Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
  • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
  • B01J8/34—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with stationary packing material in the fluidised bed, e.g. bricks, wire rings, baffles
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/005—Separating solid material from the gas/liquid stream
  • B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/005—Separating solid material from the gas/liquid stream
  • B01J8/006—Separating solid material from the gas/liquid stream by filtration
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
  • B01J8/1836—Heating and cooling the reactor
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B7/00—Halogens; Halogen acids
  • C01B7/01—Chlorine; Hydrogen chloride
  • C01B7/03—Preparation from chlorides
  • C01B7/04—Preparation of chlorine from hydrogen chloride
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
  • B01J2208/00008—Controlling the process
  • B01J2208/00017—Controlling the temperature
  • B01J2208/00106—Controlling the temperature by indirect heat exchange
  • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
  • B01J2208/00132—Tubes
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
  • B01J2208/00008—Controlling the process
  • B01J2208/00017—Controlling the temperature
  • B01J2208/00106—Controlling the temperature by indirect heat exchange
  • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
  • B01J2208/0015—Plates; Cylinders
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
  • B01J2208/00008—Controlling the process
  • B01J2208/00017—Controlling the temperature
  • B01J2208/00477—Controlling the temperature by thermal insulation means
  • B01J2208/00495—Controlling the temperature by thermal insulation means using insulating materials or refractories
• • 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
  • B01J2219/02—Apparatus characterised by their chemically-resistant properties
  • B01J2219/025—Apparatus characterised by their chemically-resistant properties characterised by the construction materials of the reactor vessel proper
  • B01J2219/0277—Metal based
  • B01J2219/0286—Steel

Definitions

• the invention relates to a reactor for producing chlorine from hydrogen chloride by gas phase oxidation with oxygen in the presence of a heterogeneous catalyst in a fluidized bed.
• the invention further relates to a process for the production of chlorine using the reactor.
• the oxidation of hydrogen chloride to chlorine is an equilibrium reaction.
• the position of the equilibrium shifts with increasing temperature to the disadvantage of the desired end product.
• Such catalysts are in particular catalysts based on copper or on the basis of ruthenium, for example the supported catalysts described in DE-A 197 48 299 with the active composition ruthenium oxide or ruthenium mixed oxide, the content of ruthenium oxide being 0.1 to 20% by weight. % and the average particle diameter of ruthenium oxide is 1.0 to 10.0 nm.
• ruthenium chloride catalysts which contain at least one of the compounds titanium oxide and zirconium oxide, ruthenium nium carbonyl complexes, ruthenium salts of inorganic acids, ruthenium nitrosyl complexes, ruthenium amine complexes, ruthenium complexes of organic amines or ruthenium acetylacetonate complexes.
• gold can also be present in the active catalyst composition.
• EP-A 0 331 465 discloses a fluidized bed reactor in which perforated plates are accommodated in the fluidized bed at a uniform distance. The agglomerated gas bubbles disintegrate as they flow through the perforated plates. This leads to an improved mixing of the gas with the solid.
• a chromium oxide is used as a catalyst in EP-A 0 331 465.
• ruthenium-based catalysts are temperature sensitive. Volatile ruthenium compounds are formed even at temperatures above 400 ° C. To avoid loss of active mass, it is therefore necessary to run the process for producing chlorine from hydrogen chloride in the presence of ruthenium-based catalysts as isothermally as possible at temperatures below 400 ° C.
• the object of the invention is therefore to provide a reactor for the production of chlorine from hydrogen chloride by gas phase oxidation with oxygen, which allows good mixing of the gas and solid phases and operates largely isothermally.
• the object is achieved by a reactor for the production of chlorine from hydrogen chloride by gas phase oxidation with oxygen in the presence of a heterogeneous catalyst in a fluidized bed, a heat exchanger and gas-permeable plates being accommodated in the fluidized bed.
• the gas-permeable plates are thermally connected to the heat exchanger.
• the heat transfer area in the fluidized bed is increased, since the gas-permeable plates act as ribs, which absorb the heat and conduct it to the heat exchanger. For this it is necessary that the thermal conductivity of the gas-permeable plates is greater than the thermal conductivity in the fluidized bed.
• the heat-conducting connection of the gas-permeable plates to the heat exchanger can be positive, frictional or materially. Positive connections are to
• Frictional connections are, for example, screw connections, clamp seats, press fits or connections with resilient intermediate links.
• the integral connections include
• Material connections are preferred because they ensure the best heat transfer from the gas-permeable plates to the heat exchanger.
• An isothermal fluidized bed is preferably obtained by providing the largest possible heat transfer area.
• Suitable heat exchangers are, for example, tube bundle heat exchangers with tubes arranged horizontally or vertically in the fluidized bed or plates arranged vertically in the fluidized bed in which a heat transfer medium flows.
• the heat exchanger tubes or heat exchanger plates are preferably arranged within the fluidized bed in such a way that the fluidization of the fluidized bed is not disturbed by the installation of the heat exchanger.
• these are preferably connected to one another by the gas-permeable plates, the gas-permeable plates preferably being arranged perpendicular to the heat exchanger plates.
• the individual heat exchanger tubes arranged vertically in the fluidized bed are connected to one another by horizontally extending tubes.
• the gas-permeable plates are then preferably on the horizontal tubes.
• the horizontally running tubes can also be integrated in the gas-permeable plates.
• the horizontal pipes enclose the surfaces that are sealed with the gas-permeable plates.
• the heat transfer medium must be selected so that it is chemically and thermally stable at the temperatures occurring in the heat exchanger. Suitable heat transfer media are, for example, salt melts or, preferably, liquids that evaporate at the reaction temperature in the range of up to 400 ° C. Water at a pressure of 10 to 60 bar is particularly preferred as the heat transfer medium.
• the advantage of evaporating liquids as a heat transfer medium is that during the evaporation of the heat transfer medium gers whose temperature does not change. In this way, isothermal conditions can be created in the heat exchanger.
• Nickel alloys are preferably used when condensation of hydrochloric acid cannot be excluded. For example, water condenses at a pressure of 25 bar at a temperature of around 224 ° C. With the appearance of liquid water, hydrogen chloride dissolves in it to form hydrochloric acid.
• the gas residence time in the reactor is optimized by specifically influencing the movement of bubbles and solids.
• the gas-permeable plates are used in particular to tear agglomerated gas bubbles apart and thus to ensure that smaller gas bubbles are evenly distributed in the fluidized bed granulate.
• Perforated sheets or lattice-shaped structures are preferably used as gas-permeable plates.
• the size of the individual openings in the gas-permeable plates is preferably in the range from 1 to 100,000 mm 2 , more preferably in the range from 5 to 10,000 mm 2 , in particular in the
• the gas-permeable plates are designed as ordered or disordered fabric structures.
• Ordered fabric structures are, for example, lattice or net-shaped structures, disordered fabric structures are, for example, knitted fabrics or braids.
• the size of the openings or the structure of the gas-permeable plates is designed so that bubble coalescence is avoided. Contrary to the general knowledge known to the person skilled in the art that disturbances in the movement of solids caused by built-in components lead to losses in the heat transfer performance in the fluidized bed, it is found that avoiding bubble coalescence, which leads to smaller gas bubbles in the fluidized bed, improves the heat transport within the fluidized bed that this outweighs the losses caused by the internals and so the heat transport in the fluidized bed is better overall. Due to the smaller gas bubbles, the fluidized bed is mixed better, which leads to an even temperature distribution. The heat transfer within the fluidized bed is not hindered by large gas bubbles that have an insulating effect. This also leads to an improved heat transport to the heat exchanger and thus to an improved ren heat dissipation from the fluidized bed. For this reason, the heat exchanger can be made smaller, which leads to material and thus cost savings.
• the gas-permeable plates are preferably at a distance of 5 to 200 cm, more preferably from 10 cm to 100 cm and particularly preferably from 20 to 50 cm.
• the gas-permeable plates are preferably made of steel or nickel alloys.
• nickel alloys are used when condensation of hydrochloric acid cannot be ruled out.
• the fluidized bed is preferably delimited from the environment by a reactor wall.
• the reactor wall is preferably gas-tight and thermally insulated from the environment. In this way, for example, it is avoided that gases involved in the reaction can escape to the environment via the reactor wall.
• the thermal insulation of the reactor wall prevents the reaction temperature from falling in the edge region of the fluidized bed. This ensures that the reaction takes place evenly over the entire area of the fluidized bed.
• the insulation of the reactor wall also reduces the safety effort, since there are no hot surfaces outside the reactor which can cause burns when touched.
• the reactor wall is preferably cylindrical, but can also have any other cross section.
• the wall thickness of the reactor wall is preferably dimensioned such that thermal stresses over the circumference and the height of the reactor wall are avoided. At the same time, the mechanical stability of the reactor wall must be guaranteed.
• the reactor wall is preferably made of steel or nickel energies. Furthermore, the reactor wall can be lined with nickel or nickel alloys. Nickel alloys are used in particular when condensation of hydrochloric acid in the reactor cannot be ruled out.
• the feed gases hydrogen chloride and oxygen are preferably supplied via a wind box arranged below the fluidized bed.
• a gas stream containing hydrogen chloride and a gas stream containing oxygen can be fed separately to the wind box and mixed in the wind box. This is preferably done However, the mixture is already in front of the wind box, so that a gas stream containing hydrogen chloride and oxygen is supplied.
• the gas supply to the wind box can take place on the underside of the wind box, laterally or tangentially. If the gas supply is tangential, a vortex forms inside the windbox. When the gas is supplied from below, the supply is preferably centric.
• the wind box can take any form known to those skilled in the art. When using a fluidized bed reactor with a circular cross section, the wind box is preferably round-arched, conical or cylindrical.
• wind box All metal connections are suitable as material for the windbox, in which a by-product formation can be excluded and the mechanical stability is guaranteed.
• the wind box can also be made from ceramic materials.
• the educt gas stream is fed centrally into the wind box from below.
• the windbox is round-arched and designed so that sudden cross-sectional enlargements are avoided. Avoiding edges inside the windbox prevents turbulence, which can lead to erosion on the inside of the windbox.
• a baffle device is arranged in the wind box against which the inflowing gas flows.
• the deflection of the gas flow forced by the impact device leads to a dissipation of the momentum of the inflowing feed gas.
• the impact device is preferably designed as a simple plate, in the form of a funnel or with a round arch.
• the baffle plate is preferably made of steel or nickel alloys. Nickel alloys are used when condensation of hydrochloric acid cannot be ruled out.
• a gas distributor is connected to the windbox, via which the gas flow is conducted into the fluidized bed.
• the gas distributor is preferably designed so that a uniform gas distribution over the cross section is ensured.
• Suitable gas distributors are, for example, perforated bases or gas distribution nozzles distributed in a base.
• the gas distributor is preferably the boundary between the wind box and the fluidized bed.
• the gas can also be fed directly to the fluidized bed without using a wind box.
• the gas distributor is preferably designed as a pipeline system, via which the gas flows into the fluidized bed.
• the catalytic hydrogen chloride oxidation is preferably isothermal or approximately isothermal in the fluidized bed at reactor temperatures of 180 to 500 ° C., preferably 200 to 450 ° C., particularly preferably 300 to 400 ° C. and a pressure of 1 to 25 bar, preferably 1.2 up to 20 bar, particularly preferably 1.5 to 17 bar and in particular 2.0 to 15 bar.
• all known catalysts for the oxidation of hydrogen chloride to chlorine can be used for the process according to the invention, for example the catalysts based on ruthenium described at the outset and known from DE-A 197 48 299 or DE-A 197 34 412. Also suitable are the catalysts based on gold described in DE-A 102 44 996, containing 0.001 to 30% by weight of gold, 0 to 3% by weight of one or more alkaline earth metals, 0 to 3% by weight on a support.
• one or more alkali metals 0 to 10% by weight of one or more rare earth metals and 0 to 10% by weight of one or more further metals, selected from the group consisting of ruthenium, palladium, osmium, iridium, silver, Copper and rhenium, each based on the total weight of the catalyst.
• the granulate used to form the fluidized bed contains the heterogeneous catalyst.
• the individual grains of the fluidized bed granules preferably form the catalyst supports which are impregnated with active composition.
• Suitable carrier materials are, for example, silicon dioxide, graphite, titanium dioxide with a rutile or anatase structure, zirconium dioxide, aluminum oxide or mixtures thereof, preferably titanium dioxide, zirconium dioxide, aluminum oxide or mixtures thereof, particularly preferably ⁇ - or ⁇ -aluminum oxide or mixtures thereof.
• the supported copper or ruthenium catalysts can be obtained, for example, by impregnating the support material with aqueous solutions of CuCl 2 or RuCl 3 and optionally a promoter for doping, preferably in the form of their chlorides.
• the catalyst can be shaped after or preferably before the support material is impregnated.
• Suitable promoters for the doping are alkali metals such as lithium, sodium, potassium, rubidium and cesium, preferably lithium, sodium and potassium, particularly preferably potassium, alkaline earth metals such as magnesium, calcium, strontium and barium, preferably magnesium and calcium, particularly preferably magnesium, rare earth metals such as Scandium, yttrium, lanthanum, cerium, brasiodymium and neodymium, preferably scanium, yttrium, lanthanum and cerium, particularly preferably lanthanum and cerium, or mixtures thereof.
• the granules can then be dried at temperatures of 100 to 400 ° C., preferably 100 to 300 ° C., for example under a nitrogen, argon or air atmosphere and optionally calcined.
• the granules are preferably first dried at 100 to 150 ° C. and then calcined at 200 to 400 ° C.
• granules of inert material may also be present in the fluidized bed.
• titanium dioxide, zirconium dioxide or mixtures thereof, aluminum oxide, steatite, ceramic, glass, graphite or stainless steel can be used as the inert material.
• the granules of inert material preferably have similar external dimensions to the granules impregnated with active material.
• the solids separators are preferably arranged at a height which is above the discharge height of the granules which are thrown upwards when the gas bubbles emerge from the fluidized bed. The required separation performance of the solid separators is thus minimized by the appropriate distance between the fluidized bed and the solid separators.
• Cyclones or filter cartridges are suitable as solid separators.
• This area is expanded conically to reduce the empty pipe gas velocity in the separation zone.
• the necessary separation performance of the solid matter separator can be reduced further.
• Metallic compounds are preferably used as the material for the separation zone and the at least one solid separator, in which a by-product formation can be excluded and which ensure the necessary mechanical stability.
• Particularly preferred materials for solid matter separators and separation zones are steel or nickel alloys. Suitable nickel alloys are, for example, Hasteloy materials or Inconell. These are used when condensation of hydrochloric acid cannot be ruled out.
• ceramic materials can be used in addition to the suitable metal compounds.
• FIG. 1 shows a section through a fluidized bed reactor designed according to the invention
• FIG. 2 shows a section along the line AA in FIG. 1,
• FIG. 3 shows a section along the line BB in FIG. 1,
• FIG. 4 shows detail C from FIG. 1,
• FIG. 5 shows a section along the line DD in Figure 1.
• Figure 1 shows a section through a fluidized bed reactor designed according to the invention in a schematic representation.
• a reactor 1 comprises a fluidized bed 2, a wind box 3, a gas distributor 4, a separation zone 5 and at least one solid separator 6.
• the feed gases are fed to the wind box 3.
• the gas supply is marked with arrow 7 here.
• the gas supply to the wind box 3 can take place from below or from the side, as shown here.
• the hydrogen chloride-containing gas stream and the oxygen-containing gas stream can be mixed upstream of the wind box 3 or can be fed separately to the wind box 3. If the feed is separated, the mixture then takes place in the wind box 3. From the wind box 3, the gas flows via the gas distributor 4 into the fluidized bed 2.
• the task of the gas distributor 4 is that the gas flows evenly into the fluidized bed 2 flows in and so a good mixing of gas and solid in the fluidized bed 2 is achieved.
• the gas distributor 4 can be a perforated floor or a floor with gas distribution nozzles distributed therein.
• a heat transfer medium is fed to the heat exchanger 9 via at least one heat transfer fluid inlet 10.
• the heat carrier flows through at least one heat carrier inlet pipe 18 into at least one heat carrier distributor 11.
• the heat carrier inlet 10 is located in the upper region of the fluidized bed 2.
• the heat carrier inlet 10 can also be arranged at any other height of the fluidized bed 2 ,
• the angle at which the transverse tubes 16 are inclined with respect to the horizontal is preferably ⁇ 10 °, more preferably ⁇ 5 ° and particularly preferably ⁇ 2 °.
• the heat exchanger tubes 15 open into at least one steam collector 13. If the heat exchanger 9 comprises a plurality of steam collectors 13, these are preferably connected to a steam exhaust 14. The vaporized heat transfer medium is withdrawn from the heat exchanger 9 via the steam outlet 14. The heat transfer medium is then preferably fed to a further heat exchanger, in which it condenses again, so that again To be able to supply heat exchanger 9 in liquid form. In this way, a closed heat transfer circuit can be implemented.
• gas-permeable plates 17 are accommodated in the fluidized bed transversely to the direction of flow of the gas.
• the gas-permeable plates 17 are thermally connected to the heat exchanger tubes 15.
• the connection is preferably made cohesively by welding.
• the gas-permeable plates 17 are integrally connected to the cross tubes 16, for example by welding.
• the gas-permeable plates 17 are preferably designed as a perforated plate or as an ordered or disordered fabric structure.
• the separation zone 5 adjoins the fluidized bed 2.
• the cross section of the separation zone 5 increases in the direction of flow of the gas.
• the separation zone 5 describes the area in which the fluidized bed granulate separates from the gas.
• at least one solid separator 6 is preferably arranged in the upper region of the separation zone 5.
• the at least one solid separator 6 can also be arranged outside the reactor 1.
• the arrow 8 indicates the product removal following the at least one solid matter separator 6.
• FIG. 2 shows a section in plan view along the line AA in FIG. 1.
• the reactor 1 is delimited by a reactor wall 21 with a circular cross section.
• the reactor wall 21 is preferably insulated so that only a small heat flow is dissipated via the reactor wall 21. At the same time, this serves for operational safety, since it prevents the outside of the reactor wall 21 from becoming too warm and thus can cause burns when touched.
• the heat generated during the reaction is dissipated via the heat exchanger 9.
• the temperature control medium is supplied in the direction of arrows 19 via the temperature control medium inlets 10.
• the temperature control medium flows via the temperature control medium supply pipes 18 shown in FIG. 3 to the temperature control medium distributors 11.
• the temperature control medium flows in the direction of the steam collectors 13 shown in FIG. 2
• the vaporized temperature control medium is collected in the steam collectors 13 and the steam outlet 14 fed.
• the vaporous temperature control medium is withdrawn from the heat exchanger 9 from the steam outlet 14. This is indicated by the arrow with the reference number 22.
• gas-permeable plates 17 are shown in FIGS. 2 and 3.
• FIG 4 shows the detail marked C in Figure 1.
• the vertically extending heat exchanger tubes 15 are preferably connected to one another at regular intervals by the cross tubes 16.
• the distances preferably correspond to the distances in which the gas-permeable plates 17 are arranged.
• the cross tubes 16 are preferably integrally connected to the heat exchanger tubes 15. However, the connection can also be non-positively, for example by means of pipe clamps or any other pipe connections known to the person skilled in the art.
• the gas-permeable plates 17 are preferably connected to the cross tubes 16 in a heat-conducting manner.
• the gas-permeable plates 17 can be arranged above the cross tubes 16, as shown here, but an arrangement is also conceivable in which the gas-permeable plates 17 are arranged below the cross tubes 16 or the gas-permeable plates 17 are traversed by the cross tubes 16.
• the heat transfer medium preferably flows from the vertically running heat exchanger tubes 15 into the cross tubes 16.
• the cross tubes 16 are preferably arranged at a slight inclination.
• FIG. 5 shows a section along the line DD in FIG. 1.
• FIG. 5 shows that the heat carrier inlet pipes 18 are not connected to the heat exchanger pipes 15 via cross pipes 16. This ensures that no evaporated heat transfer medium can flow into the heat transfer supply pipes 18. This also ensures that the entire heat transfer medium reaches the heat exchanger tubes 15 via the heat transfer distributor 11. In this way, a uniform temperature distribution and heat carrier distribution in the heat exchanger 9 is achieved.
• all heat exchanger tubes 15 are connected to one another by the cross tubes 16.
• a gas-permeable plate 17 of grid-shaped design can also be seen in the embodiment shown here.

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• Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Engineering & Computer Science (AREA)
• Combustion & Propulsion (AREA)
• Inorganic Chemistry (AREA)
• Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
• Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)

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• 2004
  • 2004-02-11 DE DE102004006610A patent/DE102004006610A1/de not_active Withdrawn
• 2005
  • 2005-02-08 EP EP05701378A patent/EP1715946A1/de not_active Withdrawn
  • 2005-02-08 JP JP2006552524A patent/JP2007522071A/ja active Pending
  • 2005-02-08 US US10/588,511 patent/US7736598B2/en not_active Expired - Fee Related
  • 2005-02-08 WO PCT/EP2005/001249 patent/WO2005077520A1/de active Application Filing
  • 2005-02-08 CN CNB2005800046767A patent/CN100509134C/zh not_active Expired - Fee Related

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