DE10356369B4 - Apparatus and methods for generating fluid assemblies from fluids - Google Patents

Abstract

Device for producing a fluid arrangement of fluids with the following features:
a rotary body (124; 140) rotatable about a rotation axis, in which a closed fluid channel (12; 40; 70; 120; 170; 170 ') with a channel geometry is arranged between a channel inlet (14; 52; 72) and a channel outlet (16) is formed, wherein the fluid channel in the main extension direction with respect to the axis of rotation has radial components;
means (140, 142, 144) for pressurizing the fluid channel (12; 40; 70; 120; 170; 170 ') at a rotational speed about the axis of rotation to drive fluid by centrifugal force through the fluid channel;
wherein the channel geometry and the rotational speed are set such that the centrifugal force due to the channel geometry causes a velocity profile across the channel cross section through which different Coriolis forces are exerted on the fluid over the channel cross section, such that a fluid arrangement of a first fluid and a second fluid at the channel inlet (14; 52; 72), a fluid arrangement is created at the channel outlet (16), in which the diffusive mixing time ...

Description

The The present invention relates to devices and methods for producing a fluid assembly of fluids.

The Mixing liquids can formally be divided into two steps. The first Step consists in the contacting of the liquids to be mixed at the macroscopic level, while the second step in the mixing of substances on molecular Level consists of diffusion. To increase the speed of mixing maximize the diffusion lengths between the fluids, which of the minimum distance between zones with different ones Corresponds to phases and square in the diffusion time, to minimize. This diffusion length is determined in the above-mentioned first step, while the molecular diffusion in the second step essentially by the Diffusion constants of the usually predetermined starting materials is determined.

Technical Mixing concepts are therefore primarily aimed at optimization of the first step. This is by the coupling of mechanical Energy creates turbulence, which is the interface for the mutual Distorting or even dismembering the transfer of substances and thus the effective surface extremely large. One simple example of this is a stirrer.

issues the mixing is in the spatial and temporal homogeneity. Technical procedures, for example, by a motor-driven stirrer, run perio in time and spatially not homogeneous, which only after some time in a quasi-chaotic and thus the homogeneity guaranteeing Behavior is reflected. typically, will be a good mix first produced in zones, before over time entire medium extends. In macroscopic vessels becomes the chaotic behavior supported by the formation of turbulence, resulting in the strictly laminar conditions in microchannels with characteristic channel widths of 10 microns to several 100 microns not the Case is.

Basically too different are mixers for miscible and immiscible fluids. In the first case, a thorough mixing At the molecular level, that is, a solution can be achieved, in the second a dispersion of several phases, such as liquid-liquid. (Emulsion) or gaseous solid (Aerosol).

at all microchannels The laminar flow conditions cause severe limitations in terms of the speed of diffusion-driven processes, for example mixing and subsequent chemical reactions. Since the beginnings In the field of microfluidics, many concepts have been developed to date improve mixing, the active elements, such as piezo actuators, Heating elements and external pumps, or passive three-dimensional microstructures, such as caterpillar structures and the like, whose manufacture is complex with standard equipment is, include. It is clear that these requirements are not typical technological and economic restrictions are compatible, especially for disposable devices in many life science applications.

G. Ekstrand u. a. describe in "Microfluidics in a rotating CD ", in: Proc. μTAS 2000, pp. 311-314, Kluwer, The Netherlands, Microfluidic Applications on a CD Platform. In particular, the handling of discrete liquid volumes in the nanoliter range using centrifugal force on a rotating CD.

Also in MJ Madou et al., "The LabCD ^™ : A Centrifuge-Based Microfluidic Platform for Diagnostics", in: Proceedings of SPIE, Vol. 3259, pp. 80-93, 1998, the handling of fluids on rotating discs is described below using centrifugal pumps, valves, mixers, and metering devices in the form of capillaries structured with hydrophobic coatings.

From the US 6585237 B2 For example, a mixer is known in which a stirrer has a plurality of notched and twisted strips which are bundled in the form of a heir with a longitudinal axis. The stirrer is mounted on a shaft to be immersed in a vessel filled with liquid and rotated to effect mixing of the liquid. The axis of rotation can either coincide with the longitudinal axis or be perpendicular to the same.

The Object of the present invention is devices and to provide methods of producing fluid assemblies from fluids, wherein the fluid arrangement for a fast diffusive mixture of fluids is suitable with Fluidic structures of a simple structure can be implemented.

These The object is achieved by devices according to claims 1, 2, 15 and 16 and method the claims 17 and 18 solved.

The present invention relates to a novel concept for mixing fluids in a fluid channel utilizing centrifugal force. The present invention makes use of the knowledge that a parabola which forms in a rotating or rotationally accelerated fluid channel by the centrifugal force or Euler force sches flow profile can be used together with the acting in the transverse direction of the Coriolis effect to change the arrangement of two fluids to be mixed with each other such that the diffusive mixing time between them is reduced. The diffusive mixing time is reduced by reducing the diffusion length between the fluids. This diffusion length may preferably be reduced by causing the fluids to have, for example in a thin layer, a larger contact area with each other. In addition, the diffusion length can be reduced by creating a fluid assembly having a larger number of fluid layers thin relative to the layers of the exit assembly.

at preferred embodiments According to the invention, the fluid channel comprises a plurality of subchannels. Further is the fluid channel in preferred embodiments at a radial inner portion extending to a radially outer portion in a rotation body formed, which is rotatable about an axis of rotation. The alignment the fluid channel is such that the same at least radial components so that a fluid therein in rotation is subjected to a centrifugal force. In preferred embodiments the fluid channel will be arranged radially.

The present invention enables a significant acceleration of the mixing of laminar flows generally radial microchannels on the rotation body, which can be a rotating disk. This will be transversal Flow pattern generated in the fluid channel by the pseudo-Coriolis force. By adjusting or optimizing the channel geometry and the rotational speed as the key parameters The induced convection can be used to align two parallel rivers to control and even reverse. These findings can too a novel laminator by dividing and recombining to lead, which by a simple arrangement of rectangular microchannels with low aspect ratio gebil det is achieved by the drastically reduced mixing times can.

preferred embodiments The present invention will be described below with reference to FIG the enclosed drawings closer explained. Show it:

1a a schematic plan view of an embodiment of a rotary body with a fluid channel for use according to the invention;

1b a schematic representation of by rotation in the fluid channel of 1a generated effects;

1c a schematic plan view of another embodiment of a rotary body with a fluid channel for use according to the invention;

1d a schematic representation of by rotation in the fluid channel of 1c generated effects;

2 a schematic representation of a divided into quarter-length fluid channel;

3 schematic diagrams showing a comparison of measured and simulated results of the fluid channel of 2 show at constant rotational speed;

4 schematic diagrams showing a comparison of measured and simulated results for the in 2 shown fluid channel at different rotational speeds;

5a a schematic representation of a fluid channel having a plurality of sub-channels;

5b a schematic representation of another embodiment of a fluid channel used in the invention;

6 a schematic representation of a practical implementation of a fluid channel having a plurality of sub-channels;

7 a detail of a plan view of a disc, in whose surface structures for implementing a mixer according to the invention are formed;

8th a schematic representation of an implementation of a mixer according to the invention;

9 and 10 schematic plan views of embodiments of the in 8th shown mixer usable rotating bodies; and

11 a schematic plan view of a rotary body in which fluid channels, which allow high throughput, are arranged.

Before discussing preferred embodiments of the present invention, reference will first be made to FIGS 1a and 1b the physical effects underlying the present invention explained in more detail.

The present invention will generally find application for the mixing of liquids, however, it may also be used to mix gases and liquids or to mix gases with each other. Moreover, the present invention may be used to effect mixing of fluids without simultaneous and subsequent reaction therebetween or mixing of fluids with a simultaneous or subsequent reaction therebetween.

In 1a is a substantially circular body of revolution 10 shown in which a fluid channel 12 is formed. On the surface in which the fluid channel 12 is formed, a lid may be applied, wherein a channel inlet and a channel outlet are provided for the fluid channel.

The liquids to be mixed are in a channel inlet 14 let in on the inside and on rotation of the body of revolution 10 with an angular velocity ω in common via the centrifugal force with the flow velocity ν → (F → ω ) are driven outwards. The fluids then leave the fluid channel 12 via a duct outlet 16 and are either in a vessel (not shown) on the body of revolution 10 or a surrounding vessel (not shown) into which the fluids pass via the channel outlet 16 arrive, collected.

In the rotating reference system, in which the channel structure, ie the fluid channel 12 , is at rest, acts in addition to the centrifugal force and the Coriolis force F _Coriolis (Coriolis apparent force), which at a radially extending fluid channel perpendicular to the local velocity vector ν → (F → ω ) of the fluid and directed to the vector of rotational movement ω. This Coriolis force thus creates across the channel structure a cross-flow which distorts the interface between the fluids and thus shortens the maximum diffusion lengths.

In 1b is the fluid channel 12 shown with the following channel geometry: channel width Δx, channel height h and channel length l. The channel width .DELTA.x may for example be 300 .mu.m, the channel length may be, for example, 2 cm and the channel height may be 120 .mu.m, for example, in order to realize a fluid channel with a low aspect ratio. The dimensions given are purely examples and any channel dimensions can be used , as long as by the centrifugal force or Eulerkraft a speed profile 18 is generated across the channel cross-section through which different Coriolis forces are exerted on the fluid over the channel cross-section, as by the arrows of different length in the Coriolis force distribution 20 in 1b is shown. Due to the nonuniform distribution of the transverse Coriolis force, which is a consequence of the parabolic shaped component 18 of the velocity field ν → (F → ω ) respectively. ν → (F → Euler ) is, caused transversal "stirring" flow 22 is also in 1b shown.

Due to the specified stirring flow, the arrangement of two in the channel inlet 14 introduced fluids are modified such that the diffusive mixing time between the first fluid and the second fluid compared to the fluid arrangement at the channel inlet is reduced at the channel outlet, ie a mixing of the two fluids can be brought about so that a subsequent molecular diffusion can proceed faster.

The generation of a stirring flow through the velocity distribution ν → (F → Euler ) is in the 1c and 1d shown. A stirring flow can also be achieved if a fluid channel in the form of a circular arc segment is formed in a rotary body and the rotational body is subjected to a rotational acceleration. In 1c is a substantially circular body of revolution 220 shown in which a fluid channel 222 is formed. Again, a lid may be applied, with a channel inlet and a channel outlet for the fluid channel 222 are provided.

With a rotational acceleration, the fluid can also be driven on intermediate pieces along a circular arc via the Euler force. Viewed from a rotationally accelerated system, the fluid experiences along a circular arc the Euler acceleration and the ensuing Euler force F _Euler . This creates an inhomogeneous azimuthal flow profile 224 which then has an inhomogeneous Coriolis force field (F _Coriolis ) 226 as well as the centrifugal force F _ω act.

Consequently For example, the present invention may also be implemented using a channel with azimuthal course with a corresponding device for Implementation of the channel with a rotational acceleration implemented be. Such a device may be powered by a device of the rotational body be formed with a rotation, wherein a respective rotational acceleration then causes when starting and / or stopping the rotating body becomes. Furthermore, the present invention with a channel with azimuthal and radial components are implemented so that a combination of elliptical force and centrifugal force occurs.

As will be shown below, the channel geometry of the fluid channel 12 and the rotational speed ω and the rotational acceleration dω / dt, respectively, to establish advantageous arrangements between the two at the channel Allow introduced fluids to effect at the duct outlet.

2 shows a schematic representation of the fluid channel 12 which is subjected to rotation at an angular velocity ω, whereby a centrifugal force F → ω and a Coriolis force F → Coriolis placed on one in the fluid channel 12 present fluid act, are generated.

As in 2 is shown located at the fluid inlet 14 an arrangement of a first fluid A and a second fluid B. The fluids A and B are in the fluid channel 12 arranged with low aspect ratio horizontally next to each other. Such an arrangement can be achieved, for example, in that two sub-channels running in the same plane merge into a common channel, wherein the point at which the sub-channels merge into the common channel can be understood as a channel inlet in the sense according to the invention.

Using the in 2 The arrangement of the two fluids A and B to each other along the length of the channel was simulated. The fluids used were miscible inks of different colors, the dimensions of the channel referring to the above 1b described corresponded. Furthermore, a rotation speed of 300 rad s ^{-1 was used} for the simulation. Further, the behavior was experimentally measured in an identical channel formed in a round disk.

In 2 are the simulated mixed patterns at the channel inlet 14 , after a quarter of the canal, position 30 , after half of the channel, position 32 , after three quarters of the canal, position 34 , and at the duct outlet 16 shown. As can be clearly seen, under the influence of the Coriolis force, the initially undisturbed flow pattern in the flow direction is increasingly deformed. At 3/4 of the channel length, position 34 , the liquid B has penetrated far into the liquid A, so that substantially a vertical arrangement of three layers, ABA has resulted.

3 shows a comparison of the simulated and measured results obtained at the different channel positions. More specifically contains 3 four diagrams, one for the channel inlet, one for the position 30 , one for the position 32 and one for the position 34 , On the x-axis of the respective diagrams, the lateral position is plotted in microns (across the width of the channel), while along the y-axis the optical intensity accumulated along the dashed line, ie across the height of the channel, is plotted. The solid curves correspond to the measured results, while the dotted lines represent the simulated results.

In the right outer diagram of 3 is the mentioned three-layer structure of three vertically superimposed liquid layers to recognize. In this vertical stack of thin liquid layers, the characteristic diffusion length d is about a factor of about 3 versus the characteristic diffusion length d at the fluid channel inlet (left outer side of FIG 3 ) reduced. This results in a reduction of the diffusion times t _d proportional d ² by a factor of 9 in a normal straight microchannel. It is clear that this effect occurs more intensively with even lower aspect ratios which can be easily produced. Furthermore, the good qualitative agreement between the measured results and the corresponding simulations should be noted.

Out 3 It can be seen that the resulting mixing pattern depends on the length of the fluid channel, so that by a suitable adjustment of the length a mixing pattern with desired properties, for example one in which the characteristic diffusion length is reduced, can be obtained.

4 shows measured and simulated results at the outlet of 2 shown channel, which was acted upon at different rotational speeds. As in the middle diagram of 4 can be seen results in a rotational speed of 50 rad s ^-1, only a very small change in the Fluidkanaleinlass present fluid pattern, so that the Fluidkanalauslass turn the two liquids A and B are arranged substantially horizontally arranged side by side fluid layers. As in the middle diagram of 4 can be seen results at a rotational speed of 200 rad s ^-1 at Kanalaus let the liquid pattern of substantially three vertically stacked layers BAB. Finally, at a rotational speed of 300 rad s ^-1 at the fluid channel outlet, there is essentially a reversal of the fluid layers present at the channel inlet, so that, as in the right-hand diagram of FIG 4 is shown, the liquid B is arranged to the left of the liquid A.

The in the 3 and 4 The results shown show that the exact flow profile is determined by the interaction of the rotational frequency or rotational acceleration with the geometry of the channel structure. On the one hand, the centrifugal force or the Euler force and thus the radial pumping rate can be adjusted via the rotational frequency or rotational acceleration. On the other hand, the rotational frequency or rotational acceleration but also determines the mixing process, in the transverse direction via the Coriolis effect and in the longitudinal direction via the formation of a parabolic flow profile, the so-called Taylor dispersion.

As stated above, in the simplest case the channel structure can consist of a radially guided channel with a rectangular cross-section. By appropriate adjustment of the channel geometry and the rotational frequency, as shown above, a desired liquid pattern at the fluid channel outlet can be brought about. It should be noted that with respect to the 2 to 4 The simulations that have been described in each case essentially ignore the diffusion between the liquids that occurs during the propagation of the fluids through the fluid channel. It should also be noted that the viscosity of the liquids to be mixed enters into the mixing process, so that the adjustment of fluid channel geometry and rotational frequency also has to be made depending on the fluids to be mixed.

The principle of hydrodynamic flux lamination based on the flow through a radial microchannel on a rotating disk has been described above. In this case, the centrifugal force F _ω or Euler force F _Euler acting at an angular velocity (or an angular acceleration dω / dt on the fluids in the microchannel F _Euler , which is proportional to ω → 2 or dω / dt, results in a parabolic velocity profile. This in turn has a velocity-dependent Coriolis force F → Coriolis result, which is proportional to ν → · ω → and perpendicular to ν → (F → ω ) respectively. ν → (F → Euler ) is such that it is largest in the middle of the channel where the centrifugal velocity profile is maximum. This Coriolis force can be used to control the arrangement of two or more flows in the microchannel to each other. As shown, the inhomogeneous force field caused by the Coriolis force causes fluid movement from the center of the microchannel to one of its walls. The continuity dictates that the slow fluid escapes in the outer region along the outer circumference, where the field counteracted by the Coriolis force is minimal. The resulting transversal fluid flows lead to a "stirring" of two parallel flows, as in the simulations and experiments described in the 2 to 4 are shown, can be seen. As has been stated, the key influencing parameters that control this hydrodynamic process are the channel geometry, the viscosity and the rotational speed ω and the rotational acceleration in the case of azimuthal channel sections, respectively.

By the splitting of the flow caused by the centrifugal force the liquids to be mixed into several, parallel channels, which farther out merged again can, can In addition, a multilamination can be achieved, which makes the times for the diffusive Mixing to a considerable extent can further shorten.

A schematic representation of a fluid channel that can be used for this purpose 40 is in 5a shown. The fluid channel 40 includes a first channel section 42 , a first branching 44 , at which the first channel section 42 in four subchannels 46a - 46d branches, a second branch 48 at which the four subchannels are brought together again, and a second common channel section 50 that with the second branch 48 fluidly connected.

At the canal inlet 52 of the fluid channel 40 lie at the 54 shown arrangement of a first liquid A and a second liquid B before. Furthermore, the first channel section 42 such channel geometry, height, length and width, on that in the end 56 of the first channel section at 58 in 5a shown liquid pattern of the liquid layers ABA is present, ie that the two horizontally adjacent liquid layers A and B were transferred into three horizontally superimposed liquid layers ABA. At the entrances of the subchannels 46a - 46d then arise at 60 in 5a shown liquid pattern of three superimposed layers. The subchannels 46a - 46d Now have such a length that at the given rotational speed ω present at the entrance of the sub-channels liquid pattern 60 in the at 62 in 5a shown liquid pattern are transferred at the output of the sub-channels. After merging the subchannels through the branch 48 is then at the beginning 64 the second common channel section 50 that at 66 in 5a shown fluid pattern of vertically juxtaposed fluid layers BABABABA ago.

Thus, by using the in 5a shown fluid channel 40 from the fluid assembly AB at the fluid channel inlet 52 a multilaminated fluid arrangement 66 fluidly behind the second branch 48 , The first branch 44 is placed where from the fluid assembly AB at the channel inlet 52 the vertical ABA sandwich 58 was generated. The second branch 48 is then placed where from the vertical ABA arrangements 60 the horizontal BA arrangements 62 caused by the Coriolis force, where then finally the eightfold lamination at the entrance of the common outlet channel, ie the second common channel section 50 is reached.

The in 5a shown fluid channel 40 , which is subjected to a rotational speed, thus represents a novel split and recombine Lami nator (split and recombine) by means of a simple micro-channel geometry.

Another embodiment of a fluid channel 70 a laminator according to the invention is in 5b shown. The fluid channel 70 shares directly with the canal inlet 72 in three subchannels 74a . 74b and 74c , The subchannels 74a . 74b and 74c then reunite to a common channel section 76 into a duct outlet 78 empties.

At the canal inlet 72 Again, there is a horizontal AB fluid arrangement, as in 80 in 5b is shown. Such a fluid arrangement can be effected, for example, by two partial channels at the channel inlet 82a . 82b be merged as in 5b indicated by dashed lines. The subchannel 82a doing the liquid A, while the sub-channel 82b the liquid B leads.

The two rivers become the three subchannels 74a . 74b and 74c split, where in the sub-channel 74a the liquid A flows, in the sub-channel 74c the liquid B flows and at the beginning of the middle sub-channel 74b a horizontal AB arrangement is present. The resulting at the entrance of the sub-channels fluid assembly is at 84 in 5b shown. The sub-channels now have such a length that an inversion of the 84 shown BA arrangement in the middle sub-channel 74b so that at the output of the subchannels at 86 in 5b shown fluid arrangement in the form of an ABAB pattern.

This pattern, which is present at the output of the subchannels, becomes at further flow along the common channel section 76 directly disturbed by the present due to the rotational speed Coriolis force, so that along the common channel section 76 a mixing starting from the at 86 shown fluid pattern takes place.

By the in 5b As shown, the thickness of the liquid layers decreases from the entrance of the sub-channels to the exit thereof by a factor of two. By cascading a series of n (for example, 3) congruent laminators, the maximum layer thickness can be reduced by a factor of 2 ^-n (8) to reduce the mixing time t _D for subsequent diffusive mixing by a factor of 2 ^-2n (64). to reduce. In order to prevent sub-channels with a high aspect ratio, the in 5b shown, the sub-channels defining ribs 90 be designed with a larger width, without disturbing the lamination mechanism.

In the in the 5a and 5b In the exemplary embodiments shown, the channel outlet may, in the sense according to the invention, be located both at the channel section at which the partial channels are reunited in each case, and at the end of a specific length of the second common channel section 50 respectively. 76 , The terms channel inlet and channel outlet are thus according to the invention to be understood as meaning respective channel sections on which the respective fluid arrangements are present. Such channel sections are not limited to those at which the channel actually starts or ends, but rather can connect to the channel inlet or channel outlet further channel sections, which may have other channel geometries.

An implementation of a fluid channel having four sub-channels, as may be formed in the surface of a rotary disc, is shown in FIG 6 shown. Since it is the in 6 shown fluid channel to a practical rea lization of in 5a can be schematically shown fluid channel are in 6 same elements as in 5a denoted by the same reference numerals. To form the channel are in the surface of a rotation disk 100 Recesses formed, which are the first channel section 42 , the subchannels 46a - 46d and the second common channel section 50 define. The subchannels 46a - 46d are here by respective bars 102 defined, which may have a width to realize a low aspect ratio of the sub-channels.

The channel geometry of in 6 In turn, the fluidic structure shown may be of the type that the reference to 5a described multilamination after the second branch 48 is obtained.

To produce such a laminated structure, for example, when mixing two inks of different colors at the channel inlet 52 For example, the channel geometries may be as follows:
Depth of the channels in the plate 100 : 150 μm;
Width of the channel section 42 : 680 μm;
Length of the channel section 42 : about 8 mm;
Length of the sub-channels about 8.4 mm;
Width of the common channel section 50 : about 480 μm;
Width of the sub-channels about 250 microns.

As in 6 can be seen, the channel structure may be formed by the production of recesses in the surface of a rotating body. The rotational body can be, for example, a disc made of plastic, glass or silicon, wherein the channel structures can be produced by etching, scribing, laser treatment or the like in any known manner. The channel structures used in the invention provide Thus, so-called 2.5-dimensional microchannels that can be easily formed in the surface of a rotating body.

Of the Expression 2.5-dimensional stands for that in the third dimension only the depth is manipulated, but not in different Layers running channels must be generated.

From the in 6 The surface structure shown, the finished channel structure can then be produced by a lid is applied to the surface in which the recesses are formed, for example by gluing or bonding. The liquid supply or discharge into or out of the channel structures can then take place through the openings remaining at the edge. Alternatively, in the lid (or in the rotating body 100 ) Openings are provided, through which the liquids can get into and out of the channel structure.

A section of an embodiment of a rotary body having fluid structures formed therein for implementing the present invention is shown in FIG 7 shown. In the rotary body is a fluid channel 120 formed, which may have, for example, one of the forms described above. The outlet of the fluid channel 120 is with an outlet reservoir 122 fluidly connected. The outlet reservoir 122 is as a circumferential ring in a disk 124 , which serves as a body of revolution and may have the form of a compact disk (CD) formed. The fluid inlet of the fluid channel 120 is (via subchannels 126a . 126b ) with a first inlet reservoir 128 and a second inlet reservoir 130 connected. Located in the inlet reservoir 128 the liquid A and in the inlet reservoir 130 the liquid B, so can through the in 7 shown arrangement in the inlet of the fluid channel 120 a horizontal AB arrangement (such as in 54 in 5a shown).

The disc 124 has in the example shown a central hole 132 through which the disc 124 can be placed on a drive device to apply to the disc in the manner of a CD at a rotational speed.

An exemplary embodiment of an apparatus according to the invention for producing a fluid arrangement, which can be referred to as a Coriolis mixer and can serve, for example, as a compact tabletop unit for laboratory use, is disclosed in US Pat 8th shown.

The mixer comprises a body of revolution 140 in the form of a disk in which fluid channels are formed, as hereinafter referred to 9 and 10 is explained in more detail. The disc 140 sits on a pedestal 142 , in turn, with a wave 144 a drive motor (not shown) is connected. By the drive motor, the shaft 144 and the pedestal 142 can the rotation body 140 with a rotational speed ω or a Rotationsbeschleunugung dω / dt be applied.

On the from the pedestal 142 opposite side of the rotating body are a first liquid reservoir 146 for a liquid A and a second liquid reservoir 148 for a liquid B. The first liquid reservoir 146 is circular about an axis of rotation 150 of the rotational body 140 (with the rotation axis of the base 142 and the wave 144 coincident). The second fluid reservoir 148 is formed concentrically around the first liquid reservoir A. The liquid reservoirs 146 and 148 are fixed to the rotation body 140 attached for rotation with the same.

At the in 8th In the embodiment shown, the arrangement described above is in a rigid holder arrangement 152 arranged. The holder assembly 152 has a suitable bearing, which is a rotatable mounting of the shaft 144 or the base 142 allows. Alternatively, the drive motor (not shown) is in the holder assembly 152 appropriate.

The rigid holder arrangement 152 can, as shown schematically in 8th through arrows 154 is shown to have mounts to refill the Flüssigkeitsreservoire 146 and 148 with respect to the holder assembly 152 to allow stationary dispensers.

The rotation body 140 has lateral channel outlets, which in the embodiment shown by centrifugal ball valves 156 are closed at rest. Upon application of the rotating body 140 at a rotational speed, the centrifugal ball valves are opened by the centrifugal force that occurs.

The stationary holder assembly 152 further comprises a circumferential, circular side wall 160 , pointing to the lateral outlet openings of the rotating body 140 emerging fluids impinge, as indicated by arrows in 8th is indicated. Outflowed fluid runs on the side wall 160 down, as by arrows 162 in 8th is indicated. The liquid running down collects in a receptacle 164 that may be part of the rigid holder assembly.

In order to be able to control the temperature of the ejected liquids exactly, a tempering device can be used 166 in the form of one or more heating elements or cooling elements on the outside the side wall 160 be provided. The tempering device may be formed as a circulating tempering device to control the temperature of the circumferential side wall to a desired temperature.

Schematic top views of the rotating body 140 with the liquid reservoirs 146 and 148 to explain the structure of the same are in the 9 and 10 shown. According to 9 is in the rotation body 140 a fluid channel 170 formed, in the over a first and a second part of the channel 172 and 174 Liquids from the reservoirs 146 and 148 be fed to the inlet of the fluid channel, a horizontal arrangement of the liquids A and B, as for example at 54 in 5a is shown to effect. In which the fluid channels 170 . 172 and 174 Covering lids are openings 176 formed over which the reservoirs 146 and 148 with the subchannels 172 and 174 are fluidly connected. Thus it is possible through the reservoirs 146 and 148 continuously liquid in the fluid channel 170 supply. Furthermore, it is possible to use the fluid reservoirs 146 and 148 through the dispensers 154 be continuously supplied with liquids, so that the arrangement shown allows continuous operation.

The fluid channel 170 has any structure to mix over the subchannels 172 and 174 to bring in supplied liquids. For example, the channel 170 be designed as a single channel with appropriate channel geometry, as in 9 is shown. Alternatively, a channel 170 ' be provided with a plurality of sub-channels, such as in 10 is shown.

Although in the 9 and 10 only one radially outwardly extending channel 170 respectively. 170 ' is shown, may be provided to increase the throughput, a plurality of radially outwardly extending channels. A schematic representation of a rotating body 140 with such a plurality of radially outwardly extending fluid channels is in 11 shown.

In operation of the Coriolis mixer used in 8th is shown, the rotational body 140 over the pedestal 142 and the wave 144 with a rotational speed ω and rotational acceleration dω / dt acted upon. It has been found that to achieve transverse mixing using the Coriolis force as utilized in the present invention, it is preferred to use a rotational speed greater than 100 rad s ^-1 where the Coriolis force prevails.

From the liquid reservoirs 146 and 148 the liquids A and B pass over the openings 176 by gravitational force 180 ( 8th ) into the subchannels 172 and 174 where they are driven by the prevailing due to the rotational speed ω centrifugal force to the outside. From there, they are forced into the fluid channels by the centrifugal force 170 respectively. 170 ' driven, where due to the also prevailing Coriolis force mixing of the liquid A and B takes place. Finally, the fluids leave the body of revolution 140 at the side outlets of the same and hit the wall 160 where they run down in a thin movie. Because the mixed fluids in a thin film on the wall 160 can run down through the tempering device 166 a homogeneous temperature distribution can be achieved in these fluids. Finally, the mixed liquids in the receptacle 164 collected.

The in 8th For example, the Coriolis mixer shown can be used as a compact bench-top device for laboratory use and is characterized by its extremely fast mixing of reactants. For the chemical process technology, it could be contacted with cooling or heating elements, which allows the temperature of the reactants to be set very precisely and promptly, particularly in microstructures. For example, it is conceivable to realize a cooling or heating device by a disk on which the disk of the rotating body 140 sits, said heating disk or cooling disk is brought to the temperature to which the liquids or reactants in the rotary body 140 to be brought. This tempering disk could have fluidic structures for tempering liquids or tempering gases and could be used for rotation with the rotation body 140 be arranged. As a result, the tempering liquids or tempering gases can likewise be conveyed through the tempering disk by the centrifugal force. Alternatively, appropriate temperature control channels on the base 142 be provided. The residence time of the liquid can be increased by azimuthal channel segments in which the Coriolis force also, in addition to the Zentrigugalkraft, transversely to the channel abuts.

Since the mixing process is induced in the devices and methods of the invention via a force field which extends over the entire channel, the homogeneity of the mixing tends to improve over a point-acting actuator. In addition, the centrifugal force represents a volume force and thus allows higher flow rates with a given structural cross-section compared to a pressure-driven flow. As referring to 11 was addressed, the total throughput can be increased by parallelization on the arrangement of the channel structures symmetrical to the center of rotation similar to the spokes of a wheel easily. It can all parallel channels are driven by the same "pump", namely the rotary motor The centrifugal pump drive used according to the invention does not require a fluidic connection to a pump.

For the inventive method and devices suffice as channel structures in principle simple radial channels with low Aspect ratios, which are microtechnologically easy to manufacture and thus for a cost-effective mass production accessible are. Thus, the blending structure can be used as a disposable module with a reusable rotary motor are designed. In microstructures is the flow behavior laminar and actuators are heavy and only expensive to integrate. The Centrifugal force here provides a unique way of energy for mixing to be able to couple into the fluids without integrated actuators. The laminar behavior in microstructures also ensures very good reproducible mixing results. The temperatures of the liquids in micro channels can be very be quickly regulated. Reduce the low volumes in microchannels Furthermore, the risk of uncontrolled reactions, such as Explosions. Furthermore, the small channel volumes of microchannels mean low Dead volumes.

Devices according to the invention for producing a fluid arrangement, i. H. inventive mixer, can have further equipment. To name here are in particular the already mentioned heating or cooling elements, through which the temperature the educts and products precise can be adjusted. Furthermore, a device for pressurizing the, preferably cylindrically symmetric, reservoirs, from which the educts over the gravity and the suction of the downstream centrifugally expelled Fluids in the channels be provided to adapt to different viscosities or to provide flow rates of the reactants. Finally, integrated flow sensors for monitoring be provided. After all can instead of the mentioned centrifugally controlled ball valves the outlet openings of the channels if necessary, other valves may be provided which are at rest leakage of liquids prevent while they enable it in operation.

The present invention provides devices and methods for mixing fluids which, on the one hand, manage with a simple structure and, on the other hand, enable high throughput and thorough mixing of the fluids. The present invention is not limited to mixing two fluids, and the systems described herein may be readily understood by one skilled in the art to mix more than two fluids. In particular, the realization of a fluid channel with a plurality of n subchannels, which are connected in fluidic parallel, allow a 2n-fold multilamination, which reduces the diffusive mixing time with respect to an incoming AB pattern by a factor of n ² . Thus, for example, a number of ten parallel channels results in a reduction of the diffusive mixing time by a factor of 100. According to the invention, a mixing speed comparable to conventional LIGA micromixers using multilamination by a pressure-driven flow can thus be achieved. However, according to the invention, fabrication is greatly simplified because no high aspect ratios are required to minimize flow resistance, and no three-dimensional guiding structures are needed to implement split-and-recombine flow schemes. The complexity of the system according to the invention is further reduced because the centrifugal volume force provides an inherent pump.

Claims (18)

Device for producing a fluid arrangement from fluids with the following features: a rotational body which can be rotated about an axis of rotation ( 124 ; 140 ), in which between a channel inlet ( 14 ; 52 ; 72 ) and a channel outlet ( 16 ) a closed fluid channel ( 12 ; 40 ; 70 ; 120 ; 170 ; 170 ' ) is formed with a channel geometry, wherein the fluid channel in the main extension direction with respect to the axis of rotation has radial components; a facility ( 140 . 142 . 144 ) for acting on the fluid channel ( 12 ; 40 ; 70 ; 120 ; 170 ; 170 ' at a rotational speed about the axis of rotation for driving fluid by centrifugal force through the fluid channel; wherein the channel geometry and the rotational speed are set such that the centrifugal force due to the channel geometry causes a velocity profile across the channel cross section through which different Coriolis forces are exerted on the fluid over the channel cross section, such that a fluid arrangement of a first fluid and a second fluid at the channel inlet ( 14 ; 52 ; 72 ) a fluid arrangement at the channel outlet ( 16 ), in which the diffusive mixing time between the first fluid and the second fluid with respect to the fluid arrangement at the channel inlet ( 14 ; 52 ; 72 ), wherein the first and the second fluid in the fluid arrangement at the channel outlet have a larger contact surface with each other than in the fluid arrangement at the channel inlet. Device for producing a fluid arrangement from fluids with the following features: a rotational body which can be rotated about an axis of rotation ( 124 ; 140 ), in which between a channel inlet ( 14 ; 52 ; 72 ) and a channel outlet ( 16 ) a closed fluid channel ( 40 ; 70 ; 120 ; 170 ; 170 '; 222 ) is formed with a channel geometry, wherein the fluid channel in the main extension direction with respect to the axis of rotation azimuthal and / or radial components; a facility ( 140 . 142 . 144 ) for acting on the fluid channel ( 12 ; 40 ; 70 ; 120 ; 170 ; 170 '; 222 ) at a rotational speed and / or a time-varying rotational speed about the axis of rotation for driving fluid by the force of the bulb and / or centrifugal force through the fluid channel; wherein the channel geometry and the rotational speed are set such that the Eulerkraft and / or centrifugal force due to the channel geometry causes a velocity profile over the channel cross-section through which different Coriolis forces are exerted on the fluid over the channel cross-section, so that from a fluid arrangement of a first fluid and a second fluid at the channel inlet ( 14 ; 52 ; 72 ) a fluid arrangement at the channel outlet ( 16 ), in which the diffusive mixing time between the first fluid and the second fluid with respect to the fluid arrangement at the channel inlet ( 14 ; 52 ; 72 ), wherein the first and the second fluid in the fluid arrangement at the channel outlet have a larger contact surface to one another than in the fluid arrangement at the channel inlet. Apparatus according to claim 1 or 2, wherein the fluid assembly at the fluid outlet a larger number of fluid layers than the fluid assembly at the fluid inlet. Device according to one of claims 1 to 3, wherein the fluid channel ( 40 ; 70 ) a plurality of fluidically connected partial channels ( 46a - 46d ; 74a - 74c ) having. Device according to Claim 4, in which the fluid channel ( 40 ) a first channel section ( 42 ) between the channel inlet ( 52 ) and a first branch ( 44 ), at which the fluid channel into the plurality of sub-channels ( 46a - 46d ) and the plurality of subchannels ( 46a - 46d ) having. Device according to Claim 5, in which the channel geometry of the first section ( 42 ) of the fluid channel ( 40 ) and the rotational speed are set such that from a first number of layers of the first and second fluids at the channel inlet ( 52 ) is generated a second number of layers of the first and second fluid before the first branch, which is greater than the first number. Apparatus according to claim 5 or 6, wherein the fluid channel ( 40 ) further comprises a second channel section ( 50 ) between a second branch ( 48 ) at which the plurality of subchannels ( 46a - 46d ) are merged into a fluid channel, and having the channel outlet. The apparatus of claim 7, wherein the channel geometry of the plurality of subchannels and the rotational speed are set such that a plurality of layers of the first and second fluids prior to the first branch have a number of layers of the first and second fluids after the second branch. 48 ) which is greater than the number of layers before the first branch ( 44 ). Device according to one of claims 1 to 8, wherein the fluid channel ( 120 ; 170 ; 170 ' ) extending from a radially inner portion to a radially outer portion, possibly supplemented by azimuthal segments, in the rotational body ( 124 ; 140 ) is formed. Apparatus according to claim 8, further comprising a first reservoir ( 128 ; 146 ) for the first fluid and a second reservoir ( 130 ; 148 ) for the second fluid fluidly connected to the channel inlet and for rotation with the rotary body ( 124 ; 140 ) are formed. Apparatus according to claim 10, wherein the first and second reservoirs ( 128 . 130 ; 146 . 148 ) rotationally symmetrical with respect to the axis of rotation ( 150 ) are arranged. Device according to one of claims 8 to 11, wherein the channel outlet at a radially outer end of the Ro tationskörpers ( 140 ) is arranged so that fluid upon rotation of the rotary body ( 140 ) is drivable by the centrifugal force from the channel outlet. Apparatus according to claim 12, further comprising a receptacle ( 164 ) having a wall ( 160 ), which with respect to the rotational body ( 140 ) is arranged such that fluid driven from the channel outlet to the wall ( 160 ) meets. Device according to one of claims 9 to 13, wherein the rotary body ( 140 ) a plurality of fluid channels ( 170 ), which extends from a radially inner portion to a radially outer portion of the rotational body (FIG. 140 ). Rotational body ( 140 ) having the following features: a rotation axis ( 150 ); a closed fluid channel formed therein between a channel inlet and a channel outlet ( 170 ; 170 ' ) having a channel geometry, wherein the fluid channel in the main extension direction with respect to the axis of rotation has radial components; wherein the channel geometry of the fluid channel is set such that upon rotation of the Rotationskör pers with a given rotational speed about the axis of rotation causes the force acting on a fluid in the fluid channel centrifugal force due to the channel geometry a velocity profile over the channel cross-section, are exerted over the channel cross section under different Coriolis forces on the fluid, so that from a fluid arrangement of a first fluid and second fluid at the channel inlet, a fluid assembly is created at the channel outlet, wherein the diffusive mixing time between the first fluid and the second fluid relative to the fluid assembly is reduced at the channel inlet wherein the first and the second fluid in the fluid assembly at the channel outlet have a larger contact surface than in the fluid arrangement at the channel inlet. Rotational body ( 220 ) having the following features: a rotation axis; a closed fluid channel formed therein between a channel inlet and a channel outlet ( 222 ) having a channel geometry, wherein the fluid channel in the main direction of extension with respect to the axis of rotation azimuthal and / or radial components; wherein the channel geometry of the fluid channel is set such that upon rotation of the rotary body at a given rotational speed and / or rate of rotation about the axis of rotation, the centrifugal force and / or the orbital force acting on a fluid in the fluid channel causes a velocity profile across the channel geometry Channel cross-section causes, are exerted by the over the channel cross section different Coriolis forces on the fluid, so that from a fluid arrangement of a first fluid and a second fluid at the channel inlet, a fluid arrangement is generated at the channel outlet, wherein the diffusive mixing time between the first fluid and the second fluid is reduced with respect to the fluid arrangement at the channel inlet, wherein the first and the second fluid in the fluid arrangement at the channel outlet to a larger contact surface to each other than in the fluid arrangement at the channel inlet. A method of producing a fluid assembly of fluids, comprising: providing one between a channel inlet ( 14 ; 52 ; 72 ) and a channel outlet ( 16 ) closed fluid channel ( 12 ; 40 ; 70 ; 120 ; 170 ; 170 ' ) having a channel geometry, wherein the fluid channel in the main extension direction with respect to the axis of rotation has radial components; Producing a fluid arrangement of a first fluid and a second fluid at the channel inlet ( 14 ; 52 ; 72 ); and impinging the fluid passage at a rotational speed about the rotation axis to drive the first fluid and the second fluid by centrifugal force through the passage (FIG. 12 ; 40 ; 70 ; 120 ; 170 ; 170 ' ); wherein the channel geometry and the rotational speed are set such that the centrifugal force due to the channel geometry causes a velocity profile across the channel cross section through which different Coriolis forces are exerted on the fluid over the channel cross-section so that the fluid arrangement of the first fluid and the second fluid at the channel inlet ( 14 ; 52 ; 72 ) a fluid arrangement at the channel outlet ( 16 ), wherein the diffusive mixing time between the first fluid and the second fluid is reduced with respect to the fluid assembly at the channel inlet, the first and second fluid having a greater contact area with the fluid assembly at the channel outlet than the fluid assembly at the channel inlet. A method of producing a fluid assembly of fluids, comprising: providing one between a channel inlet ( 14 ; 52 ; 72 ) and a channel outlet ( 16 ) closed fluid channel ( 12 ; 40 ; 70 ; 120 ; 170 ; 170 ' ) having a channel geometry, wherein the fluid channel in the main direction of extension with respect to the axis of rotation azimuthal and / or radial components; Producing a fluid arrangement of a first fluid and a second fluid at the channel inlet ( 14 ; 52 ; 72 ); and impinging the fluid channel with a rotational speed and / or a time-varying rotational speed for driving the first fluid and the second fluid through the channel by centrifugal force and / or elliptical force. 12 ; 40 ; 70 ; 120 ; 170 ; 170 ' ); wherein the channel geometry and the rotational speed and / or time-varying Rotationsge speed are set such that the centrifugal force and / or Eulerkraft due to the channel geometry causes a velocity profile over the channel cross-section through which different over the channel cross-section Coriolis forces are exerted on the fluid, so that from the fluid arrangement of the first fluid and the second fluid at the channel inlet ( 14 ; 52 ; 72 ) a fluid arrangement at the channel outlet ( 16 ), in which the diffusive mixing time between the first fluid and the second fluid is reduced relative to the fluid arrangement at the channel inlet, wherein the first and the second fluid in the fluid arrangement at the channel outlet ( 16 ) have a larger contact area with one another than with the fluid arrangement at the channel inlet.