WO2004091771A1 - Mikroreaktor in plattenbauweise mit einem katalysator - Google Patents
Mikroreaktor in plattenbauweise mit einem katalysator Download PDFInfo
- Publication number
- WO2004091771A1 WO2004091771A1 PCT/EP2004/003377 EP2004003377W WO2004091771A1 WO 2004091771 A1 WO2004091771 A1 WO 2004091771A1 EP 2004003377 W EP2004003377 W EP 2004003377W WO 2004091771 A1 WO2004091771 A1 WO 2004091771A1
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- WIPO (PCT)
- Prior art keywords
- reaction
- spaces
- heat transport
- rooms
- ideally
- Prior art date
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Classifications
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- 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
- B01J19/0093—Microreactors, e.g. miniaturised or microfabricated reactors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
- B01F25/30—Injector mixers
- B01F25/31—Injector mixers in conduits or tubes through which the main component flows
- B01F25/314—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced at the circumference of the conduit
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F33/00—Other mixers; Mixing plants; Combinations of mixers
- B01F33/30—Micromixers
-
- 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
- B01J19/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
-
- 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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
- B01F2025/91—Direction of flow or arrangement of feed and discharge openings
- B01F2025/918—Counter current flow, i.e. flows moving in opposite direction and colliding
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- 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
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00783—Laminate assemblies, i.e. the reactor comprising a stack of plates
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- 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
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00819—Materials of construction
- B01J2219/00835—Comprising catalytically active material
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- 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
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00851—Additional features
- B01J2219/00858—Aspects relating to the size of the reactor
- B01J2219/0086—Dimensions of the flow channels
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- 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
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00889—Mixing
Definitions
- the invention relates to a microreactor with catalytic wall preparation for carrying out heterogeneously catalyzed gas phase reactions on an industrial scale.
- the reactor is constructed in layers analogous to a plate heat exchanger, the spaces thus created and stabilized and segmented by spacer elements representing reaction spaces and heat transport spaces.
- the layer structure is dimensioned in such a way that there are optimal conditions for flow, heat and mass transfer, reaction kinetics, process safety and statics for large-scale use for tonnage production.
- DE 39 26 466 describes a microreactor for carrying out chemical two-substance reactions, the use of which is named for reactions with strong exothermicity and which is also suitable for heterogeneous catalytic reactions.
- Longitudinal grooves are arranged in the layers, through which the reaction partner flows after essentially two media have been brought together, while a cooling medium flows alternately in a subsequent layer.
- This cooling which runs transversely to the reaction grooves, takes place according to DE 39 26 466 at the end of the longitudinal grooves over the layer wall or over the entire layer length.
- wall thicknesses of less than 1000 / -m are specified, which prohibits the use of this reactor for more aggressive reactions under high pressures.
- catalyst materials that do not come from the group of the catalytically active metals mentioned and that cannot be used as base material are still frequently used.
- DE 196 54361 describes a stacked-type reactor which is used for chemical-catalytic processes, the catalyst being applied as a layer on the inner walls of the reaction channels. Layers are arranged alternately to the layers containing the reaction channels, in which layers a heat transport medium is conducted analogously to the abovementioned documents, with layers of the same type being in fluidic connection.
- DE 196 54361 discloses a very simple variant of the flow guidance within the reactor, in that the reaction fluid arriving from the previous layer is distributed to the subsequent reaction layer or the discharge channel via a transverse slot.
- EP 0 903 174 discloses a microreactor for liquid-phase reactions of organic compounds using peroxides as an oxidizing agent, which solves the problem of safe temperature control via an alternating and batch-wise sequence of reaction and cooling layers, the microchannels of the adjacent layer always being are at right angles to each other and a maximum residual wall thickness between the reaction channel and the adjacent cooling layer of 1000 ⁇ m and a maximum hydraulic diameter of the reaction channels of likewise 1000 ⁇ m is shown.
- the central challenge of the peroxidic reactions mentioned in this document is explosion protection. Leak tightness of the system and ensuring optimal mixing of the reactants used are therefore fundamental in order to avoid areas with explosive peroxide concentrations. However, apart from the dimensioning of the channel cross sections, no teaching can be found in EP 0 903 174. Explosion protection is only considered in the cited document from the point of view of the safe observance of the required temperature and concentrations.
- a device and a method are known in which at least two fluid media react with one another, with a free-flowing or wall-adhering catalyst optionally also being present.
- the reaction takes place in the reactor described in flat-gap reaction spaces. Cavities or bores are provided in the plates forming these reaction spaces, through which the heat transport medium is passed.
- the basic idea of this reactor disclosed in DE 10042 746 is a parallel and planar flow through the reaction space without further internals, with individual spacers in the edge area ensuring the gap between two plates. Microdimensions in the range from 50 to 5000 ⁇ m are only set in one dimension, namely in the gap width. Another key feature is the inherent safety of this reactor since the small free diameter prevents flame spread.
- the rooms are formed by stacked plates or layers, one part of the rooms representing reaction rooms in which the chemical-catalytic reaction takes place and the other part of the rooms representing heat transport rooms for the passage of a cooling or heating medium, the heat transport between reaction and heat transport spaces is carried out by at least one common room wall or directly adjacent panels. Spacers are arranged in all rooms in order to guide the force transmission of an external contact pressure through the stack of plates and to prevent the microchannels from being closed by deforming the free range. This deformation is the result of a differential pressure between the reaction and heat transport space.
- catalyst material is at least partially applied to the inner walls of the reactor rooms.
- the free flow cross section in the microstructures of this construction after the application of the catalyst must have a hydraulic diameter of less than 4000 ⁇ m and a ratio of slot width to slot height of less than 800.
- the catalyst coating of the interior spaces can also be extended to the collection or distribution space, it also being possible for a catalyst which is different from the one in the reaction slots to be attached to the wall surfaces in these areas.
- the shape of the spacer elements is not restricted in any meadow and can be rotationally symmetrical, drop-shaped, rhomboid-shaped or advantageously designed as webs and ideally as continuous webs.
- the decisive factor is a sufficient load-bearing ratio, which is a function of the material properties of the base material, the process temperature and the differential pressure between adjacent rooms and the resulting contact pressure to be applied from the outside.
- the main advantage of designing the spacer elements as continuous webs is the influence on the flow behavior in the rectangular reaction slots formed in this way, the additionally generated adhesive surface for the catalyst material and production-related aspects.
- reference surfaces are only to be understood as those surfaces of the plates which lie within the peripheral seals and sealing the reaction spaces or heat transfer spaces, as well as sealing weld seams or sealing solder seams.
- the plate material arranged outside the seals is largely designed as a solid material and is of no importance for the aforementioned consideration of the wings.
- the top surfaces of the spacer elements With a high pressure difference between the process rooms and the heat transport spaces, the top surfaces of the spacer elements thus enable a sufficient load-bearing ratio for the force transmission of a contact pressure applied via the two end plates or terminal anchors or anchor plates. If the spacer elements are designed as webs, the smallest web width is 1000 m. A web width over 6000 ⁇ m is usually no longer interesting economically and in terms of production technology.
- the invention further encompasses that at least parts of the plate or the web material have a catalytic effect.
- metallic materials such as precious metals, manganese, molybdenum, iron, chromium, nickel and others are used.
- the main flow directions of the adjacent reaction and heat transport spaces can be arranged in such a way that the flow is co-current, counter-current or meandering in relation to the closest space.
- the heat transport also takes place in direct connection with each reaction chamber. If there is a metallic base material and if the slot and plate geometries have been optimized in accordance with the above-mentioned information, the heat transport is primarily limited by the layer thickness of the catalyst material.
- the webs of two plates are directed towards each other and these webs form an angle to one another of 0 ° to 90 °.
- these webs are arranged parallel and directly one above the other. If the webs are not arranged in parallel, a strong mixing and swirling effect is achieved.
- At least one area is provided in the entrance and within the reaction spaces, in which at least two fluids are mixed, at least one gaseous or liquid fluid being injected onto which there is a homogenization section can connect.
- a device of any design is arranged in front of or along this homogenization path, which reduces the free cross-sectional area perpendicular to the main flow direction. This reduction in the cross-sectional area creates an increase in the flow velocities and thus a strong mixing of the fluids.
- the areas with a reduced free flow cross-section represent a mechanical flame barrier with a corresponding design. This flame barrier or quench effect thus prevents ignition processes from passing over from the reaction zone, which primarily occur in the area of the reaction slots with catalyst coating. is localized to other process units, as well as the flame entry into the reaction zone, starting from the distributor or collection unit.
- the invention further includes that at least one device is provided in the flow direction at the end of the reaction spaces, which reduces the free cross-sectional area perpendicular to the main flow direction, the device having any shape and advantageously as a plurality of spacer elements, as extensions of the web widths or is designed as panels and ideally as a reduction in the gap height.
- This reduction in cross-section at the end of the reaction spaces serves to even out the flow and, analogous to the aforementioned design of the entrance area with a suitable microstructuring, represents a mechanical flame barrier and thus prevents ignition from the catalyst into the adjacent and generally macrostructured reactor or process units.
- no catalyst material may be arranged in the area of the stowage zone, since an ignition originating from the catalytic converter can otherwise hit the collection unit even with existing mechanical flame retardancy.
- the equalization of the flow is very advantageous because, for example, bumps in the catalyst layer generate different pressure differences either in areas of the reaction spaces or individual slots, so that there would be an uneven flow, which leads to corresponding disadvantages in the product quality, as it is is known from the prior art. It was shown that the pressure loss due to the narrowing of the cross-section at the outlet of the plates must be at least 5 times greater than the fluctuation in the pressure difference which results from the manufacturing tolerances of the catalyst layer. Ideally, the pressure drop across the storage zone should be 10 times higher than the aforementioned pressure drop due to fluctuations.
- methods for using the aforementioned reactor are furthermore disclosed, which are carried out at differential pressures in the range from 0 bar to 15 bar, the ideal area of use depending on the base material chosen being between 0 bar and 5 bar.
- the possible process temperatures range from low temperatures below 0 ° C to temperatures of around 500 ° C. Liquid or gaseous media can be passed through for heat transport in the heat transport rooms.
- a special embodiment of the invention provides that the media in the heat transport spaces completely or partially change the state of the aggregate during conduction or condensation.
- the invention thus encompasses processes such as, for example, the synthesis of propylene oxide from essentially propene and hydrogen peroxide or phenol from essentially aromatic hydrocarbons, and further synthesis of hydrocarbon compounds and in particular of oxygenates from hydrocarbon compounds.
- the reactor is also suitable for the synthesis of hydrogen peroxide from hydrogen and oxygen.
- FIG. 1 shows a single reactor plate in top view and the position of the detail view
- FIG. 5 in the entrance area of the plate and the position of the detail view
- FIG. 7 at the outlet of the plate and the sealing and guide bar arrangement
- FIG. 2 analogously to FIG. 1, a plan view of a single reactor plate, which does not have an integrated distributor unit, but instead is flowed across the entire width on the narrow plate side; ;
- Figure 3 is a single heat transfer plate in plan view and a variant of the sealing arrangement and the guide bars.
- FIG. 4 shows, as a sectional drawing, an example of a stacking sequence of reactor and heat transport spaces
- FIG. 5 shows a detailed view of the entrance area of the slots and the device for injecting fluids and the homogenization section in two design variants;
- Fig. 6 shows the location of the dimensions used
- Fig. 8 possible arrangements in a reaction space.
- FIG. 1 shows a reactor plate forming a reaction chamber, on which an incoming starting material can be fed via the central feed line 2 into the distributor unit 6 of the reaction chamber 8.
- Guide bars 9 are arranged in the distributor unit, which distributes this educt evenly over the slots coated with catalyst material, which are formed between the spacer elements 11, shown here as bars.
- the slots are arranged in parallel and specify the main flow direction 14. Shown at the end of the slots in the collecting unit 7, in which a product stream is taken and is fed there to the central discharge line 4 by means of further guide webs 9.
- 1 also shows the central feed line 24 for a second feed stream, which feeds channels 24a lying in the base plate 1 transversely to the main flow direction 14 and which are connected to the bores 25 shown in FIG. 5.
- reaction spaces 8 heat transport spaces 10 and their inflows and outflows are sealed off by irreversible connections and / or seals 26.
- the plate of a heat transport space shown in FIG. 3 is constructed in a similar manner, the webs 11 in the embodiment shown running parallel and congruently with the webs of the reaction space. The catalyst coating and the feed line for further fluids are not provided here.
- FIG. 2 shows a reactor plate which does not have an integrated distributor space in the reaction space, but instead is flowed through by a central reactant stream together with the other reactor plates, not shown here.
- reaction space 4 shows, as a sectional drawing, an example of a stacking sequence of reactor and heat transport spaces, the main direction of flow leading perpendicularly out of or into the plane of the drawing.
- Slits coated on one side with catalyst material 12 can be seen in the reaction space a), the subsequent heat transport space being designed identically.
- the maximum possible flow cross section of the reaction slots is compared to the slots of the adjacent heat transport space reduced by the cross-sectional area of the catalyst layer.
- reaction space b slits can be seen which are provided with catalyst on both plate surfaces. This is followed by heat transfer rooms which contain a different number of slots.
- both plate walls are coated with catalyst, one plate surface being provided with grooves in which the catalyst material 12 (see also FIG. 6 c)) is introduced.
- the maximum possible flow cross section therefore only decreases by the cross-sectional area of a catalyst layer.
- 5 shows in three variants the inflow area of individual reaction slots, the educt stream coming from the distributor unit flowing into the mixing zone 30, where a second and third fluid is admixed to the educt stream via the inlet 24a and the bores 25.
- the bores 25 are at right angles as shown in a) or are inclined at an angle ⁇ (FIG. 5 b)) with or against the main flow direction.
- a homogenization zone 31 is arranged in which turbulent conditions are created by means of internals 29 and turbulent conditions are achieved and optimal mixing is achieved.
- 5 b) shows two design variants of possible internals.
- the internals 29 b) already reduce the free flow cross section in the area of the mixing zone 30, so that microstructures are formed and thus form a more extensive mechanical flame barrier than is the case with the internals 29 a).
- Fig. 6 shows the location of the dimensions used and the length specifications used in this document. It can be seen that the free flow cross-section of a slot results from the gap width 16 times the web height 17 minus the cross-sectional area before the applied catalyst material 12, the catalyst cross-sectional area usually representing the product of the layer thickness and gap width 16. Exceptions are, for example, the variants shown in FIG. 6 c), in which the web flanks are also coated with catalyst material or the catalyst material is introduced in a groove or groove (see FIG. 6 c)).
- the decisive factor for the strength considerations is the effective plate height 22, which is in the area of the smallest plate thickness and in example c) is in the area of the groove. In examples a) and b) of FIG. 6, it is the plate height 21.
- Fig. 7 shows a detailed view of the outlet zone of the reaction slots in three design variants and embodiments of the spacer elements. It's in that Embodiment a) shown in Fig. 7 enlargements of the web widths 18, which represent stagnation zones 32.
- the slots are formed by a kind of colonnade, in which rotationally symmetrical spacer elements are arranged in alleys and catalyst material, depicted as a dotted surface, is applied in the alleys.
- the congestion effect is achieved via oval spacer elements or screens 29, which are arranged in the main flow of the slots.
- the spacer elements are arranged in any distribution in space, the storage zone 32 being formed by a closer arrangement of spacer elements.
- the catalyst material is applied to the entire surface of the plate and also extends to the area behind the barrage.
Abstract
Description
Claims
Priority Applications (13)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
NZ542958A NZ542958A (en) | 2003-04-16 | 2004-03-31 | Microreactor composed of plates and comprising a catalyst |
EP04724561.8A EP1613424B1 (de) | 2003-04-16 | 2004-03-31 | Mikroreaktor in plattenbauweise mit einem katalysator |
US10/553,312 US7678361B2 (en) | 2003-04-16 | 2004-03-31 | Microreactor composed of plates and comprising a catalyst |
MXPA05011217A MXPA05011217A (es) | 2003-04-16 | 2004-03-31 | Microrreactor compuesto de placas y que comprende un catalizador. |
AU2004229150A AU2004229150B2 (en) | 2003-04-16 | 2004-03-31 | Microreactor composed of plates and comprising a catalyst |
JP2006504923A JP2006523522A (ja) | 2003-04-16 | 2004-03-31 | 触媒を備えたプレート構造のマイクロ型反応器 |
EA200501619A EA009346B1 (ru) | 2003-04-16 | 2004-03-31 | Пластинчатый микрореактор с катализатором |
BRPI0409581-2A BRPI0409581A (pt) | 2003-04-16 | 2004-03-31 | microrreator composto de placas e compreendendo um catalisador |
CA002522339A CA2522339A1 (en) | 2003-04-16 | 2004-03-31 | Reactor for heterrogeneous catalytic reactions |
KR1020057019637A KR101055118B1 (ko) | 2003-04-16 | 2004-03-31 | 플레이트 및 촉매를 포함하여 구성되는 마이크로리액터 |
IL171380A IL171380A (en) | 2003-04-16 | 2005-10-11 | Microreactor composed of plates and comprising a catalyst and process for its use |
NO20055394A NO20055394L (no) | 2003-04-16 | 2005-11-15 | Plateminereaktor med en katalysator |
HK06113982.7A HK1093173A1 (en) | 2003-04-16 | 2006-12-20 | Microreactor composed of plates and comprising a catalyst as well as the application method thereof |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10317451A DE10317451A1 (de) | 2003-04-16 | 2003-04-16 | Reaktor für heterogen katalysierte Reaktionen |
DE10317451.6 | 2003-04-16 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2004091771A1 true WO2004091771A1 (de) | 2004-10-28 |
Family
ID=33185666
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2004/003377 WO2004091771A1 (de) | 2003-04-16 | 2004-03-31 | Mikroreaktor in plattenbauweise mit einem katalysator |
Country Status (17)
Country | Link |
---|---|
US (1) | US7678361B2 (de) |
EP (1) | EP1613424B1 (de) |
JP (1) | JP2006523522A (de) |
KR (1) | KR101055118B1 (de) |
CN (1) | CN100400152C (de) |
AU (1) | AU2004229150B2 (de) |
BR (1) | BRPI0409581A (de) |
CA (1) | CA2522339A1 (de) |
DE (1) | DE10317451A1 (de) |
EA (1) | EA009346B1 (de) |
HK (1) | HK1093173A1 (de) |
IL (1) | IL171380A (de) |
MX (1) | MXPA05011217A (de) |
NO (1) | NO20055394L (de) |
NZ (1) | NZ542958A (de) |
WO (1) | WO2004091771A1 (de) |
ZA (1) | ZA200508366B (de) |
Cited By (33)
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WO2005075349A1 (en) * | 2004-01-27 | 2005-08-18 | Velocys Inc. | Process for producing hydrogen peroxide using microchannel technology |
WO2005105665A2 (en) * | 2004-04-27 | 2005-11-10 | Velocys, Inc. | Hydrogen peroxide production in microchannel reactors |
WO2006020709A1 (en) * | 2004-08-12 | 2006-02-23 | Velocys Inc. | Process for converting ethylene to ethylene oxide using microchannel process technology |
WO2006042598A1 (de) * | 2004-10-15 | 2006-04-27 | Uhde Gmbh | Verfahren zur herstellung von olefinoxiden und peroxiden, reaktor und dessen verwendung |
AT503116B1 (de) * | 2006-03-17 | 2007-08-15 | Dbs Daily Business Support Sof | Mikroreaktor |
JP2007230908A (ja) * | 2006-03-01 | 2007-09-13 | Arakawa Chem Ind Co Ltd | エポキシ化合物の製造方法 |
WO2007112866A1 (de) * | 2006-04-01 | 2007-10-11 | Cognis Ip Management Gmbh | Verfahren zur herstellung von alkylenoxiden |
JP2008529953A (ja) * | 2005-04-01 | 2008-08-07 | エルジー・ケム・リミテッド | 水素生産装置及びそれを用いた水素生産方法 |
FR2918584A1 (fr) * | 2007-07-10 | 2009-01-16 | Centre Nat Rech Scient | Microreacteur catalytique integre. |
JP2009529549A (ja) * | 2006-03-14 | 2009-08-20 | バイエル・テクノロジー・サービシーズ・ゲゼルシャフト・ミット・ベシュレンクテル・ハフツング | 不均一系触媒による水素化を利用する芳香族アミンの製造方法及び装置 |
WO2010009021A2 (en) * | 2008-07-14 | 2010-01-21 | Velocys Inc. | Process for making ethylene oxide using microchannel process technology |
US7816411B2 (en) | 2004-10-01 | 2010-10-19 | Velocys, Inc. | Multiphase mixing process using microchannel process technology |
US7935734B2 (en) | 2005-07-08 | 2011-05-03 | Anna Lee Tonkovich | Catalytic reaction process using microchannel technology |
US8100996B2 (en) | 2008-04-09 | 2012-01-24 | Velocys, Inc. | Process for upgrading a carbonaceous material using microchannel process technology |
US8383872B2 (en) | 2004-11-16 | 2013-02-26 | Velocys, Inc. | Multiphase reaction process using microchannel technology |
EP2500086A3 (de) * | 2011-03-18 | 2013-05-08 | Kabushiki Kaisha Kobe Seiko Sho (Kobe Steel, Ltd.) | Strömungskanalstruktur und Mischverfahren, Extraktionsverfahren und Reaktionsverfahren für Flüssigkeiten |
US8524927B2 (en) | 2009-07-13 | 2013-09-03 | Velocys, Inc. | Process for making ethylene oxide using microchannel process technology |
US8632729B2 (en) | 2008-10-15 | 2014-01-21 | National Institute of Advanced Industrial Scienec and Technology | Fixed bed mixed gas/liquid phase reactor and mixed gas/liquid phase reaction process using the same |
EP2719447A1 (de) * | 2012-10-11 | 2014-04-16 | Scambia Holdings Cyprus Limited | Kombinierte Wärmetausch- und Flüssigkeitsmischvorrichtung |
US8747656B2 (en) | 2008-10-10 | 2014-06-10 | Velocys, Inc. | Process and apparatus employing microchannel process technology |
US8933254B2 (en) | 2008-07-14 | 2015-01-13 | Basf Se | Process for making ethylene oxide |
US9101890B2 (en) | 2005-05-25 | 2015-08-11 | Velocys, Inc. | Support for use in microchannel processing |
US9150494B2 (en) | 2004-11-12 | 2015-10-06 | Velocys, Inc. | Process using microchannel technology for conducting alkylation or acylation reaction |
WO2015069762A3 (en) * | 2013-11-06 | 2015-10-15 | Watt Fuel Cell Corp. | Chemical reactor with manifold for management of a flow of gaseous reaction medium thereto |
WO2015195051A1 (en) * | 2014-06-20 | 2015-12-23 | National University Of Singapore | Triphasic flow millireactors |
US9627699B2 (en) | 2013-11-06 | 2017-04-18 | Watt Fuel Cell Corp. | Gaseous fuel CPOX reformers and methods of CPOX reforming |
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Also Published As
Publication number | Publication date |
---|---|
IL171380A (en) | 2012-05-31 |
JP2006523522A (ja) | 2006-10-19 |
AU2004229150A1 (en) | 2004-10-28 |
NO20055394L (no) | 2005-11-15 |
KR101055118B1 (ko) | 2011-08-08 |
CA2522339A1 (en) | 2004-10-28 |
CN100400152C (zh) | 2008-07-09 |
KR20060012586A (ko) | 2006-02-08 |
HK1093173A1 (en) | 2007-02-23 |
US7678361B2 (en) | 2010-03-16 |
DE10317451A1 (de) | 2004-11-18 |
ZA200508366B (en) | 2007-02-28 |
MXPA05011217A (es) | 2006-03-30 |
NZ542958A (en) | 2010-03-26 |
CN1791461A (zh) | 2006-06-21 |
EA009346B1 (ru) | 2007-12-28 |
AU2004229150B2 (en) | 2009-10-08 |
EP1613424A1 (de) | 2006-01-11 |
EA200501619A1 (ru) | 2006-04-28 |
BRPI0409581A (pt) | 2006-04-18 |
US20070053808A1 (en) | 2007-03-08 |
EP1613424B1 (de) | 2018-09-26 |
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