs for the sideways introduction of bypass flows from the respective partial flow of the gas mixture into the flow channels, c) flow baffles for generating turbulence in the respective partial flow of the gas mixture are arranged within the flow channels and d) in the flow spaces between the pairs of corrugated sheets, flow guide sheets and spacer sheets that form flow paths are arranged for generating turbulence in the cooling medium.
  • the flow guide and spacer sheet comprises a thin corrugated sheet with spacer profiles that are formed into the corrugation crests and exceed the height of the corrugation crests, which are offset from one another from wave crest to wave crest, with the spacer profiles in the corrugated sheet metal pairs formed by the webs of the corrugated sheet pairs lying above and below one another Engage in an offset supporting manner and the respective spacer profile is fixed in a materially bonded manner at each end on the associated pair of corrugated sheets.
  • the flow guide and spacer plates not only generate the turbulence in the cooling medium, but at the same time also keep the corrugated iron pairs formed from the mirror-inverted corrugated iron sheets at a distance from one another, so that the cooling medium flows in cross-flow to the flow channels during the catalytic reaction. or can be guided through the flow spaces in several ways without hindrance. Furthermore, the flow guide and spacer plates contribute to a compact design of the reactor according to the invention.
  • Flow baffles are formed by embossments which are formed transversely and / or parallel to the flow direction of the respective partial flow of the gas mixture in the wall of the flow channels inwards and / or from the wall outwards.
  • the flow baffles make it possible to direct the partial flow of the process gas entering the respective flow channel into the interior of the channel and to generate turbulence which counteracts the marginal accessibility, in particular in flow channels with a small cross section.
  • the flow transition is arranged transversely to the longitudinal direction of the webs, the passage openings of which open into the adjacent flow channels, the flow transition being formed from at least one recess / groove formed in the web, which is formed by the above- or the region of the web arranged laterally reversed to it is covered, the webs being materially connected in the longitudinal and transverse directions.
  • the material connection can comprise weld seams or brazed connections produced by laser line welding.
  • the flow transition can consist of at least one flat gap with passage openings between the webs connected in a gas-tight manner in the longitudinal direction with a weld seam, the webs being sealed gas-tight in the transverse direction by welds running parallel to the gap.
  • the passage openings associated with the depression or the gap have a geometry or shape that is smaller than the dimensions and shape of the smallest particle size of the catalyst bed, so that catalyst particles cannot get from one flow channel into the other.
  • the passage opening of the flow transition has a cross-sectional area over which a certain amount of the partial flow of the gas mixture that has entered the flow channel passes as a bypass flow into the respective adjacent flow channel, the respective passage opening being of a size and Shape is adapted, which is smaller than the size and shape of the smallest particle size of the catalyst bed. This ensures that the particles of the catalyst bed cannot get into adjacent flow channels via the passage opening.
  • the flow channels on the inflow and outflow side are covered with a sieve which can flow through and dismantle the process gas, reaction gas and clean gas, the mesh size of which is smaller than the smallest particle size of the catalyst bed. If it becomes necessary to replace the catalyst, the sieve can be dismantled from the flow channels and the used catalyst bed can be easily removed via the distribution chamber on the supply side.
  • the flow channels are filled with new catalyst after removing the outflow-side screen and reassembling the inflow-side screen vertically into the open flow channels via the outflow-side distribution space.
  • a reaction gas line for admixing reaction gas in the flow direction upstream of the heater binds into the supply line for the process gas.
  • Another embodiment of the reactor according to the invention provides that a cooler with a condensate drain for condensed water is integrated into the clean gas line.
  • a cooler with a condensate drain for condensed water is integrated into the clean gas line.
  • an economizer can also be used Heat recovery can be used.
  • the cooling circuit assigned to the flow spaces for the heat exchange in the cross-flow ensures that the heat of reaction can be dissipated directly at the point where it is generated, thereby smoothing out the reaction behavior on the catalyst and at the same time avoiding overheating of the catalyst bed becomes.
  • the catalyst consists of a loose bed of particles, which comprises the following materials: palladium, platinum, vanadium, tungsten, chromium, molybdenum, titanium, manganese, cobalt, nickel, silver, copper, zinc , Iron, aluminum, silicon, magnesium, phosphorus, beryllium and its oxides, barium, ruthenium or their mixtures with an average particle size between 0.6 and 6.0 mm.
  • the particle size is matched to the dimensions, the cross section and the shape of the flow channels so that the particles are at a small distance from the wall of the flow channel for high heat conduction.
  • the reactor provides that the modified cross-flow plate heat exchanger forms a rectangular structural unit which is arranged in the interior of a rectangular or cylindrical housing, the distribution space being designed as a foot part, the collecting space being designed as a head part, and the distribution space for the cooling medium enclosing all flow spaces with open flow .
  • the structural unit has an inflow-side floor and an outflow-side floor, the respective floor consisting either of a single molded part or of several molded parts adapted to the contour of the flow channels, which are firmly connected to each other and to the corrugated sheet metal bar .
  • each structural unit being provided with an inflow-side distribution space, an outflow-side collection space and a distribution space for the cooling medium, and the distribution spaces and collection spaces are flow-connected to one another through the flow channels.
  • the modified cross-flow plate heat exchangers consist of thin stainless steel sheet, carbon steel sheet, copper or aluminum sheet with a thickness of 0.1 mm to 1.0 mm, which is formed by corrugated rolling into corrugated or profiled sheet with different profile shapes.
  • the corrugated sheets can have a semicircular, oval, triangular, trapezoidal or square profile, so that when the profiled or corrugated sheets are placed on top of one another, the resulting flow channels have a tubular, wave-like, rhombic, rectangular or polygonal cross-section.
  • FIG. 1 a is a perspective exploded view of two mutually offset, mirror-inverted pairs of corrugated iron sheets, in whose mutually cohesively connected webs at least one flow transition is formed from depressions,
  • FIG. 1b shows a section along the line A ⁇ A in FIG
  • FIG. 1c shows a section along the line B-B of FIG.
  • FIG. 1d shows a section along the line OC in FIG [0045]
  • FIG. 2 shows a detail in plan view of FIG.
  • FIG 3 shows a perspective illustration of the flow guide and spacer plate inserted in the flow spaces between the pairs of corrugated sheets.
  • FIG. 5 shows an example of flow baffles in the wall of a
  • FIG. 6 is a side view of a modified cross-flow
  • FIG. 7 is a side view of a modified cross-flow plate heat exchanger in the interior of a cylindrical housing
  • Plate heat exchanger from, for example, two structural units arranged one above the other,
  • Fig. 9a shows a section along the line D-D of Fig. 9,
  • Fig. 9b shows a section along the line E-E of Figs. 9a and
  • Fig. 10 is a schematic representation of the inventive
  • La shows the basic structure of pairs of corrugated sheets 7c, which consist of mirror-inverted corrugated sheets 7a and 7b made of stainless steel with a thickness of 0.3 mm.
  • the corrugated sheets 7a and 7b with their corrugated profiles 8 each form vertical flow channels 9 lying parallel to one another, the webs 10a and 10b of which face one another.
  • At least one indentation 14a or 14b is formed in the web 10a or 10b transversely to the longitudinal direction LR over the entire width B of the web 10a or 10b, which is introduced when the corrugated or profiled sheets 7a or 7b are corrugated.
  • the depressions 14a and 14b are each laterally reversed and are covered by the web 10a and 10b of the corrugated or profiled sheet 7a and 7b located above and below.
  • the flat areas of the webs 10a and 10b facing one another are superimposed on one another and support one another.
  • the webs 10a and 10b are mechanically pressed together, fixed and connected in a gas-tight manner by laser welding or brazing in the longitudinal direction LR.
  • the depressions 14a and 14b thus penetrate the cohesive connection / weld seam 16a running in the longitudinal direction LR in the transverse direction QR.
  • the gas-tight connection between webs 10a and 10b lying one above the other is made by further weld seams 16b running parallel to the respective indentation 14a and 14b, as can be seen from FIGS. 1b and 1c.
  • the depressions 14a and 14b represent depressions in the webs 10a and 10b, the webs in the area of the depressions 14a and 14 do not touch and remain unwelded, so that a flow transition 17 with passage openings 18 is created, which into the respective adjacent flow channels 9 open.
  • the depressions 14a and 14b have a depth T which is smaller than the smallest grain size of the catalyst of the catalyst bed KS, so that no catalyst particles can get from one flow channel into the other flow channel.
  • the corrugated metal couples 7c above ⁇ or arranged to each other and face each other an offset 24, wherein the over- or under-side corrugated sheet pairs 7c are spaced apart and form between themselves flow spaces 12, in which a cooling medium K in cross flow to the flow channel 9 catchy, ie simultaneously by all flow spaces 12 can be guided.
  • the cooling medium K it is likewise also possible for the cooling medium K to be passed through the flow spaces 12 in several ways, ie one after the other. In such a case, adjacent flow spaces 12 are connected to one another, as a result of which the cooling medium K is deflected from flow space to flow space.
  • the corrugated or profiled sheets 7a and 7b have a semicircular, oval, triangular, trapezoidal or square profile 8, so that when the corrugated or profiled sheets 7a or 7b are placed on top of one another, the flow channels 9 are tubular, wave-like, rhombic, rectangular or polygonal May have cross-section.
  • a flow guide and spacer sheet 22 shaped like a corrugated sheet is inserted.
  • spacer profiles 23 are formed at regular intervals from one another, each of which engages alternately in a supporting manner in the area of the corrugated sheet pairs 7c formed by the offset 24, the spacer profile 12 on the respective corrugated sheet pair 7c at the beginning and end is firmly attached, so that a displacement of the flow guide and spacer plate 22 in the flow space 12 is excluded.
  • the flow guide and spacer plates 22 contribute to the stiffening of the corrugated sheet metal pairs 7c arranged above or below one another.
  • the spacer profiles 23 are in the adjacent Wave crests WB of the flow guide and spacer plate 2 are arranged offset to one another on a gap 25, so that flow paths SF arise which force the cooling medium K guided in the cross flow to deflect and thereby generate turbulence.
  • An example of a flow path SF is indicated by arrows in FIG. 3.
  • FIGS 4a and 4b illustrate the structure of one of several
  • Corrugated iron pairs 7c composite unit la The pairs of corrugated sheets 7c with their open-ended flow channels 9 penetrate a head-side floor 26 and a downstream-side floor 27.
  • the bases 26 and 27 are composed of molded parts 26.1 to 26.n and 27.1 to 27.n, the contour of which is adapted to the shape and dimensions of the corrugated sheet metal pairs 7c, expediently by laser cutting.
  • the molded parts are joined together with the inserted corrugated sheet metal pairs 7c along the contour and materially connected by laser welding or brazing, so that an essentially rectangular structural unit is created that can be inserted into a rectangular or cylindrical housing 2 as required.
  • the joining direction is indicated by an arrow in FIG. 4b.
  • the flow channels 9 - as shown in Fig. 5 - have flow baffles 19, which are formed in the corrugated profile 8 of the corrugated sheets 7a or 7b in the form of embossed areas 21 and from the wall 20 into the interior of the flow channels 9 protrude and / or emerge from the wall 20 into the flow space 12 for the cooling medium K.
  • the embossments 21 are arranged transversely and parallel to the flow direction SRR of the partial flow TG of the gas mixture on the wall 20 of the flow channels 9.
  • the flow baffles 19 have the effect that the gas located in the vicinity of the wall is directed into the interior of the flow channel 9 and thus turbulence is generated which largely prevents the passage on the edge.
  • 6 shows the structure of the reactor according to the invention in
  • Plate heat exchanger 1 is housed as a structural unit la in a housing 2 made of stainless steel.
  • the housing 2 consists of a rectangular housing jacket 2a, in the interior of which the structural unit 1 is arranged.
  • the head-side bottom 26, together with a head part 28 belonging to the housing 2 is flanged on the end face of the wall 29 of the housing jacket 2a, so that a distribution space 3 for the gas mixture of process gas G and reaction gas GR is created on the inflow side, into which the gas mixture is fed via a with the head part 28 connected supply line 4 enters.
  • the foot-side floor 27 of the structural unit la and a foot part 30 flanged at the end face to the wall 29 of the housing shell 2a form a collecting space 5 for the clean gas RG leaving the flow channels 9, which is fed to a consumer (not shown) via a discharge line 6 connected to the foot part 30 is released into the atmosphere as exhaust air.
  • the inflow-side distribution space 3 is located at the top of the cross-flow plate heat exchanger 1, whereby the flow direction SRR of the gas mixture of process gas G and reaction gas GR runs vertically downward through the structural unit la.
  • the gas mixture can also flow vertically upwards through the structural unit la.
  • the flow channels 9 filled with a catalyst are preferably aligned vertically and connect the distribution space 3 with the collecting space 5, open to flow through, the flow channels 9 are covered at the end with a removable gas-permeable sieve 11 each.
  • the sieve 11 has a mesh size which is selected to be smaller than the smallest grain size of the particles of the catalyst bed KS filled into the flow channels 9, so that the catalyst cannot get out of the flow channels.
  • the flow channels 9 have a clear width (W) of at least 10 to a maximum of 120 mm.
  • W clear width
  • the length of the flow channels can be 1 to 2 m and the mean particle size of the catalyst can be 0.6 to 6 mm.
  • Process gas G enters together with a reaction gas GR via feed line 4 in the distribution space 3 and is divided into partial flows TG, each of which flows through a flow channel 9 filled with a catalyst, for example palladium or platinum, and is catalytically converted on the catalyst.
  • a catalyst for example palladium or platinum
  • the modified cross-flow plate heat exchanger 1 has a collecting space 5 for the clean gas RG, which is fed via a discharge line 6 to a consumer, not shown further.
  • the structural unit la arranged in the interior of the housing 2 is surrounded by a distribution space 13 for the supply and discharge of a cooling medium K, which is formed between the wall 29 of the housing jacket 2a and the structural unit la.
  • the flow spaces 12 between the corrugated sheet metal pairs 7c open into the distribution space 13 with open flow.
  • the head-side bottom 26 of the structural unit la rests on the wall 29 of the housing jacket 2a of the housing 2 and is end-or-end together with the head part 28 in the form of a dished bottom and the foot-side bottom 27 of the structural unit la with the foot part 30. flanged at the foot to the wall 29 of the cylindrical housing jacket 2a.
  • the distribution space 3 and the collecting space 5 are formed by the head part 28 and the foot part 30 with the corresponding floors 26 and 27 of the structural unit la.
  • the modified cross-flow plate heat exchanger 1 consists of thin stainless steel, copper or aluminum corrugated sheet with a thickness between 0.1 and 3.0 mm,
  • FIG. 8 shows a reactor which consists of two structural units 1 a arranged one above the other, the two structural units being accommodated in a common housing 2.
  • 9, 9a and 9b show a second embodiment of a
  • the flow transition 17 is formed by a shallow gap 15 when the corrugated or profiled sheets are loosely placed on top of one another between the webs 10a and 10b.
  • the webs 10a and 10b are connected to one another in a gas-tight manner by a weld seam 16a which runs in the longitudinal direction LR and is interrupted by at least one gap 15.
  • the gap 15 provides a flow transition 17 with Passage openings 18, which connect the adjacent flow channels 9 to one another in an open-flow manner.
  • the gap 15 is sealed gas-tight in the transverse direction QR of the webs 10a and 10b by weld seams 16b (see FIG. 9b).
  • the number, geometry and shape of the flow transitions 17 can influence the size or quantity of the bypass flows BS reaching the flow channels 9. For example, depending on the design, the number of flow transitions 17 between adjacent flow channels 9 can be increased or decreased, so that the cross-sectional area QF can be adapted depending on the type of process gases and the catalyst KS and a blockage of the flow channels 9 due to an even or uneven distribution of the Bypass flows BS can be counteracted via the catalyst column.
  • Plate heat exchanger 1 leads the supply line 4 for the process gas G, which is conveyed into the distribution space 3 by a fan 31 connected to the supply line 4.
  • An electrically operated heater 32 is integrated into the supply line 4.
  • the measuring probes 34 and 35 belong to an automatic controlled system 36 which includes a shut-off valve 37 assigned to the measuring probe 34 with a switching valve 38 which opens or closes the reaction gas line 33, and a control valve 39 assigned to the measuring probe 35 which controls the amount of reaction gas GR at a Keeps the minimum value constant, so that only the amount of reaction gas GR that is absolutely necessary is consumed even in the case of strongly fluctuating operating conditions.
  • the measuring probes 34 and 35, the switching valve 38 and the regulating valve 39 are connected via control lines 31 to a control unit 41 which monitors the amount of the admixed reaction gas GR.
  • Process gas G is heated to a temperature at which the following reactions take place on the catalyst, depending on the presence of the gas components in the process gas:
  • Plate heat exchanger 1 a supply line 43 for the cooling medium K, which can be opened and closed by a shut-off valve 42, opens into the flow spaces 12, which ascends vertically in a cross flow to the flow channels 9 up to the flow space 12 below the collecting space 5 into a through a shut-off valve 44 opening. and closable discharge line 45 for the cooling medium K to be discharged.
  • the direction of flow of the cooling medium K runs horizontally ascending in the direction of flow of the divided substreams TG of the gas mixture of process gas G and reaction gas GR. The direction of flow is indicated by arrows.
  • the flow spaces 12 assigned to the distribution space 13 are at the same time connected to an emptying line 47 which can be opened and closed by a shut-off valve 46 Drain the cooling medium K connected.
  • the heater 32, the shut-off valves 42, 44 and 46 are electrically connected via the control lines 40 to the control unit 41, which outputs the setting commands for the shut-off valves 42 and 44 as a function of the reaction temperature set by the heater 32.
  • Process gas G and reaction gas GR are brought together in collecting space 5 and discharged as pure gas RG via discharge line 6.
  • the discharge line 6 is connected to a cooler 48, which discharges the water via a condensate drain 49.
  • shut-off valve 50 is in the supply line
  • shut-off valves 42 and 44 belonging to the cooling circuit are open, whereas the shut-off valve 46 of the drain line 47 is closed.
  • the process gas G heated to the reaction temperature with the admixed reaction gas GR thus reaches the distribution space 3, divides into partial flows TG, which flow vertically upwards into the flow channels 9 filled with catalyst KS.
  • the undesired gas components here hydrogen, oxygen, carbon monoxide or hydrocarbons, oxidize on the catalyst with the reaction gas GR to form water and carbon dioxide.
  • the heat of reaction generated during the oxidation is continuously removed by the cooling medium K, in this case water, which is guided in cross-flow to the flow channels 9 in the flow spaces 12.
  • a process gas G contaminated with oxygen is to be cleaned using the method according to the invention.
  • the following operating data are based on:
  • Catalyst 0.3% platinum or palladium on alumina gel
  • Catalyst large 1.0 to 2.5 mm
  • Width of the flow channels 20 mm
  • Reaction gas consumption approx. 28 m 3 / h.
  • Reaction product H2O approx. 21.1 kg / h
  • a residual content of less than 10 ppmv oxygen was achieved in the cleaned process gas.
  • the method according to the invention proceeds as follows.
  • the mixture of process gas G and reaction gas GR is fed into the distribution space 3 of the cross-flow plate heat exchanger 1 via the feed line 4 and the fan or compressor 31.
  • the reactor consists of a package of 10 stainless steel corrugated sheet
  • the vertical flow channels 9 are flowed around by a cooling medium K guided in flow spaces 12 in a cross flow, whereby the mass transfer taking place in the flow channel 9 on the catalyst KS is in heat exchange with the cooling medium K, so that the resulting reaction heat of approx. 80 kW is dissipated where it is generated becomes.
  • the catalyst KS used is platinum or palladium on an aluminum oxide gel with a particle size of 1.0 to 2.5 mm, which enters the flow channels 9 is poured.
  • a hydrogen produced regeneratively with an electrolyser is intended to react catalytically with carbon dioxide to methane (sebating process). This reaction is highly exothermic and requires intensive cooling of the reactor.
  • Catalyst Nickel, zirconium dioxide stabilized Catalyst size: 1.0 to 3.0 mm Length of the flow channels: 1,000 mm Width of the flow channels: 20 mm Inlet concentration: 80% by volume of H2, 20% by volume of CO2 Inlet temperature: approx. 120 to 150 ° C (Compression heat from the compressor)
  • Reaction temperature at the catalyst 20 to 350 ° C.
  • Heat of reaction to be dissipated approx. 260 kW
  • Cooling medium Thermal oil at 2.0 to 4.0 bar
  • Thermal oil conducted as a cooling medium K cross-flow in the flow spaces 12 ensures an exactly adjustable reaction temperature over the entire area of the flow channels 9, which leads to low by-product formation and thus to a very good methane yield.
  • the resulting reaction heat of approx. 260 kW can be dissipated very well both radially and axially and decoupled with the thermal oil and used well for further energetic use. Local overheating of the catalytic converter is avoided by the uniform dissipation of heat.
  • Flow transitions 17 allow at least one bypass flow BS into the adjacent flow channels 9. This makes it possible to dissolve an incipient blockage of the flow channels and at the same time to equalize the reaction conditions in the individual flow channels despite the tolerance differences in the internal dimensions of the flow channels 9 and thus not the same bulk quantities of catalyst.
  • the flow chicanes 19 arranged in the flow channels 9 also counteract the marginal accessibility in the flow channels 9 by generating turbulence.
  • Supply line for process gas G 4 collecting space on the downstream side from 1 5

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Abstract

L'invention concerne un procédé et un réacteur pour des réactions exothermes en phase gazeuse, rendant possible l'utilisation à grande échelle d'un point de vue technique d'échangeurs de chaleur à plaques à flux croisés dotés de canaux de circulation minces pour le traitement d'un gaz chargé en constituants indésirables ou pour la réaction exotherme entre des gaz, grâce à l'emploi d'au moins un échangeur de chaleur à plaques à flux croisés modifié comportant : des canaux de circulation ouverts au passage de flux d'une chambre de répartition à une chambre collectrice, un canal de circulation ayant une largeur intérieure d'au moins 10 jusqu'au maximum 120 mm ; des parties de transfert entre des canaux de circulation voisins (pour des flux de dérivation) ; des tôles de conduction de flux et d'espacement qui forment pour le liquide de refroidissement des chicanes de circulation positionnées dans les canaux de circulation et des voies de circulation formées dans les chambres de circulation, et qui servent à produire des turbulences dans des flux partiels du mélange à partir de gaz de processus et de gaz réactionnel à l'intérieur des canaux de circulation et dans le liquide de refroidissement à l'intérieur des chambres de circulation.
PCT/DE2020/000304 2019-12-17 2020-12-04 Procédé et réacteur pour réactions catalytiques exothermes en phase gazeuse WO2021121451A1 (fr)

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DE102019008705.4 2019-12-17
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DE102020007214.3A DE102020007214A1 (de) 2019-12-17 2020-11-25 Verfahren und Reaktor für exotherme Reaktionen in der Gasphase

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PCT/DE2020/000303 WO2021121450A1 (fr) 2019-12-17 2020-12-04 Appareil de froid à adsorption et procédé pour produire du froid d'adsorption à partir de chaleur
PCT/DE2020/000306 WO2021121453A1 (fr) 2019-12-17 2020-12-04 Dispositif et procédé pour traiter un gaz chargé en composants nuisibles et/ou utiles
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PCT/DE2020/000303 WO2021121450A1 (fr) 2019-12-17 2020-12-04 Appareil de froid à adsorption et procédé pour produire du froid d'adsorption à partir de chaleur
PCT/DE2020/000306 WO2021121453A1 (fr) 2019-12-17 2020-12-04 Dispositif et procédé pour traiter un gaz chargé en composants nuisibles et/ou utiles

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CN116589115A (zh) * 2023-04-25 2023-08-15 山东岱岳制盐有限公司 深井盐卤水净化处理系统

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CN114042363B (zh) * 2021-10-28 2024-04-09 西安建筑科技大学 一种抑制脱硫脱硝活性炭自燃的吸附塔及方法
DE102022000430A1 (de) 2022-01-26 2023-07-27 Apodis Gmbh Brennstoffzellensystem für ein Brennstoffzellenfahrzeug
DE102022000431A1 (de) 2022-01-26 2023-07-27 Apodis Gmbh Brennstoffzellensystem für ein Brennstoffzellenfahrzeug

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