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
  • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J19/24—Stationary reactors without moving elements inside
  • B01J19/2475—Membrane 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
  • B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
• • 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
  • B01D53/22—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 diffusion
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
  • B01D71/02—Inorganic material
  • B01D71/024—Oxides
  • B01D71/0271—Perovskites
• • 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
  • B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
  • B01J12/007—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous 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
  • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
• • 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
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
  • B01J8/009—Membranes, e.g. feeding or removing reactants or products to or from the catalyst bed through a membrane
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
  • B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
  • B01J8/025—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical in a cylindrical shaped bed
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • 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
  • B01J8/0278—Feeding reactive fluids
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
  • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
  • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
  • B01J8/065—Feeding reactive fluids
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
  • C01B13/02—Preparation of oxygen
  • C01B13/0229—Purification or separation processes
  • C01B13/0248—Physical processing only
  • C01B13/0251—Physical processing only by making use of membranes
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen; Reversible storage of hydrogen
  • C01B3/02—Production of hydrogen; Production of gaseous mixtures containing hydrogen
  • C01B3/32—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air
  • C01B3/34—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air by reaction of hydrocarbons with gasifying agents
  • C01B3/38—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air by reaction of hydrocarbons with gasifying agents using catalysts
  • C01B3/386—Catalytic partial combustion
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
  • C01B2203/02—Processes for making hydrogen or synthesis gas
  • C01B2203/025—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]
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B2210/00—Purification or separation of specific gases
  • C01B2210/0043—Impurity removed
  • C01B2210/0046—Nitrogen
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P20/00—Technologies relating to chemical industry
  • Y02P20/50—Improvements relating to the production of bulk chemicals
  • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

• the invention is directed to an oxidation reactor and a method for use of this reactor, in which a plurality of gas-tight oxygen-conducting membrane elements are arranged, whose outer surfaces are arranged on the side of a catalyst-fillable reaction space, and which can be flowed through with an oxygen-containing gas Membrane elements represent the spatial connection of the distributor space and a collecting space and / or an outlet of the reactor.
• the reactor is characterized in that by means of one or more spacer elements, a defined minimum distance between the outer surface of a membrane element and the catalyst of the reaction space is ensured.
• Synthesis gas ie gas mixtures with the main constituents CO and H 2 (and, if appropriate, further components such as, for example, CO 2 , H 2 , N 2 and inert constituents, depending on the preparation and purification steps), is attributed to the current state of the art
• the endothermic steam reforming of hydrocarbons eg methane
• derived compounds according to
• the oxygen required for the partial oxidation can originate, for example, from a cryogenic air separation plant.
• the transport of oxygen takes place in ionic form, d. H.
• the result is a theoretical selectivity of a dense membrane with respect to oxygen of infinity.
• a separation of the oxygen from the remaining air components such as nitrogen is thus made possible, for example when using air as the oxygen-supplying medium.
• a reactor which is subdivided by a mixed-conducting membrane into two spaces or regions.
• oxygen-supplying gas or gas mixture on one side of the membrane or membrane module submitted oxygen-supplying gas or gas mixture, while on the opposite side of the membrane, which is hereinafter referred to as outer surface or permeate side, a medium to be oxidized is introduced.
• Oxygen-supplying gases are often water vapor, CO 2 or preferably air.
• oxygen permeates through the membrane from the higher oxygen partial pressure side and reacts with the oxidizable medium located on the opposite side.
• the oxidizable medium is preferably a hydrocarbon such as methane or natural gas with a high methane content, to which water vapor is typically added to prevent possible coking.
• the oxygen partial pressure of the permeate side is below the oxygen partial pressure of the feed side, so that oxygen continues to permeate. Therefore, for example, air with a more or less arbitrary pressure can be used on the feed side, while at the same time there is a significantly increased pressure on the permeate side.
• the lower limit for the pressure on the feed side is that the oxygen partial pressure of the feed side must be above the oxygen partial pressure of the permeate side.
• a suitable catalyst is typically used in the reaction space of the reactor. Examples of this can be found, for example, in EP 0 999 180 A2, EP 1 035 072 A1, US Pat. No. 6,077,323 or US Pat. No. 6,695,983.
• oxygen permeates from the feed side through the membrane and is reacted on the opposite permeate side.
• the driving force for this permeation is the oxygen partial pressure difference between the two sides of the membrane. Since this is constantly maintained by the Abretician of the oxygen, in the case of syngas production with air on the feed side and a hydrocarbon / water vapor mixture on the permeate side, the air at ambient pressure or only slightly elevated pressure can be used.
• the mixed conducting materials are ceramic materials which have the ability to conduct oxygen ions due to an oxygen defect structure under suitable operating conditions.
• Suitable operating conditions are a sufficiently high temperature of typically above 600 0 C and a Sauerstoffpartial horrdifferenz on the ceramic material.
• Such materials may, for example, belong to the group of perovskite (ABO 3 ) or perovskite turned out to have structures derived from fluorite structures (AO 2 ), Aurivillius structures ([Bi 2 O 2 ] [A n .-, B n O x ]) or brownmillerite structures (A 2 B 2 O 5 ).
• composite materials of ion-conducting and electron-conducting materials are also conceivable are composite materials of ion-conducting and electron-conducting materials.
• Typical examples of systems listed in the literature as oxygen-conducting materials or classes of materials are La 1 -X (Ca, Sr, Ba) x Co 1 . y Fe y 0 3 . ⁇ , Ba (Sr) COv x Fe x O 3-8 , Sr (Ba) Ti (Zr) 1. ⁇ , Co y Fe x O 3 . ⁇ , Lai. ⁇ Sr x Gai. y FeyO 3 s, La 015 Sr 015 MnO 3 -S, LaFe (Ni) O 3 . ⁇ , La 019 Sr 0 ,! FeO 3 . ⁇ or ö . (A. Thursfield, IS Metcalfe, J. Mat. Sci., 2004, 14, 275-2485)
• multiphase composite materials can be used.
• Materials that can be used for a technical application are those which have the highest possible oxygen permeance. Typical values are on the order of> 0.1 Nm 3 / (m 2 h) oxygen.
• the materials used as mixed-conducting membranes are generally oxidic ceramics, which tend below a dependent of the constituents of the membrane oxygen partial pressure for the reduction and thus destruction of the crystal structure.
• the frequently occurring in such materials CoO at a temperature of 900 0 C and said oxygen partial pressure of less than 10 '16 bar is reduced to elemental Co. This theoretical estimate can also be confirmed experimentally, as shown in the comparative example.
• Fig. 1 shows the results of the comparative example.
• the relative intensity over diffraction angle (theta) is plotted for the six selected residence times of the membrane.
• the new peaks of relative intensity with longer maturities compared to the Oh curve indicate, inter alia, to the formation of elemental Co and various independent oxide phases.
• the peaks of the perovskite phase crucial for oxygen permeation disappear. It is obvious that even at residence times of only 50 h, a significant degradation of the crystal structure occurs, which is associated with a loss of the proper functionality of the membrane, that leads to a local decomposition.
• the object of the prior art is thus to develop an oxidation reactor with an oxygen-conducting membrane, wherein the membrane has a high reduction stability and high mechanical stability.
• the present invention solves this problem by an oxidation reactor, which comprises a supply line for an oxygen-containing gas, which leads into a distributor space or a distributor element. Furthermore, the oxidation reactor comprises a supply line for a raw or fully oxidized raw gas, which leads into a reaction space, wherein in the reaction space a plurality of gas-tight oxygen-conducting membrane elements are arranged.
• the membrane elements have an inlet and an outlet surface relative to the transport of oxygen, wherein the outlet surface is defined as an outer surface, which is arranged on the side of the reaction space.
• the membrane elements provide the spatial connection of distributor space and a collecting space and / or an outlet During operation of the reactor, the oxygen-containing gas can flow through the reactor in the following order: inlet, distributor space, membrane element, collecting space and / or outlet, wherein the reaction space can be filled with catalyst.
• a defined minimum distance between the outer surface of a membrane element and / or a composite of membrane elements ensures the fillable catalyst.
• the composite may be a bundle or group of parallel or interwoven or twisted membrane elements.
• the spacer elements of the reactor according to the invention are inert molded bodies which encase the membrane elements individually or as a bundle or group or are upstream of the reaction space.
• the moldings may be present as a bed and / or be formed as a single element, such as a jacket tube.
• the inert material in this case has a pore volume or a perforation which is smaller than the fine grain content of the fillable catalyst.
• the spacer elements may be formed in one further embodiment of one or more inert materials, which adhere directly to the outer membrane surface. Spacers of such a shape would prevent the catalyst from direct contact with the oxygen-conducting membrane by a suitable pore structure, which is smaller than the fines content of a catalyst bed.
• spacer elements are catalytically active moldings, which are oxidized in those areas during normal operation of the reactor and thereby rendered inert, which are arranged opposite the outlet surface of the membrane and / or touching.
• the shaping of the spacer elements in the oxidation reactor according to the invention is either regular or has an irregular structure.
• the spacer elements can be further improved by having one or more catalytically active surfaces.
• the spacer elements are shaped such that the surfaces facing the reaction space are coated with catalytically active material or formed from catalytically active material.
• the invention also encompasses an oxidation reactor which essentially corresponds to the abovementioned one, but in which a defined minimum distance between the outer surface and the outer surface is defined by means of the shaping of the catalyst in the reaction space. berlithography a membrane element or a group or a combination of membrane elements and the catalyst is ensured.
• the catalyst is shaped in the form of strands or flat elements.
• An improvement of said oxidation reactor is to fix the catalyst in a plate at least on one side by means of an adhesive or sintering. In general, you will align the membrane and the catalyst in such a construction in parallel and ensure in this way a defined minimum distance.
• the membrane elements of the two aforementioned oxidation reactors are formed from one or more of the materials selected from the group of perovskites (ABO 3 ), perovskite-related structures, fluorite structures (AO 2 ), Aurivillius structures ([Bi 2 O 2 ] [A ⁇ 1 B n O x ]) or the Brownmillerit Scheme (A 2 B 2 O 5 ) come.
• Particularly suitable for the O 2 transport and thus the use in the oxidation reactor according to the invention are membrane elements formed from one or more of the materials which can be described by the following general structural formulas: Ba (Sr) Co 1-X Fe x O 3-5 , Sr (Ba) Ti (Zr) 1-X .
• the membrane elements in this case have an oxygen permeance at 950 0 C and a Sauerstoffpartial horrdifferenz of> 0.1 bar between the located on both sides of the membrane free gas phases on average equal to or greater than 0.1 Nn ⁇ 7 (m 2 h).
• the invention further comprises a process for the oxidation of substances, in which an oxidation reactor according to one of the preceding embodiments is used, the reaction space is filled with a catalyst and
• Oxygen or an oxygen-containing gas is passed via the inlet into the distributor space of the oxidation reactor,
• the temperature in the reaction chamber between 200 - 1200 0 C, preferably 500 - 1000 0 C and ideally 700 - 900 ° C and further
• the pressure between 1 - 200 bar, preferably 10 - 70 bar and ideally 30 to 60 bar.
• gas to be oxidized is preferably methane or natural gas with a high methane content, which may also contain non-oxidizable constituents.
• the invention also includes the use of the abovementioned oxidation process in one of the embodiments for the production of synthesis gas with the main components H 2 and CO. Also encompassed by the invention is the use of the oxidation process according to the invention for the oxidative dehydrogenation of alkanes, the oxidative methane coupling, the partial oxidation of higher hydrocarbons and / or hydrocarbon derivatives or the selective oxidation of individual constituents of gas mixtures.
• a hollow-fiber shaped membrane 1, hereinafter also called a membrane module, of the abovementioned material was installed in a reaction space 2, the membrane 1 being approximately 1.5 cm long fragments of a porous Al 2 O 3 tube 3 with a diameter of 3 mm was surrounded.
• a nickel catalyst 4 shown as a dotted area was applied on the outside of this Al 2 O 3 tube 3.
• the nickel catalyst 4 is a common oxidation catalyst for steam reforming or for the oxidation of methane.
• the membrane 1 was traversed on the inside of the hollow fiber with air 5 at a pressure of 1 bar, while in the reaction chamber 2 outside the membrane 1 with methane 6 was introduced under a pressure of 1 bar.
• the oxygen depleted output stream 7 and the product stream 8 are discharged.
• the individual gas streams are added separately or removed from the oxidation reactor, without any mixing of the streams.
• the entire reactor was operated at 85O 0 C continuously for several hundred hours.
• oxygen permeates from the air side through the membrane and was converted on the permeate side with methane to synthesis gas.
• An exemplary diagram for the composition of the product gas is shown in FIG. 3. It is obvious that the composition of the synthesis gas phase given in this experiment corresponds approximately to the composition of the comparative example.
• the reason for this unexpected stability could be the formation of an oxygen protective layer over the membrane in the described reactor system. It is believed that due to the porous membrane disposed around the membrane AI 2 0 3 , an increased mass transport resistance of the oxygen is built up from the permeate side membrane surface to the catalyst. Thus, a local maximum of the oxygen concentration forms directly on the permeate side surface of the membrane, thereby protecting it from destruction.
• the extent of oxygen mass transport inhibition on the permeate side can thus be adjusted so that a local oxygen protection layer of the desired intensity is formed over the membrane surface.
• Crucial here is the targeted removal of oxygen from the permeate side of the membrane, so that the subsequent conversion of the oxygen is braked on the catalyst.
• reactive media such as methane or Hydrogen
• it is not crucial to transport masses of reactive media, such as methane or Hydrogen, towards the membrane, since the protection of the membrane does not result from a low concentration of the reactive component at the permeate side surface of the membrane. The protection results rather from the fact that a sufficiently slow removal of the oxygen is coupled with a simultaneously sufficiently high oxygen permeation through the membrane. As a consequence, a significant amount of free oxygen is locally present at the permeate-side membrane surface.
• the membrane 1 which is formed as a bundle of hollow membrane fibers, by a gas-permeable tube 3 comprises. Outside the tubes 3, a catalyst bed 9 is arranged, which is indicated by the dotted area. The ends of the individual hollow membrane fibers are guided in the tube 3 by connecting elements 10 and fixed in this. These connecting elements 10 serve simultaneously for
• the individual bundles of the membrane 1 enveloping gas-permeable tubes 3 are in turn fixed at both ends in tube sheets 11.
• the bundles of the membrane modules 1 protrude with the one opening side into the distributor chamber 12 and with the other in the collecting chamber 13 of the oxidation reactor.
• These connecting elements 10 may be, for example drilled steel plates, in which the individual membrane modules are glued.
• the bundle of membrane fibers can, as indicated in FIG. 5, be arranged as a multiplicity of parallel individual fibers or else be present in the form of interconnected fiber bundles according to DE 10 2005 005 464.1.
• the oxygen-providing stream 5 flows through the fibers and releases some or all of its contained oxygen through the membrane into the fiber space. Subsequently, the oxygen depleted residual stream 7 leaves the fiber bundle.
• the catalyst bed 9 is flowed through by the stream 6 to be oxidized, the latter being reacted by reaction with the oxygen permeated through the membrane 1 and optionally further reactions to the product stream 8.
• the invention is not limited to the above constructive examples.
• the examples described do not represent a limitation of the invention, as the skilled person a number of ways are known to produce a targeted mass transfer resistance between two parts of a reactor and / or by selecting the operating conditions.
• the reactor according to the invention and the process can also be used for further oxidation reactions in which oxygen-transporting membranes can be usefully used.
• oxygen-transporting membranes can be usefully used. Examples of such applications are the oxidative dehydrogenation of alkanes, the oxidative methane coupling, the partial oxidation of higher hydrocarbons and / or hydrocarbon derivatives or the selective oxidation of individual constituents of gas mixtures.

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• Chemical & Material Sciences (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Organic Chemistry (AREA)
• Engineering & Computer Science (AREA)
• Inorganic Chemistry (AREA)
• Combustion & Propulsion (AREA)
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• General Health & Medical Sciences (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• General Chemical & Material Sciences (AREA)
• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
• Separation Using Semi-Permeable Membranes (AREA)
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• 2005
  • 2005-12-14 DE DE102005060171A patent/DE102005060171A1/de not_active Withdrawn
• 2006
  • 2006-12-05 WO PCT/EP2006/011629 patent/WO2007068369A1/de not_active Ceased
  • 2006-12-05 US US12/097,020 patent/US20090018373A1/en not_active Abandoned
  • 2006-12-05 EA EA200870037A patent/EA200870037A1/ru unknown
  • 2006-12-05 JP JP2008544812A patent/JP5366556B2/ja not_active Expired - Fee Related
  • 2006-12-05 KR KR1020087016552A patent/KR101376082B1/ko not_active Expired - Fee Related
  • 2006-12-05 CA CA002634263A patent/CA2634263A1/en not_active Abandoned
  • 2006-12-05 DK DK06829277.0T patent/DK1968738T3/da active
  • 2006-12-05 CN CN2006800528590A patent/CN101394924B/zh not_active Expired - Fee Related
  • 2006-12-05 EP EP06829277A patent/EP1968738B1/de not_active Not-in-force
  • 2006-12-05 ES ES06829277T patent/ES2397966T3/es active Active
• 2008
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  • 2008-06-11 ZA ZA200805086A patent/ZA200805086B/xx unknown

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