EP0859660A1 - Procede et dispositif pour effectuer des reactions chimiques au moyen d'un melangeur microlaminaire - Google Patents

Procede et dispositif pour effectuer des reactions chimiques au moyen d'un melangeur microlaminaire

Info

Publication number
EP0859660A1
EP0859660A1 EP96934817A EP96934817A EP0859660A1 EP 0859660 A1 EP0859660 A1 EP 0859660A1 EP 96934817 A EP96934817 A EP 96934817A EP 96934817 A EP96934817 A EP 96934817A EP 0859660 A1 EP0859660 A1 EP 0859660A1
Authority
EP
European Patent Office
Prior art keywords
mixing
fluid
mixer
channels
micro
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP96934817A
Other languages
German (de)
English (en)
Inventor
Klaus Schubert
Wilhelm Bier
Gerd Linder
Erhard Herrmann
Bernd Koglin
Thomas Menzel
Christine Maul
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Bayer AG
Forschungszentrum Karlsruhe GmbH
Original Assignee
Bayer AG
Forschungszentrum Karlsruhe GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Bayer AG, Forschungszentrum Karlsruhe GmbH filed Critical Bayer AG
Publication of EP0859660A1 publication Critical patent/EP0859660A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • B01F25/20—Jet mixers, i.e. mixers using high-speed fluid streams
    • B01F25/23—Mixing by intersecting jets
    • 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
    • B01F25/40—Static mixers
    • B01F25/42—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions
    • B01F25/43—Mixing tubes, e.g. wherein the material is moved in a radial or partly reversed direction
    • B01F25/432—Mixing tubes, e.g. wherein the material is moved in a radial or partly reversed direction with means for dividing the material flow into separate sub-flows and for repositioning and recombining these sub-flows; Cross-mixing, e.g. conducting the outer layer of the material nearer to the axis of the tube or vice-versa
    • B01F25/4323—Mixing tubes, e.g. wherein the material is moved in a radial or partly reversed direction with means for dividing the material flow into separate sub-flows and for repositioning and recombining these sub-flows; Cross-mixing, e.g. conducting the outer layer of the material nearer to the axis of the tube or vice-versa using elements provided with a plurality of channels or using a plurality of tubes which can either be placed between common spaces or collectors
    • 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
    • B01F33/301—Micromixers using specific means for arranging the streams to be mixed, e.g. channel geometries or dispositions
    • B01F33/3012—Interdigital streams, e.g. lamellae
    • 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
    • B01F33/301—Micromixers using specific means for arranging the streams to be mixed, e.g. channel geometries or dispositions
    • B01F33/3017—Mixing chamber
    • 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
    • B01F33/304—Micromixers the mixing being performed in a mixing chamber where the products are brought into contact
    • 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
    • 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
    • B01J19/18—Stationary reactors having 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
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2415—Tubular 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
    • B01J2219/00085—Plates; Jackets; 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00164—Controlling or regulating processes controlling the flow
    • 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
    • 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
    • B01J2219/00873—Heat exchange
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F2260/00—Heat exchangers or heat exchange elements having special size, e.g. microstructures
    • F28F2260/02—Heat exchangers or heat exchange elements having special size, e.g. microstructures having microchannels
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S366/00—Agitating
    • Y10S366/03—Micromixers: variable geometry from the pathway influences mixing/agitation of non-laminar fluid flow
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T137/00—Fluid handling
    • Y10T137/2496—Self-proportioning or correlating systems
    • Y10T137/2514—Self-proportioning flow systems
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T137/00—Fluid handling
    • Y10T137/2496—Self-proportioning or correlating systems
    • Y10T137/2514—Self-proportioning flow systems
    • Y10T137/2516—Interconnected flow displacement elements
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T137/00—Fluid handling
    • Y10T137/2496—Self-proportioning or correlating systems
    • Y10T137/2559—Self-controlled branched flow systems
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T137/00—Fluid handling
    • Y10T137/2496—Self-proportioning or correlating systems
    • Y10T137/2559—Self-controlled branched flow systems
    • Y10T137/2562—Dividing and recombining
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T137/00—Fluid handling
    • Y10T137/2496—Self-proportioning or correlating systems
    • Y10T137/2559—Self-controlled branched flow systems
    • Y10T137/2564—Plural inflows

Definitions

  • the reactants must be fed continuously to a chemical reactor and brought into intimate contact with the aid of a mixing device (mixer), i.e. be mixed well.
  • a mixing device i.e. be mixed well.
  • a simple reactor is e.g. a container with a stirrer as a mixing element.
  • main and secondary reactions take place in the reactor when the reactants come into contact.
  • the aim of the process engineer is to conduct the reactions and thus also the mixing in such a way that the highest possible yield of the desired product is selectively achieved.
  • the quality of the mixing and the influence of the mixing organ on the yield of the desired product largely depends on the ratio of the
  • Reaction kinetics given chemical reaction speed to the mixing speed If the chemical reactions are slow reactions, the chemical reaction is generally much slower than the mixing. The gross reaction rate and the yield of desired. Product is then determined by the slowest step, namely the kinetics of the chemical reactions taking place, and by the global mixing behavior (residence time distribution, macromixing) of the chemical reactor used. If the chemical reaction rates and the mixing rate are of the same order of magnitude, there are complex interactions between the kinetics of the reactions and the local mixing behavior determined by the turbulence in the reactor used and on the mixing element (micromixing). If it happens that the chemical reaction rates are significantly faster than the mixing rate, the gross rates of the reactions taking place and the yields are essentially determined by the mixing, i.e. by the local, time-dependent velocity and concentration field of the reactants, i.e. determines the turbulence structure in the reactor or on the mixing element [1].
  • Continuous driving style used a number of mixing elements.
  • dynamic mixers such as stirrers, turbines or Rotor-stator systems
  • static mixers such as Kenics mixers, Schasch ⁇ lik mixers or SMV mixers
  • jet mixers such as nozzle mixers or T mixers [2-4].
  • Nozzle mixers are preferably used for the rapid mixing of the starting materials in the case of rapid reactions with undesirable secondary or secondary reactions.
  • one of the two starting components is sprayed into the other component at high flow velocity (see FIG. 1).
  • the kinetic energy of the injected jet (B) is essentially dissipated behind the nozzle, i.e. through turbulent decay of the beam into eddies and further turbulent decay of the eddies into ever smaller eddies converted into heat.
  • the vertebrae each contain the starting components that are present next to each other in the fluid bales (macro mixture). At the beginning of the turbulent vortex decay, a slight mixture due to diffusion occurs at the edges of these initially larger structures. The complete one
  • the object of the invention is to provide a method and a device in which the mixing takes place quickly and the formation of secondary or by-products is suppressed or reduced. It must be achieved that the educts are homogeneously mixed with one another, so that no local and no temporal over-concentrations of the educts occur in the shortest possible time. In the case of fluids which react chemically with one another, a complete reaction of the fluids is to be achieved. If required, the heat of reaction should also be able to be removed or supplied effectively and as quickly as possible.
  • Laminar flow conditions for the starting materials A, B are preferably maintained in the micro-slot channels. However, nothing stands in the way of working with turbulent flows in the micro-slot channels, if necessary.
  • the geometry of the microstructure lamella mixer is advantageously designed in such a way that the thickness of the fluid lamellae d at the inlet into the mixing /
  • Reaction space can be set to a value between 10 microns and 1000 microns, preferably between 10 microns and 100 microns.
  • a thickness d is preferably set which is of the order of magnitude of the concentration micrometer, so that after exiting the microstructure mixer, without another Vertebral decay is necessary, the micromixing of the components can be done quickly by diffusion.
  • the width b of the fluid lamellae or of the micro-slot channels, via which the lamellae exit the microstructure lamella mixer, should be as large as possible in order to keep the pressure loss in the mixer as low as possible by reducing the wall area per educt volume.
  • the width b can vary from values in the range of the order of 0.5 mm to large values in the range of several centimeters and is essentially only limited by the mechanical stability of the component.
  • the lowest possible thickness d of the fluid lamella is decisive for the mixing speed and thus the quality of the mixture, but not the width b.
  • a further development of the method according to the invention is that in addition to a fluid lamella of a starting material, a fluid lamella of a tempered inert fluid, e.g. for heating or cooling purposes, is fed into the mixing / reaction space.
  • the process according to the invention is therefore based on the fact that the feed streams A, B are first convectively divided into thin lamellae with a thickness d by means of the micro-structure lamella mixer, which then mix with one another after diffusion and / or turbulence in the mixing / reaction space.
  • the task of the microstructure lamella mixer is to convectively divide the feed streams and to produce fine fluid lamellae with a characteristic thickness d without the starting components coming into contact with one another within the mixer device.
  • the same geometrical dimensioning (same cross-section and same length) for the micro-slot channels each assigned to an educt ensures that the fluid lamellae emerge from all channels assigned to each educt at the same flow rates.
  • the flow velocities in the microslit channels are mutually the same for one educt.
  • the flow velocities of the two educts (in relation to each other) can be quite different.
  • the device according to the invention makes it possible to substantially save the time for the turbulent vortex decay during mixing and thereby to speed up the mixing process considerably.
  • undesirable by-products or secondary products occur to a much lesser extent than in the case of mixers according to the prior art.
  • a main application is therefore quick reactions, which have characteristic reaction times ⁇ 10 s and in particular ⁇ 1 s.
  • “Reaction time” is usually understood to mean the half-life, ie the time after the start of the reaction after which the starting material concentration has dropped to half the value.
  • a static microstructure lamella mixer with at least one mixing chamber and an upstream guide component for the supply of mixed or reaction fluids (educts) has proven to be a device.
  • the guide component is composed of a plurality of plate-like, layered elements which are crossed by microchannels running obliquely to the longitudinal axis of the micromixer, the channels of adjacent elements crossing without contact and opening into the mixing chamber. According to the invention, this device is characterized by the following features:
  • the plate-like elements consist of thin foils, in each of which a single or a group of closely adjacent slit-shaped micro-slot channels running with an alternating slope to the longitudinal axis of the micro-mixer is incorporated, so that when the foils are layered one on top of the other, a series of closed channels for the guidance the fluids to be mixed (starting materials A, B) are formed.
  • the micro-slot channels have a depth d ⁇ 1000 ⁇ m, preferably ⁇ 100 ⁇ m, with wall thicknesses of the intermediate webs and channel floors of ⁇ 1000 ⁇ m, preferably ⁇ 100 ⁇ m and a width that is at least 10 times, preferably 20 times the depth d is.
  • microslit channels of adjacent foils diverge towards the fluid inlet side of the micromixer in such a way that the fluids to be mixed (starting materials A, B) can be fed in separately.
  • pins or webs can be attached perpendicular to the channel floors, which are firmly connected to the channel floors and support them against each other.
  • an intermediate film is connected between each two films with the oblique micro-slot channels diverging to the fluid inlet side, which has micro-slot channels running perpendicular to the longitudinal axis of the micro-mixer and is used to pass a coolant or heating medium.
  • a micro-heat exchanger is connected to the mixing chamber.
  • the mixing chamber itself can also be designed as a micro heat exchanger which is connected directly to the guide component.
  • the fluids to be mixed are subdivided in rows and "on a gap" into thin, adjacent fluid lamellae which, when entering the mixing chamber, fill a common, correspondingly narrow volume and can thereby mix in the fastest and shortest way.
  • the formation of extremely thin fluid lamellae allows a few hundred to a thousand lamellae to lie one above the other or next to one another over a height of 1 cm, and these fluid lamellae are alternately fed by educt A or educt B.
  • the device according to the invention enables two or more fluids to be mixed. If chemically reacting fluids (educts) are mixed, the (exothermic reactions) or required (endothermic reactions) heat of reaction can be dissipated or supplied by the connected micro heat exchanger.
  • Channel depth d the contact area between the fluid and the channel wall is minimized. This leads to significantly lower friction pressure losses in the microstructure lamella mixer, in particular in a channel depth d ⁇ 100 ⁇ m, than in a microstructure mixer in which the width b of the micro-slot channels is of the order of the depth d (approximately square cross section).
  • Fig. 2 shows the schematic representation of one another
  • Fig. 3 shows the basic structure of a preferred embodiment of the
  • Micro-structure lamella mixer for two educts A, B with symmetrical flow paths, 4 shows the mixing of the fluid lamellae entering the mixing or reaction space from the IVfil- ⁇ ostx für lamella mixer and assigned to the educts A, B,
  • Fluid lamellae associated with educts A, B when entering the mixing / reaction space are characterized by alternately superimposed or adjacent layers.
  • Fig. 6 is a flow diagram for an apparatus for examining chemical reactions that take place using the device according to the invention
  • FIG. 8a shows two views of a guide component made of foils.
  • 9a and 9b schematically a microstructure lamella mixer with a coolable or heatable guide component
  • Mixing chamber a heat exchanger is connected 10b shows a microstructure lamella mixer with a mixing chamber designed as a heat exchanger.
  • two reactants A, B which react with one another are fed to a smooth jet mixer or smooth jet nozzle reactor according to the prior art.
  • the reactant B is fed into the through the concentric annular space between the
  • Nozzle and educt stream A fed to the reactor wall are injected at a different flow rate. There is intensive mixing (vortex formation) and immediate use of the chemical reaction between the starting materials or reactants A, B.
  • each lamella consisting of fluid A is followed by a lamella made of fluid B.
  • the thickness d of the lamellae is small compared to their width b.
  • the fluids A, B can consist of a gas or a liquid and are referred to below as starting materials A, B.
  • FIG. 3 schematically shows an embodiment of a microstructure lamella mixer or reactor corresponding to the device according to the invention.
  • the construction principle of this mixer / reactor is based on the fact that different layers of the plates with inclined micro-slot channels are stacked vertically one above the other in a sandwich construction.
  • Each plate with the micro-slot channels la is followed by a plate with the micro-slot channels 1b, i.e. two plates arranged directly one above the other in the stack are each provided with a family of micro-slot channels la, lb, the micro-slot channel groups of successive plates forming an angle ⁇ with one another and being arranged symmetrically to the horizontal axis in FIG.
  • the plates have a thickness of 100 ⁇ m, for example.
  • the slot channels have e.g. a depth d of 70 ⁇ m and a width b> 700 ⁇ m
  • micro-slot channels of a family are each identical in terms of flow, ie that the micro-slot channels la all have the same flow resistance.
  • the same condition applies to the flow resistance of the micro-slot channels 1b, but the flow resistances of the two microchannel groups la, lb
  • the same flow resistance can be achieved in that the length and the cross section are the same for all microslit channels la
  • the starting material fed to a distribution chamber 3a, 3b for example a gaseous reactant, is each distributed over the micro-slit channels la, lb.
  • the two reactants are brought together when they enter the mixing chamber.
  • FIG. 4 the mouth cross section of the microstructure lamella mixer is shown in perspective
  • the micro-slot channels la assigned to the starting material A and in the subsequent layer or plate below the micro-slot channels lb of the starting material B flow into the mixing / reaction space. This is followed by another layer or plate with those belonging to starting material A. Micro-slot channels etc.
  • FIG. 4 it is also shown schematically how the fluid streams guided in the micro-slot channels enter the mixing / reaction space as fluid lamellae 6a, 6b and change with increasing distance from the
  • the third educt consists of a tempered inert fluid.
  • Fluid lamellae are then guided in the microstructure lamella mixer in such a way that a fluid lamella of the tempered inert fluid is fed into the mixing / reaction space in the vicinity of a fluid lamella of an educt for heating or cooling purposes.
  • the films 1 and 2 according to FIG. 8a have a thickness of 100 ⁇ m.
  • the type of film 1 is traversed by one or a group of preferably parallel, closely adjacent and slanting to the longitudinal axis 3 of the micro slots which start from the left left relative to this axis 3 and have an acute angle + ⁇ and open in the central region of the front longitudinal side of the film.
  • Fig. 8a shows a version with one micro slot channel per film.
  • the type of film 2 is traversed in the same way by a micro-slot channel 1b; however here the angle between the longitudinal axis of the groove and the longitudinal axis of the mixer is - ⁇ ; i.e.
  • the micro-slot channel lb runs from the right rear to the central area of the front long film side. However, the amount of the angle need not be the same.
  • the micro slot channels la, lb z. B. be incorporated with shape diamonds and preferably have a width b> 700 microns and a depth d of 70 microns.
  • the thickness of the channel bottoms 5a, 5b is 30 ⁇ m.
  • micro-slot channels it may be expedient to support the foils or the channel bases 5a, 5b against one another by vertically arranged, continuous pins 15 or webs with small transverse dimensions which are welded to the channel bases.
  • the micro-slot channels la, lb can be made as wide as desired without impairing the mechanical stability.
  • Fig. 8b and 8c show how for the production of a guide member 6, the film types 1 and 2 alternately stacked, provided with an upper and a lower cover plate 7a, 7b and z. B. by means of diffusion welding a homogeneous, vacuum-tight and pressure-resistant microstructure body.
  • microslit channels la, lb form a common block, for example a square cross section, with a density of a few tens to a few hundred orifices per cm 2 , which adjoin the common mixing chamber 4.
  • FIG. 8c shows the guide component 6 as seen from the inflow side of the fluids A and B.
  • the channels 1a, 1b which run obliquely to the longitudinal axis 3 diverge alternately from the mixing chamber 4 to the fluid inlet side such that the fluids A and B each have an inlet chamber or distributor chamber 3a and 3b can be fed separately to the guide component 6.
  • the fine fluid lamellae 6a, 6b of the fluids A and B are intimately mixed with one another and form a common flow C in the mixing chamber 4 (see also FIG. 4).
  • 9a and 9b show a variant in which intermediate films 8 are connected between two types of film 1 and 2 or between the films and the cover plates 7a, 7b, which have micro-slot channels 9 running perpendicular to the longitudinal axis 3 for the passage of a coolant or heating medium . This allows the mixing time and the reaction rate of fluids A and B to be influenced.
  • FIGS. 10a shows a guide component 6 corresponding to FIGS. 8a to 8d in section with a connected mixing chamber 4.
  • a heat exchanger 10 is connected to this mixing chamber, which, similar to the variant according to FIGS. 9a and 9b, runs from transverse to the flow direction C. Channels l la is drawn through for the removal or supply of the heat of reaction from or to the channels
  • the heat exchanger 12 is connected directly to the guide component 13.
  • the arrangement is made by spacer films 14 so that two superposed channels 13a, 13b for the fluids A, B each open into a common partial mixing chamber 12a of the heat exchanger, these
  • the azo coupling reaction of ⁇ -naphthol with 4-sulfonic acid benzene diazonium salt is used in the literature to assess the mixing behavior of a wide variety of mixer devices [2, 8, 9].
  • This reaction corresponds to a reaction scheme consisting of the desired main reaction and an undesired competing subsequent reaction, in which the product formed via the main reaction reacts with an unreacted starting material to form an undesirable secondary product.
  • the subsequent product can be analyzed in a simple manner with the aid of absorption spectra. The quality of the process is judged by the selectivity of the undesired secondary product S, X s . The more
  • FIG. 6 The investigations for carrying out rapid chemical reactions using a microstructure mixture were carried out in the apparatus shown in FIG. 6. It consists of the reservoir 5 for the starting components A and B, the dosing and control devices 6, filters 7 to protect the microstructure.
  • the microstructure lamella mixer has slot channels with a depth d of 70 ⁇ m and a width b of 4 mm.
  • the Mil ⁇ ostrutor lamella mixer was equipped with a microstructure mixer with rectangular microchannels, the free jets with a width of 100 ⁇ m and a thickness
  • the mixing behavior of the microstructure-lamella mixer is approximately the same as that of the microstructure-mixer, the main advantages of the microstructure-lamella mixer being that the friction pressure loss is at least a factor of 3 smaller and less backmixing due to turbulence at the entry into the mixing / reaction space occurs due to a smaller number of fluid elements.
  • the free jet tube reactor An effective reactor design to suppress loss of selectivity through fast, undesirable secondary reactions Chem.-Ing.-Tech. MS 1708/88, synopsis in Chem.-Ing.-Tech. 60, 1988

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Dispersion Chemistry (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

Selon ce procédé de réaction, au moins deux éduits A et B sont divisés par une série de microcanaux en forme de fentes (1a, 1b) en lamelles fluidiques spatialement distinctes, qui aboutissent dans une chambre de mélange et de réaction commune. Les lamelles fluidiques ont une épaisseur inférieure à 1000 νm, de préférence inférieure à 100 νm, avec un rapport largeur/épaisseur égal ou supérieur à 10. Selon l'invention, les éduits A et B sortent de la chambre de mélange/réaction sous forme de fines lamelles fluidiques (6a, 6b), chaque lamelle fluidique (6a) d'un éduit A pénétrant dans la chambre de mélange/ réaction à proximité immédiate d'une lamelle fluidique (6b) d'un autre éduit B. Les lamelles fluidiques voisines (6a, 6b) se mélangent ensuite par diffusion et/ou turbulence, ce qui accélère notablement le processus de mélange par rapport aux réacteurs conventionnels. Ces réactions chimiques rapides empêchent dans une large mesure la formation de sous-produits ou de produits secondaires indésirables.
EP96934817A 1995-11-06 1996-10-24 Procede et dispositif pour effectuer des reactions chimiques au moyen d'un melangeur microlaminaire Withdrawn EP0859660A1 (fr)

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DE19541266A DE19541266A1 (de) 1995-11-06 1995-11-06 Verfahren und Vorrichtung zur Durchführung chemischer Reaktionen mittels eines Mikrostruktur-Lamellenmischers
DE19541266 1995-11-06
PCT/EP1996/004665 WO1997017130A1 (fr) 1995-11-06 1996-10-24 Procede et dispositif pour effectuer des reactions chimiques au moyen d'un melangeur microlaminaire

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Families Citing this family (80)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6907921B2 (en) 1998-06-18 2005-06-21 3M Innovative Properties Company Microchanneled active fluid heat exchanger
DE19741645A1 (de) * 1997-09-22 1999-03-25 Bayer Ag Verfahren und Vorrichtung zur Oxidation organischer Verbindungen in flüssiger Phase unter Verwendung peroxidischer Oxidationsmittel
DE19800529A1 (de) * 1998-01-09 1999-07-15 Bayer Ag Verfahren zur Phosgenierung von Aminen in der Gasphase unter Einsatz von Mikrostrukturmischern
AU5211900A (en) * 1999-05-10 2000-11-21 Pirelli Cavi E Sistemi S.P.A. Method and induction furnace for drawing large diameter preforms to optical fibres
DE19928123A1 (de) 1999-06-19 2000-12-28 Karlsruhe Forschzent Statischer Mikrovermischer
US7223364B1 (en) 1999-07-07 2007-05-29 3M Innovative Properties Company Detection article having fluid control film
ES2294389T3 (es) † 1999-07-07 2008-04-01 3M Innovative Properties Company Articulo microfluidico.
DE19963594C2 (de) * 1999-12-23 2002-06-27 Mannesmann Ag Vorrichtung in Mikrostrukturtechnik zum Hindurchleiten von Medien sowie Verwendung als Brennstoffzellensystem
US7056477B1 (en) 2000-02-03 2006-06-06 Cellular Process Chemistry, Inc. Modular chemical production system incorporating a microreactor
US7241423B2 (en) * 2000-02-03 2007-07-10 Cellular Process Chemistry, Inc. Enhancing fluid flow in a stacked plate microreactor
US6537506B1 (en) * 2000-02-03 2003-03-25 Cellular Process Chemistry, Inc. Miniaturized reaction apparatus
US7435392B2 (en) * 2000-02-03 2008-10-14 Acclavis, Llc Scalable continuous production system
US7413714B1 (en) 2000-07-16 2008-08-19 Ymc Co. Ltd. Sequential reaction system
DE10036602A1 (de) * 2000-07-27 2002-02-14 Cpc Cellular Process Chemistry Mikroreaktor für Reaktionen zwischen Gasen und Flüssigkeiten
EP1309404A2 (fr) * 2000-08-07 2003-05-14 Nanostream, Inc. Melangeur fluidique pour systeme microfluidique
US6890093B2 (en) * 2000-08-07 2005-05-10 Nanostream, Inc. Multi-stream microfludic mixers
DE10041823C2 (de) * 2000-08-25 2002-12-19 Inst Mikrotechnik Mainz Gmbh Verfahren und statischer Mikrovermischer zum Mischen mindestens zweier Fluide
US7017651B1 (en) * 2000-09-13 2006-03-28 Raytheon Company Method and apparatus for temperature gradient control in an electronic system
EP1321015B1 (fr) 2000-09-29 2004-05-19 Nanostream, Inc. Dispositifs microfluidiques pour transfert thermique
DE10055758A1 (de) 2000-11-07 2002-05-16 Siemens Axiva Gmbh & Co Kg Verfahren zur Herstellung von Aldolen unter Verwendung eines mikrostrukturierten Reaktionssystems
DE10055856C2 (de) * 2000-11-10 2003-04-10 Kundo Systemtechnik Gmbh Vorrichtung zum Herstellen von mit Kohlendioxid versetztem Tafelwasser
JP2002292275A (ja) * 2001-03-29 2002-10-08 Kanagawa Acad Of Sci & Technol マイクロチップパイルアップ型化学反応システム
US20040221920A1 (en) * 2001-05-01 2004-11-11 Ferguson James D Fuel dispensing nozzle construction
JP3694877B2 (ja) * 2001-05-28 2005-09-14 株式会社山武 マイクロ混合器
US6919046B2 (en) * 2001-06-07 2005-07-19 Nanostream, Inc. Microfluidic analytical devices and methods
JP4792664B2 (ja) * 2001-06-15 2011-10-12 コニカミノルタホールディングス株式会社 混合方法、混合機構、該混合機構を備えたマイクロミキサーおよびマイクロチップ
US20030082632A1 (en) * 2001-10-25 2003-05-01 Cytoprint, Inc. Assay method and apparatus
DE10158160A1 (de) * 2001-11-28 2003-06-12 Basf Ag Herstellung von Isocyanaten in der Gasphase
DE10160440A1 (de) * 2001-12-08 2003-07-03 Forschungszentrum Juelich Gmbh Vorrichtung und Verfahren zum Temperieren von Mikroströmen
US6877892B2 (en) * 2002-01-11 2005-04-12 Nanostream, Inc. Multi-stream microfluidic aperture mixers
DE10216947B4 (de) * 2002-04-17 2007-10-04 Ehrfeld Mikrotechnik Bts Gmbh Verfahren zum Homogenisieren von Emulsionen
CA2411220C (fr) * 2002-06-28 2010-11-16 Lubomyr M. Cymbalisty Melangeur fixe a ecoulement hydrodynamique et methode d'utilisation connexe pour separer des sables bitumineux et des matieres de nature semblable
US20040134557A1 (en) * 2002-06-28 2004-07-15 Cymbalisty Lubomyr M. Hydrodynamic static mixing apparatus and method for use thereof in transporting, conditioning and separating oil sands and the like
US7118920B2 (en) 2002-10-22 2006-10-10 Battelle Memorial Institute Multiphasic microchannel reactions
KR100485317B1 (ko) * 2002-10-25 2005-04-27 전자부품연구원 마이크로 혼합기 및 그의 제조방법
DE20218972U1 (de) * 2002-12-07 2003-02-13 Ehrfeld Mikrotechnik Ag Statischer Laminationsmikrovermischer
US7094354B2 (en) * 2002-12-19 2006-08-22 Bayer Healthcare Llc Method and apparatus for separation of particles in a microfluidic device
US7125711B2 (en) * 2002-12-19 2006-10-24 Bayer Healthcare Llc Method and apparatus for splitting of specimens into multiple channels of a microfluidic device
US6946011B2 (en) * 2003-03-18 2005-09-20 The Babcock & Wilcox Company Intermittent mixer with low pressure drop
WO2004092908A2 (fr) * 2003-04-14 2004-10-28 Cellular Process Chemistry, Inc. Systeme et procede de determination de parametres de reaction optimaux au moyen d'un processus continu
DE10318061A1 (de) * 2003-04-17 2004-10-28 Behr Gmbh & Co. Kg Mischvorrichtung
US7294734B2 (en) * 2003-05-02 2007-11-13 Velocys, Inc. Process for converting a hydrocarbon to an oxygenate or a nitrile
US6916113B2 (en) * 2003-05-16 2005-07-12 Agilent Technologies, Inc. Devices and methods for fluid mixing
US7435381B2 (en) * 2003-05-29 2008-10-14 Siemens Healthcare Diagnostics Inc. Packaging of microfluidic devices
JP4407177B2 (ja) 2003-05-30 2010-02-03 富士フイルム株式会社 マイクロリアクターを用いた反応方法
US20040265172A1 (en) * 2003-06-27 2004-12-30 Pugia Michael J. Method and apparatus for entry and storage of specimens into a microfluidic device
US20040265171A1 (en) * 2003-06-27 2004-12-30 Pugia Michael J. Method for uniform application of fluid into a reactive reagent area
US20080257754A1 (en) * 2003-06-27 2008-10-23 Pugia Michael J Method and apparatus for entry of specimens into a microfluidic device
DE10333922B4 (de) 2003-07-25 2005-11-17 Wella Ag Bauteile für statische Mikromischer, daraus aufgebaute Mikromischer und deren Verwendung zum Mischen, zum Dispergieren oder zur Durchführung chemischer Reaktionen
DE10333921B4 (de) 2003-07-25 2005-10-20 Wella Ag Extraktionsverfahren unter Verwendung eines statischen Mikromischers
US7347617B2 (en) * 2003-08-19 2008-03-25 Siemens Healthcare Diagnostics Inc. Mixing in microfluidic devices
US7470408B2 (en) * 2003-12-18 2008-12-30 Velocys In situ mixing in microchannels
JP4547606B2 (ja) * 2004-03-17 2010-09-22 富士フイルム株式会社 マイクロリアクターの複合反応方法及びマイクロリアクター
WO2005103788A1 (fr) * 2004-04-26 2005-11-03 Carl Zeiss Smt Ag Procede pour fixer un element optique a une structure de maintien
WO2006031058A1 (fr) * 2004-09-13 2006-03-23 Spec Co., Ltd Reacteur a microcanaux
DE102004062074A1 (de) * 2004-12-23 2006-07-06 Forschungszentrum Karlsruhe Gmbh Statischer Mikrovermischer
EP1904221A2 (fr) * 2005-04-06 2008-04-02 Stichting voor de Technische Wetenschappen Partie d'admission pour microreacteur
KR100695151B1 (ko) * 2005-05-18 2007-03-14 삼성전자주식회사 교차 채널을 이용한 유체 혼합 장치
US20070298486A1 (en) * 2006-06-16 2007-12-27 Velocys Inc. Microchannel Apparatus and Methods Of Conducting Unit Operations With Disrupted Flow
US20080237044A1 (en) * 2007-03-28 2008-10-02 The Charles Stark Draper Laboratory, Inc. Method and apparatus for concentrating molecules
WO2008130618A1 (fr) 2007-04-19 2008-10-30 The Charles Stark Draper Laboratory, Inc. Procédé et appareil pour séparer des particules, cellules, molécules et matières particulaires
US8206025B2 (en) * 2007-08-07 2012-06-26 International Business Machines Corporation Microfluid mixer, methods of use and methods of manufacture thereof
US7837379B2 (en) * 2007-08-13 2010-11-23 The Charles Stark Draper Laboratory, Inc. Devices for producing a continuously flowing concentration gradient in laminar flow
US8079964B2 (en) 2008-02-25 2011-12-20 Devicor Medical Products, Inc. Method and apparatus for inserting biopsy site marker in marker body
US8068895B2 (en) 2008-02-25 2011-11-29 Devicor Medical Products, Inc. Biopsy site marker deployment instrument
NL2002862C2 (en) * 2009-05-08 2010-11-09 Friesland Brands Bv Microfluidic apparatus and method for generating a dispersion.
JP5947214B2 (ja) * 2009-10-09 2016-07-06 ブルー キューブ アイピー エルエルシー 断熱栓流反応器及び該断熱栓流反応器を組み込んだプロセス
CN102665886B (zh) 2009-11-30 2015-02-18 康宁股份有限公司 蜂窝状本体u形弯曲混合器
EP2539066A2 (fr) 2010-02-28 2013-01-02 Corning Incorporated Mixers interdigités à corps en nid d'abeille et procédés pour leur production
JP5507296B2 (ja) * 2010-03-09 2014-05-28 富士フイルム株式会社 化学反応物の製造方法及び製造装置
DE102010041282A1 (de) * 2010-09-23 2012-03-29 Behr Gmbh & Co. Kg Mischelement und Mischmodul für zwei sich in einem Klimagerät kreuzende Luftströme
HUE036624T2 (hu) 2010-09-28 2018-07-30 Dow Global Technologies Llc Reaktív folyadék statikus keverõ keresztáramú akadályokkal, és keverési eljárás
US9421507B2 (en) * 2012-04-30 2016-08-23 Oregon State University Micro-channels, micro-mixers and micro-reactors
EP2689837A1 (fr) 2012-07-23 2014-01-29 Basf Se Verfahren zur Herstellung von Fettsäureniedrigalkylestern durch Umesterung
DK2972332T3 (en) 2013-03-14 2018-09-03 Siemens Healthcare Diagnostics Inc Microfluid chip with sealed reagent
US20150010874A1 (en) * 2013-07-03 2015-01-08 Oregon State University Microscale combustor-heat exchanger
US9383143B2 (en) * 2013-09-26 2016-07-05 Micro Cooling Concepts, Inc. Metallic thin-film bonding and alloy generation
US10161690B2 (en) * 2014-09-22 2018-12-25 Hamilton Sundstrand Space Systems International, Inc. Multi-layer heat exchanger and method of distributing flow within a fluid layer of a multi-layer heat exchanger
DE102017205286A1 (de) * 2017-03-29 2018-10-04 Robert Bosch Gmbh Mikrofluidische Vorrichtung und Verfahren zur Temperaturregelung eines Arbeitsfluids
DE102017009854A1 (de) * 2017-10-22 2019-04-25 Hochschule Mittweida (Fh) Eine Medienströme beeinflussende Mikroeinrichtung mit einem Kernstück mit voneinander getrennten Kanälen und mit wenigstens einem Anschlusselemente aufweisenden Anschlussstück am Kernstück

Family Cites Families (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE732632C (de) * 1937-02-25 1943-03-08 Kraftanlagen Ag Vorrichtung zur Vereinigung zweier Fluessigkeitsstroeme unter Temperaturausgleich, insbesondere fuer Warmwasserheizungs- und Gebrauchswasseranlagen
GB612012A (en) * 1945-10-09 1948-11-08 Harry Stewart Wheller Improvements in mixing chamber for use in heating or cooling devices
FR1261312A (fr) * 1960-04-05 1961-05-19 Saint Gobain Procédé et dispositif statique de mélange de fluides
JPS5134869B1 (fr) * 1971-01-11 1976-09-29
US4407785A (en) * 1972-11-28 1983-10-04 Engelhard Corporation Method of conducting catalytically promoted gas-phase reactions
US4198168A (en) * 1978-04-12 1980-04-15 Liquid Control Incorporated Phase blending static mixing process and apparatus
SE432059B (sv) 1980-04-11 1984-03-19 Munters Ab Carl Blandningsanordning for blandning av strommande medier innefattande minst tva system av atskilda genomstromningskanaler
NL8602338A (nl) * 1986-09-16 1988-04-18 Hoogovens Groep Bv Gasmenger.
DE3709278A1 (de) * 1987-03-20 1988-09-29 Kernforschungsz Karlsruhe Verfahren zur herstellung von feinstrukturkoerpern
DE3926466C2 (de) * 1989-08-10 1996-12-19 Christoph Dipl Ing Caesar Mikroreaktor zur Durchführung chemischer Reaktionen von zwei chemischen Stoffen mit starker Wärmetönung
ATE151664T1 (de) * 1990-05-08 1997-05-15 Sulzer Chemtech Ag Katalysatoranordnung in einer kolonne
ATE130220T1 (de) * 1991-07-30 1995-12-15 Sulzer Chemtech Ag Einmischvorrichtung kleiner fluidmengen.
CA2189783A1 (fr) * 1994-05-09 1995-11-16 Klaus Schubert Procede et dispositif permettant la realisation de reactions chimiques au moyen d'un melange a microstructure
DE4416343C2 (de) * 1994-05-09 1996-10-17 Karlsruhe Forschzent Statischer Mikro-Vermischer

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO9717130A1 *

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KR19990067310A (ko) 1999-08-16
JPH11514574A (ja) 1999-12-14
DE19541266A1 (de) 1997-05-07
US6264900B1 (en) 2001-07-24
WO1997017130A1 (fr) 1997-05-15
US6299657B1 (en) 2001-10-09

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